Guia de Usuario de Proii

PRO II USER’S GUIDE

Release 8.0

License and Copyright Information PRO/II 8.0 The software described in this guide is furnished under a written agreement and may be used only in accordance with the terms and conditions of the license agreement under which you obtained it. The technical documentation is being delivered to you AS IS and Invensys Systems, Inc. makes no warranty as to its accuracy or use. Any use of the technical documentation or the information contained therein is at the risk of the user. Documentation may include technical or other inaccuracies or typographical errors. Invensys Systems, Inc. reserves the right to make changes without prior notice. Copyright Notice © 2006 Invensys Systems, Inc. All rights reserved. No part of the material protected by this copyright may be reproduced or utilized in any form or by any means, electronic or mechanical, including photocopying, recording, broadcasting, or by any information storage and retrieval system, without permission in writing from Invensys Systems, Inc. Trademarks PRO/II and Invensys SIMSCI-ESSCOR are trademarks of Invensys plc, its subsidiaries and affiliates. AMSIM is a trademark of DBR Schlumberger Canada Limited. Visual Fortran is a trademark of Intel Corporation. RATEFRAC® software is a trademark registered to Koch-Glitsch. This applies to all printed and electronic documents. BATCHFRAC® software is a trademark registered to Koch-Glitsch. This applies to all printed and electronic documents. Windows 98, Windows ME, Windows NT, Windows 2000, Window 2003, Windows XP and MS-DOS are trademarks of Microsoft Corporation. Adobe, Acrobat, Exchange, and Reader are trademarks of Adobe Systems, Inc. All other products may be trademarks of their respective companies.

U.S. GOVERNMENT RESTRICTED RIGHTS LEGEND The Software and accompanying written materials are provided with restricted rights. Use, duplication, or disclosure by the Government is subject to restrictions as set forth in subparagraph (c) (1) (ii) of the Rights in Technical Data And Computer Software clause at DFARS 252.227-7013 or in subparagraphs (c) (1) and (2) of the Commercial Computer Software-Restricted Rights clause at 48 C.F.R. 52.227-19, as applicable. The Contractor/Manufacturer is: Invensys Systems, Inc. (Invensys SIMSCI-ESSCOR) 26561 Rancho Parkway South, Suite 100, Lake Forest, CA 92630, USA. Printed in the United States of America, June 2006

Table of Contents

Chapter 1 Using PRO/II .............................................................................9 Starting PRO/II...................................................................................................9 Compatibility with Previous Versions...............................................................11 PRO/II Main Window Components..................................................................12 Manipulating the PRO/II Window.....................................................................13 Working with On-screen Color Coding Cues...................................................14 Using the Menus..............................................................................................14 Using the Floating Palettes..............................................................................18 Using the Toolbar Buttons ...............................................................................18 Using the PRO/II Main Window .......................................................................22

Chapter 2 Simulation Basics...................................................................23 General Approach............................................................................................23 Building the Flowsheet.....................................................................................25 Required Data..................................................................................................26 Default Data...................................................................................................28 Optional Data.................................................................................................29

Chapter 3 Managing PFD Files...............................................................31 Opening a New Simulation ..............................................................................31 Opening an Existing Simulation.......................................................................32 Saving the Current Simulation.........................................................................32 Closing a Simulation ........................................................................................34 Deleting a Simulation.......................................................................................34 Copying a Simulation.......................................................................................35 Importing a PRO/II Keyword Input File ............................................................37 Exporting Simulation Data to a PRO/II Keyword File ......................................41 Simulation Data to Keyword File .....................................................................42 Using the Spreadsheet Tools ..........................................................................43 Exporting the Flowsheet Drawing to the Clipboard .........................................44 Exporting Stream Property Table Data............................................................44 Copying Stream Property Table Data to the Clipboard ...................................45 Exporting the PFD to an AutoCAD or PostScript File......................................46

Chapter 4 Building a Flowsheet ..............................................................47 Setting Simulation Preferences .......................................................................47 Placing a Unit on the Flowsheet ......................................................................57 Drawing Streams .............................................................................................60 Searching for a Unit or Stream ........................................................................64 Changing the Flowsheet Layout ......................................................................65 Drawing Freehand Objects..............................................................................66

Chapter 5 Manipulating Objects..............................................................71 Selecting Objects or Groups of Objects ..........................................................71 Resizing an Object...........................................................................................74 Rearranging Objects or Groups of Objects .....................................................75 Editing Text......................................................................................................77

Chapter 6 Viewing Flowsheet Contents..................................................79 Scrolling the PFD.............................................................................................79 Zooming...........................................................................................................79 Opening Multiple Viewport Windows ...............................................................80 Redraw the Simulation.....................................................................................81 Panning............................................................................................................81

Chapter 7 Data Entry Windows................................................................85 Defining the Simulation....................................................................................85 Data Entry Windows for Unit Operations.........................................................94

Chapter 8 Specifying Component, Thermodynamic and Stream Data .101 Component Data............................................................................................101 Thermodynamic Data ....................................................................................112 Stream Data...................................................................................................126 Refinery Inspection and User-defined Properties..........................................139 BVLE (Validating Equilibrium Data)...............................................................146

Chapter 9 Unit Operations and Utility Modules.....................................148 Calculator.......................................................................................................150

FORTRAN Statements ..........................................................................155 Sample Calculator Procedures.............................................................163

CAPE-OPEN..................................................................................................167 Column, Batch ...............................................................................................171 Column, Distillation ........................................................................................172

Column, Liquid–Liquid Extraction ..................................................................191 Column, Side .................................................................................................197 Compressor ...................................................................................................200 Controller .......................................................................................................205 Crystallizer .....................................................................................................208 Cyclone..........................................................................................................212 Depressuring Unit ..........................................................................................219 Dissolver ........................................................................................................224 Excel Unit.......................................................................................................225 Expander .......................................................................................................231 Flash ..............................................................................................................233 Flash With Solids ...........................................................................................237 Flowsheet Optimizer ......................................................................................238 Heat Exchanger, LNG....................................................................................244 Heat Exchanger, Rigorous.............................................................................246 Heat Exchanger, Simple................................................................................256 Heating/Cooling Curves.................................................................................260 Mixer ..............................................................................................................264 Multivariable Controller ..................................................................................265 Phase Envelope.............................................................................................268 PIPEPHASE Unit Operation ..........................................................................270 Pipe................................................................................................................273 Polymer Reactor ............................................................................................278 Procedure Data..............................................................................................280 Pump..............................................................................................................288 Reaction Data ................................................................................................289 Reactor ..........................................................................................................293 Reactor, Batch ...............................................................................................307 Solid Separator ..............................................................................................308 Splitter............................................................................................................309 Stream Calculator ..........................................................................................311 SPEC/VARY/DEFINE....................................................................................314 User-added Unit Operations..........................................................................327 Electrolyte Module .........................................................................................332 Simsci Add-on Modules.................................................................................335 Valve..............................................................................................................339 Wiped Film Evaporator ..................................................................................340

Chapter 10 Running and Viewing a Flowsheet.....................................341 Using the Run Palette....................................................................................341 Checking the Simulation Status.....................................................................343 Understanding the Unit Color Coding Cues ..................................................344 Running the Simulation..................................................................................345 Viewing Calculation History ...........................................................................349 Viewing Results .............................................................................................349 Viewing Results in Stream Property Tables ..................................................350 Running a Case Study...................................................................................353 Viewing Case Study Results .........................................................................355 Running Files in Batch Mode.........................................................................355

Chapter 11 Printing and Plotting ............................................................361 Defining Output Format .................................................................................361 Generating a Report ......................................................................................368 Viewing a Report ...........................................................................................369 Printing a Report............................................................................................369 Plotting...........................................................................................................369 The Plot Viewer .............................................................................................373 Setting Up the Printer ....................................................................................374 Printing a Flowsheet Layout ..........................................................................374

Chapter 12 Customizing the PFD Workplace ........................................375 Changing Unit Style .......................................................................................375 Changing Stream Style..................................................................................378 Modifying Drawing Preferences.....................................................................386 Specifying a Default Editor ............................................................................387 Changing the Default Font.............................................................................387

Index ......................................................................................................389

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8 PRO/II USER GUIDE JUNE 2006

Chapter 1 Using PRO/II This chapter describes how to start and exit PRO/II. In addition, it reviews some basic Windows features as they appear in PRO/II and briefly describes how to use them. Starting PRO/II If you have not yet installed PRO/II on your system, see the PRO/II PC/LAN Installation Guide. If you do not see a PRO/II icon in a SIMSCI group window or in your Program/SIMSCI Start menu, see the troubleshooting section in the PRO/II PC/LAN Installation Guide.

To start PRO/II:

information on

opening files and on the color codes used in the program.

Double-click on the PRO/II icon or launch from the Start menu. The PRO/II welcome window appears. This window contains

Chapter 1 USING PRO/II 9

Figure 1-1: The PRO/II Welcome Window

Click OK to exit the window. The PRO/II main window will appear.


Figure 1-2: The PRO/II Main Window

You can now open a new simulation file (select File/New), open an existing file (select File/Open), or import a keyword file (select File/Import). See Chapter 3,Managing PFD Files, for additional details.

ompatibility with Previous Versions

O/II can re rsions of PRO/II. When you open a sim rsion, the file is

rted to the cur a different name created

by PRO/II version 6, the conv a copy of the original file will be saved as “G3_v60.prz”.

t fil atures that are not supported by the al user interface. PRO/II issues a

hen this occurs. Fo reserved if you choose either the Read subsequently export the prob features will be lost. The

C

This release of PR ad simulation files created by previous veulation file created by a previous ve

automatically convesaved unde

rrent version and a copy of the original file is . For example, if you open G3.prz that waserted file will be saved as “G3.prz” and

Note: Some keyword inpu es that were created manually may include fe

PRO/II graphicwarning w r flowsheet execution, all features will be p

Only or Run Batch mode. In all cases, if youlem, all supported


exported file will not include any of the unsupported features. Later import of the file will reveal that th lways

prudent to make copies of yo f the

PRO/II Main Window Compo

exported e unsupported features are missing. It is aur original files and to work only on copies o

original files.

nents

Component Description Control Menu Box

d closing the active window. Displays a menu with commands for sizing, moving an

Title Bar Identifies the application and the name of thopen file; can be used to move the entire window.

e

Minimize Button Reduces the application window to an icon.

Maximize/Restore Button nlarges a window to full screen or restores it to E

its default size Menu Bar

tput, Tools, Draw, View, Options, indow and Help.

Identifies the menus available in PRO/II: File, Edit, Input, OuW

oolbar Provides push button access to various Edit, Input, Tools, View, Window, and Help options

T

PFD Main Window Provides a workspace for placing units, making

stream connections, drawing objects, and adding text.

Horizontal Scroll Bar Functions as a sliding scale for moving the flowsheet to the right or left in the PRO/II main window.

Vertical Scroll Bar Functions as a sliding scale for moving the flowsheet up or down in the PRO/II main window.

Status Bar Displays help, information and error messages for the active feature or object.

Border Handles Changes window height, width, or size when the corresponding border handle is dragged to a new position.


Manipulating the PRO/II Window The PRO/II window offers many features that enable you to customize its

reen and other applications. Detailed graphical user interface may be found in

u erous reference manuals available at any large bookstore.

ze and orientation, others enable

appearance, relative to the full scstructions on use of the Windows’ in

n m Changing Window Size The Windows interface provides tools for resizing each window. Some tools utomatically change a window to a particular sia

you to control the magnification. Using Minimize/Maximize Buttons

he minimize and maximize buttons aT utomatically adjust the size of a window.

sing the Control Menu

sing Border Handles U

You can use the window border to change the size of the main window. The border works like a handle that you can grab with the cursor and drag to a new position. U

You can also use the Control menu to Restore, Move, Size, Minimize, or

window. Open the Control mthe title bar or by pressi

hanging Window Position

position of the main window (or any pop-up indow) by dragging the title bar.

Maximize a left of

enu by clicking the PRO/II icon at the far ng <Alt+Space>.

C You can change thew


orking with On-screen Color Coding CW

ues

PRO/II provides the standard visual cue (grayed out text and icons) for menu items and toolbar buttons that are currently unavailable. In addition, PRO/II uses colored borders liberally to indicate the current status of the simulation. You may customize the color coding by accessing the Set Colors window by selecting Options/Colors… from the menu bar. PRO/II On-Screen Color Codes

Color Significance Red Required data

Actions or data required of the user

Green

Optional or default data

Blue

Data supplied by user

Yellow

Questionable data. A warning that the value supplied by user is outside the normal range.

Gray Data field not available to user

Black

Data entry not required

Using the Menus The names of the PRO/II main menus appear on the menu bar. Use these me O/II operations.

nus to access most PR


Figure 1-3: File Menu

Figure 1-4: Edit Menu


Fi ure 1-6: Output Menu g

Figure 1-5: Input Menu

Figure 1-7: Tools Menu


Figure 1-8: Draw Menu

Figure 1-10: Options Menu

Figure 1-9: View Menu

Figure 1-11: Window Menu

Figure 1-12: Hel

p Menu


Using the

he firs ams eeded to The se e

simulation. These palettes may be displView/Palettes from the menu bar.

Floating Palettes

There are two floating paln

ettes. Tconstruct a flowsheet.

t contains the unit operations and strecond contains controls used to run thayed or hidden by selecting

Menu Item

Description

View/Palettes/PFD Checking this option displays the PFD palette t wn

as the Streams nit palette).

containing uni operations and streams (also kno/U

View/Palette g s/Run Allows runnin

the simulation and viewing results.

sing the

he ain t yed in th en

ayed i iew/Too ven groups of buttons are visible. Toolbar bu the

enus on t

New, Open, Save, Print and PriMultiple View and PFD Palette

Data Entry Window buttons Go To buttons VLE Tool buttons Ru Delete and View buttons Help button

Using the Multiple View and PFD Palette Buttons

These butt u to open multi d hide or display the floating PFD palette.

U

m

Toolbar Buttons

Tdispl

oolbar can be displan standard format (V

e standard (full) or compact format. lbar/Standard from the menu bar), settons duplicate options available from

Wh

m

he menu bar.

nt Preview uttons b

n/Results buttons

ons enable yo ple views of a single flowsheet an

Button Menu Item Description

window of a single simulation problem.

View/New View Opens another viewport

View/Palette/PFD Displays or hides the

floating PFD palette.


Using the Data Entry Window Buttons

Each Data Entry Window button quick access to the main data entry ow for th section of input.

provides

wind

e selected


Input/Problem Description

Describes the current simulation and relates it to a specific project.

Input/Units of Measure Sets units of measure specific to this simulation. Each new simulation extracts defaults from the default Unit of Measure Set.

Input/Component

Selection Specifies the compcomponents for the current si

onents and pseudo mulation.

Input/C perties

Supplies perties. omponent Pro component pro

Input/Thermodynamic Data

Selects thermodynamic methods for the current simulation.

Input/Assay Characterizati

cutpoints and characterization options for generating pseudo components from Assay streams.

on Modifies TBP

Input/Reaction Data Defines reactions and provides heat of

reaction, equilibrium, or kinetic data for reaction sets.

Input/Procedure Data Use this window to create or delete Procedure blocks in order to calculate kinetic reaction rates.

Input/Casestudy Data Allows user to perform studies on a base case solution by altering parameters and rerunning.

Input/Calculation Sequence

Specifies a user-defined calculation sequence.

Input/Recycle Convergence

Specifies user-defined recycle convergence and acceleration options.

In eam Property List

User ticular stream property tabl as the toggle stream property list.

put/Toggle Str

can select a pare


s g Go uttons

he Go To buttons enable you to jump to a selected unit or stream. PRO/II positions wsheet to p r of the

main window. The Stream Lis ist (Go To) windows also allow direct ata ntry and review of output results for the selected stream or unit.

U

T

in To B

re

d e

the flo lace the selected unit or stream at the centet and Unit L


flowsheet.

View/Pan View Allows quick panning through the entire

flowsheet. By selecting a name, you can jump directly to that unit.

View/Unit List Displays a list of units in the current

View/Stream List Displays a list of streams in the current sheet. By selecting a nam p ctly to that stream.

flowdire

e, you can jum

Using VLE Tools Buttons

The VLE Tools buttons enable you to perform simulation functions, e.g., flash, a tream high sh H

s lighted on the PFD using the Fla ot-key.


Tools/Flash Stream Flashes the sPFD. (Also ca

tream highlighted on the lled the Flash Hot-key)

Tools/Binary VLE Generates pl les of K-values

n

ots and taband fugacityof compone

coefficients for binary pairs ts.

Using Run/Results Buttons

icate functions on the Run Simulation floating stop a simulation or permit viewing results and

ates an Output menu

The Run/Results buttons duplalette. They allow you to run,p

generate output reports. The Generate Output button duplicm. ite



-------- Runs the sim

ulation

n -------- Stops the simulatio

-------- Allbe vie

ows results for the selected stream or unit to wed.

Output/Generate Report

Generates an output report for the simulation problem.

Using Delete and View Buttons PRfacav

O/II provides a Delete button and a set of View buttons on the toolbar that ilitate editing and viewing of the flowsheet. These buttons duplicate items ailable on the Edit and View menus.


Edit/Delete or <Delete>

Deletes the currently selected object(s) from the flowsheet.

View/Zoom/Zoom In, Zoom Out

Zooms in or out of the flowsheet.

View/Zoom/Zoom Full or <Home>

Displays the entire flowsheet in the PFD window.

View/ Zoom/Zoom Area

Displays the selection rectangle used to select a set of units, streams or objects on the flowsheet. The selected area fills the PFD.

View/Zoom/Redraw or <Shift+Home>

Clears the PFD of any extraneous object by redrawing the flowsheet.


Using the Help Button The What Is? Help button displays context-sensitive help.


What Is? Displays help for the object you point to.

Using the PRO/II Main Window The PRO/II main window (PFD) is the main drawing board. You may place the following objects on the PFD:

Unit operations from the PFD palette Stream connections Text Drawings Stream property tables

Use the PRO/II main window to see the contents of your simulation. You can choose to view the entire flowsheet or only a portion of it. You control the view using scroll bars, pan options, the zoom bar, or arrow keys. Note: See Chapter 5, Manipulating Objects, for information about placing, selecting and changing the size of objects in the PFD.


Chapter 2 Simulation Basics In the previous chapter, you learned some of the basic window features of PRO/II. In this chapter, you will learn simulation basics; that is, how to set up simulation problems, solve them, and analyze the results. General Approach This chapter provides a quick overview of the use of PRO/II for solving engineering problems. A suggested basic approach is given as well as helpful explanations of the information flow in PRO/II. Sample data entry windows are given to illustrate data entry for PRO/II. Step-by-step examples are available in the PRO/II Tutorial Guide. Online help is also available. You have already learned that PRO/II gives you great flexibility and numerous options when supplying simulation data. For many items of data, default values are supplied. A color code informs you when data are required, supplied by default, out of normal ranges, or missing. Note: You must supply data for all red-bordered fields or red-linked text (including data required) before running your simulation. Problem data may be supplied in almost any order: PRO/II warns you when required data are missing. However, it is still best to follow a logical path when supplying simulation data. For example, some options such as stream compositions are dependent upon the components selected. Some unit operations, such as the flash drum, have features that are dependent on the thermodynamic data. For some other unit operations, performance specifications based on the components in the system are the preferred way to define the operation. For these reasons, the following approach is recommended when building a simulation flowsheet. Draw the Flowsheet Select the unit operations needed for the flowsheet calculations and position them on the PRO/II PFD main window.

Chapter 2 SIMULATION BASICS 23

Connect the Unit Operations with Streams The streams are the connectors for the process calculations, with information passed from one unit operation to another via the process streams. Define the Components in Your System It is best to order the components in volatility order, starting with the lightest component. This makes it easy to analyze the separations which occur in unit operations such as distillation. While not a necessity, for hydrocarbon/water systems, defining water as the first component is also a good idea. This makes it easy to see the break between the aqueous and nonaqueous phases. User-defined petroleum pseudocomponents and/or polymer components for which you supply data should be entered next. Petroleum pseudocomponents generated by PRO/II from petroleum stream assay data will appear last in the component lists of the output reports. Select the Thermodynamic and Transport Property Methods For many problems, a system may be selected from the Most Commonly Used thermodynamic methods. Guidelines for thermodynamic methods are provided in the PRO/II online help, and in the PRO/II Reference Manual (both in online help and in hardcopy forms). Further assistance is available through SIMSCI – ESSCOR Technical Support. Selecting a proper thermodynamic method is a critically important step in the solution of a simulation problem. Supply Data for the Feed Streams and Recycle Streams You must supply thermal conditions, flowrates, and compositions for all external feed streams to the flowsheet. It is usually desirable, although not necessary, to provide estimated data for recycle streams to speed convergence of recycle calculations. Supply Operating Conditions for the Unit Operations Double-click the icon for each unit operation to access the data entry windows. The color codes tell you what data you must supply and what data have default values. You may also use the online help to learn more about the calculation options, data entry items, etc., for each unit operation. A quick review is also a good idea at this point. Do the thermodynamic methods support the unit operation calculations? Are transport properties required for any of the unit operations?


Run the Process Simulation PRO/II lets you know, by color code, when sufficient information has been supplied to perform the calculations. When all of the borders on the toolbar icons have changed from red (indicating missing data) to green or blue, you are ready to run your simulation. At this point, you may click the Run (right arrow) icon on the toolbar or the Run button on the floating Run palette to begin the flowsheet calculations. Analyze the Simulation Results Use the many convenient report and plotting features of PRO/II to analyze the simulation results. At this point, your training as an engineer should take charge. Are the results reasonable? How do the results compare with the plant data? Can differences be reconciled? Are better data for the feedstocks needed? Are the models adequate for the intended purposes? Now that we have presented an overall plan for simulating a flowsheet, let’s look at some of the individual steps in more detail. Building the Flowsheet Unit Operations Use the floating PFD palette to begin building the flowsheet. The icons and names for the unit operations appear as buttons on the PFD palette. To add a unit operation to the flowsheet, click the unit icon on the PFD palette and click-drop it at the desired location on the flowsheet. Streams Click the Streams button on the top of the floating PFD palette. The PFD is now in stream mode and a small “S” is attached to the cursor. You will notice that all possible exit ports for each unit operation are now marked. Required outlet ports are colored in red; green is used to mark optional ports. PRO/II adds each stream to the flowsheet in an orthogonal manner, following a rectangular grid pattern. As soon as a valid flowsheet has been built, i.e., all required inlet, outlet, and connector streams have been added for all the process units, the red border around the Streams button on the PFD palette changes to blue.


Required Data Now that the flowsheet has been built, it’s time to supply the required data for the calculations: the components and thermodynamic methods must be defined, inlet feed streams and, optionally, recycle streams must be supplied, and the operating conditions for the unit operations must be specified. Components To define the components, select Input/Component Selection from the menu bar or click on the benzene ring toolbar icon to open the Component Selection main window. Note that this icon has a red border, indicating that components have ot yet been defined. n

Library components for which the library access names are known may be directly typed into this window, where they are transferred to the List of Selected Components for the problem. A convenient search procedure is also provided which may be used by clicking Select From Lists… . Petroleum (PETRO) components are defined in the Petroleum Components window, which is reached by clicking Petroleum…. Non-library components can be defined in the User-defined window which is reached by clicking User-defined…. Note that petroleum pseudocomponents defined by PRO/II from petroleum tream assay data do not appear in the Component Selection main window. s

hermodynamic Methods T

Thermodynamic methods are defined in the Thermodynamic Data main window which is reached by selecting Input/Thermodynamic Data from the menu bar or by clicking on the phase diagram icon. Note that this icon is initially outlined in red, indicating that thermodynamic methods must be defined or the problem. f

For most problems, a predefined set of thermodynamic methods for calculating K-values, enthalpies, entropies, and densities may be used. PRO/II offers numerous Categories of method sets. After a category has been selected, you may select a method set within that category as a Defined System for the problem and modify it by clicking Modify… to access the Thermodynamic System-Modification window. Note that transport property calculations are not included in the predefined method sets. If they are required for the problem, you

ust add them to the predefined thermodynamic method set in this window. m


Stream Information The identifiers for feed streams requiring input data are marked with red borders indicating that information is missing. Stream information is supplied in the Stream Data main data entry window which is reached by double-clicking a stream identifier. The predefined stream identifier may also be changed in this window. Three types of information must be supplied in this window: the thermal condition of the stream, the flowrate for the stream, and the composition of the stream. For petroleum assay streams, the assay data are provided instead of the composition data, and PRO/II defines the stream composition for you in terms of petroleum pseudocomponents. Although optional, it is good practice to provide reasonable estimates for recycle tear streams in order to accelerate convergence of problem recycle calculations. Unit Operations Unit operation identifiers for which data entries are needed are marked with red borders. To enter information for a unit operation, double-click its icon to retrieve the Unit data entry window. Various input options and numeric values are supplied via this parent window and its child windows. Required information is always bordered in red; data entry fields for items with supplied defaults are always bordered in green. After you have supplied information in a data entry field, the border color changes to blue. Information you have supplied which lies outside the normal range for the field is marked with a yellow border. You may also change the default unit identifier in this window and furnish a longer, more descriptive name for the unit operation. Notice that when you return to the flowsheet, the unit identifier on the PFD has a black instead of red border, signifying that all data entry requirements are satisfied. If the border is still red, you must return to the data entry window for that unit operation and supply the missing data. Miscellaneous Data All data entries in this category are optional. PRO/II provides default entries. In some cases, global values may be used to supply the defaults, as explained in Chapter 4, Building a Flowsheet. Miscellaneous data categories include problem descriptive information, the calculation sequence, recycle convergence options, flowsheet tolerances, and the scaling of product streams.


Problem descriptive information is optional; however, it can be beneficial to document a simulation model for future users. This information includes a project name, problem name, user name, date, site, and problem description. This information is supplied in the Problem Descriptive Information window, which is

accessed by clicking the toolbar icon with the printed page icon or by electing Input/Problem Description from the ms enu bar.

For most problems, the calculation order determined by PRO/II is satisfactory. To

supply your own sequence, click the toolbar icon with the two connected lowsheet blocks or select the Input/Calculation Sequence from the menu bar. f Definitions of recycle loops are automatic. To define your own loops, or to use

acceleration techniques, click the toolbar icon with the flowsheet loop iconenter the Problem Recycle Convergence and Acceleration

to Options window or

elect the Input/Recycle Convergence from the menu bar.

ch reached by choosing Input/Flowsheet Tolerances from the menu bar.

for a

s Flowsheet tolerances are used for convergence of unit operation specifications and may be changed in the Default Unit Specification Tolerances window, whiis All flowsheet results may be scaled so that a desired flow is obtained product stream. To use the scaling feature, select the Output/ReportFormat/Miscellaneous Data. Click Product StreamScaling… on the Miscellaneous Report Options window to access the Scale Stream Flowrate

indow.

efault Data

ays supply are indicated with a color d because they have no default values.

et

xt is also changed to blue, indicating at you have replaced the default value.

w D To simplify data input, PRO/II supplies default options and values wherever practical. Default values supplied by PRO/II are printed in black in a data entry field with a green border, or in the case of linked text, in green. For example, thedefault number of iterations for a column unit operation using the IO method is supplied as 15. Entries which you must alwre While you do not need to replace a default entry to satisfy the input requirement for PRO/II, default data should be inspected carefully to ascertain that they meyour requirements. When you replace a default value, the border color for the data entry field changes to blue, indicating that you have supplied this value. For linked-text strings, the color of the linked teth


Optional Data Optional data, which are displayed in black, are data or options not specifically necessary for the unit operations to proceed. For example, the Description entry is optional for all unit operations. A reboiler is optional for the Column unit operation, since the calculation requirements may also be satisfied by a vapor

mn reboiler, the data entry fields for a ermosiphon reboiler are colored gray.

feed to the bottom tray of the column. Data options which do not apply to a particular combination of input data appear in the color gray, and are not available for data entry. For example, when the ettle reboiler option is selected for a coluk

th


T

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Chapter 3 Managing PFD Files This chapter describes how to open, save, close, delete and copy simulation files. In addition, this chapter outlines how to import a PRO/II keyword input file or export a flowsheet. Opening a New Simulation When you start PRO/II, the program does not automatically bring up a new, untitled simulation. Note: If you want PRO/II always to open with a new simulation, select Options/New File on Startup from the menu bar. To open a new simulation:

Choose File/New. . . from the menu bar. PRO/II clears the main window for a new simulation and opens the initial viewport window, View 1.

Figure 3-1: PRO/II Main Window

Chapter 3 MANAGING PFD FILES 31

Opening an Existing Simulation You can open any previously saved simulation for modification, viewing or printing. PRO/II opens the flowsheet file and its supporting PRO/II database files. To open an existing simulation:

Choose File/Open... from the menu bar. PRO/II displays the Open Simulation window.

Figure 3-2: Open Simulation Window

n file.

Before you close a simulation, you should save it. You may also want to save the simulation periodically while creating it.

Type or select the name of the simulatio Click Open or press <Enter>. PRO/II displays the simulation in the PFD

main window. Note: PRO/II 7.x provides a file converter for import of PRO/II 4.x files with the exception of Add-On Module files. Saving the Current Simulation


To save the current simulation:

Choose File/Save from the menu bar. If you have not previously saved this simulation, PRO/II displays the Save As window.

Note: PRO/II 5.x automatically compresses the three PRO/II database files (*.pr1, *.pr2, *.pr3) and the simulation flow diagram file (*.sfd) into a single *.prz file. Beside reducing the size of stored files, PRO/II file compression assures that a complete set of files for each simulation has been saved.

Figure 3-3: Save As Dialog

Type a name for this simulation. Click Save or press <Enter>.

ates a backup file at ser-specified intervals from which recovery can be made. If you close or exit the

Note: The PRO/II Autosave functionality automatically creusimulation without saving, this backup file is deleted. Select Options/Simulation Defaults/Autosave… from the menu bar to access the Autosave Options window.

av

e. Changes you made to the imulation since the last save are saved as part of the simulation, under its new

nam

S ing a Simulation to Another Name You can save a simulation to another nams

e.


Not : If you’ve made changes to a simulation and don’t want to alter the original

ave As.

o save the current simulation to another file name:

esimulation, but do want to keep the changes, use S T

Choose File/Save As... from the menu bar.

file name.

the menu bar.

If you close a simulation without first saving the simulation files, you lose any changes you made to the simulation since the last save.

eleting a Simulation You can e current (active) simulation at any time.

:

PRO/II prompts you for a new

Type a name for the simulation. Click Save or press <Enter>.

PRO/II appends a .PRZ extension to the filename. Closing a Simulation You should save a simulation before closing it, although PRO/II will prompt you

save changes for an existing simulation. to

o close a simulation: T

Choose File/Close from

D

delete any simulation except th

To delete a simulation file

Choose File/Delete... from the menu bar. PRO/II displays a list of existing PRO/II simulation files.


Figure 3-4: List of Files

Type or select the name of the file you want to delete. (You may not

eletes all files associated with this

opying a Simulation

n copy all files associated with a simulation (one flowsheet and three ting

want to overwrite the xisting file.

o copy a simulation file:

delete the current simulation.) Click Open or press <Enter>. PRO/II dsimulation.

C You cadatabase files) to a target simulation you name. You can copy to new or exisfile. If you copy to an existing file, PRO/II verifies if you e T

Choose File/Copy... from the menu bar.


Figure 3-5: Copying Files

Select the name of the file yo the file selector. (You

may not copy the current simulation.) Enter a name for the copy (ta

Click Open or press <Enter>.

/II copies all files associated with Note: There may be as many as 17 s parate files associated with a single

. These are describ

u want to copy from

rget).

PRO the simulation.

esimulation problem ed in Table 3-1.


Table 3-1: PRO/II Simulation Files

File Extension Description

*.pr1, *.pr2, *.pr3 PRO/II database files

*.sfd Graphics file

*.prz files containing *.pr1, *.pr2, *.pr3 a d *.sfd files

Compressed n

*.out Main output file

*.ot1 Component, calculation sequence,

recycle loops/streams output data

*.ot3 Equipment/streams output data

*.sr1 Input source listing

*.ix3 utput index O

*.hs2 Calculation history

*.inp

Keyword input file

*.plt Plots saved in the plot display window

*.txt Stream property table or plot (saved in ASCII format)

*.csv Stream property table or plot (saved in tabular format)

*.clp Graphics saved in Clipboard format

*.prc Temporary procedure file created and

there is an abnormal termination. removed by PRO/II. Only remains if

Importing a PRO/II Keyword Input File

port an existing PRO/II keyword input file into the PRO/II You can im graphical use en execute the simulation problem just as if you had entered the phical main window. PRO/II automatically con put file into a flowsheet and displays it in the PFD

r interface and thproblem using the PFD graverts the specified keyword in window.


Note: In the previous versions, PFD layout was retained within the *.prz filethe current version, *.sfd file will be generated, when a simulation (PFD) is saved and exported. After the generation of *.sfd file, users can restore the PFD layouusing *.inp file.

. In

t

o import a PRO/II keyword input file:

PRO/II displays a list of ex

T

Choosing File/Import from the menu bar.

isting keyword input files.

Figu

d file that you want to import.

Click Open or press <Enter>.

e into a flowsheet and displays it in e PFD main window automatically.

Keyword Features without PRO/II GUI support The RESTART feature is not supported by the graphical user interface in this version of PRO/II. You will not be allowed to import keyword files that contain this feature.

re 3-6: List of Files

Type or select the name of the keywor

PRO/II converts the selected keyword input filth


If a RESTART keyword is detected upon import, you will be reminded that only

ee Chapter 10, Running and Viewing a Flowsheet, for information on running

n keyword features are not fully supported by the graphical user interface of PRO/II. However, if one of these unsupported features is detected, you will be

ver the GUI interface will operate in the ywords include:

PRO/II program ported features

ill run the file in Run-Only Mode.

In “Ru

ts to the PFD. Add stream property tables to the PFD. Have access to all the capabilities on the Run palette (perform all

interactive execution functions available on the Run palette for both supported/unsupported units, review the calculated results on the PFD for all streams and supported/unsupported units, generate output reports for all features, generate plots for supported features only).

Export the flowsheet and stream property table information to other Windows applications.

Edit the keyword file, reimport, and rerun (without leaving PRO/II). Use the stream flash icon.

In “Run-Only” mode, you cannot:

View simulation data with the data entry windows. This includes Component and Thermodynamic data. Double-clicking on a unit operation or stream will cause a short warning message to be displayed.

the “Run Batch” feature of PRO/II may be used with these keyword input files.Skeyword files in “Batch” mode. Keyword Features that can be imported into PRO/II in “Run-Only” Mode Certai

allowed to import the keyword file, howe“Run-Only” mode. Such unsupported ke

BVLE Data Stream Report Writer

Hydrate Unit Operation HEXTRAN Property Data Generator.

If you attempt to import a keyword input file that contains

atures not supported by the graphical user interface, the unsupfewill be automatically listed in a status window. You have the option to save or delete the unsupported features. If you choose to save the unsupported features,

RO/II wP

n-Only” mode, you can:

Review and modify the PFD graphic image. You may move unit operation icons and streams around to improve the appearance of your PFD.

Add drawing elemen


Perform any input mode functions, including changing the calculation sequence. All buttons and menu options that access simulation data will be disabled.

Perform any of the following functions: adding/deleting units, adding/deleting streams, and reconnecting streams. Export the PRO/II keyword input file.

If you attempt to import a keyword containing an unsupported feature, the following message window will be displayed:

Figure 3-7: Unsupported Features Warning Window

If you click Yes, a message window similar to the following will be displayed: Figure 3-8: Flowsheet Status Window for Unsupported Features Once you close the message window, the interface will be placed to the “Run-Only” mode as illustrated in Figure 3-9.


Figure 3-9: PRO/II in “Run-only” Mode

Click Run on the Run palette.

ote: In the current version, *.sfd file will be generated, when a simulation (PFD) generation of *.sfd file, users can restore the

FD layout using *.inp file.

Once the flowsheet has been solved, you may double-click a unit or stream to view the results. Exporting Simulation Data to a PRO/II Keyword File You can export an existing PRO/II simulation flowsheet to a keyword input file as follows:

Choose File/Export from the menu bar. PRO/II displays the Export window which lists the data export options.

Nis saved and exported. After the P


Figu

Choose the Simulation Data to Keyword File option. Click OK.

RO/II converts the current simulation flowsheet data into a PRO/II keyword put file in ASCII format. The name of the keyword file will be YYY.INP, where

wsheet PRO/II database file.

you to export le. Navigate to the

estination drive and directory of your choice using the Save In: field. Enter the nam utton to complete the

re 3-10: Available Data Export Options

PinYYY.PR1 is the name of the simulation flo Simulation Data to Keyword File This selection opens a special Save As dialog window that allows the input data of the simulation to an ".inp" keyword input fid

e of the output file in the File Name: field. Press the Save boperation.


The any compatible version of the files e the data. Note that the keyword file con In v6.0 and later, the "Simulation Data to Keyword File" option is expanded to incl ck boxes to control exporting stream and column solution data to the eyword file.

is unconverged, then the two " e Run command has not been executed

ince creation or since the last time "Restore Input Data" has been executed,

est for Convergence

hen the user selects either or both of the "Includes", upon "OK" the first thing is in an unconverged er that the data being

on dialog. "No"

ote: Beginning with PRO/II version 5.5, exported flowsheets now write all unit ope past, for keyword input files that it operations listed in the

equence List were exported.

xcluded functionality. ist of Available Unit

perations that excludes unit operations marked excluded at the time of export.

t

Usi t The

t u a side menu.

simulation database to generate reports or perform additional on-

exported keyword file then may be imported intoPRO/II program to rerun the simulation, even on another computer. Keyword also are a very compact way to archivtains all the appropriate data sections (General, Thermodynamics, etc.).

ude chek

If output data exists, even if the solutionInclude" check boxes are enabled. If thsthen these checkboxes are disabled. T Wthat PRO/II must do is test for convergence. If the solutiontate then PRO/II throws up a message box to warn the uss

written to the keyword file is unconverged.

licking on "Yes" will continue to the file name selection commCwill return the user to the Export window. N

rations in the flowsheet to the keyword file. In the had a User-Defined Sequence List, only un

S This change is necessary to support the new Included/ E

RO/II now generates a SEQUENCE statement with a lPOAdditionally in these instances, PRO/II writes a warning into the keyword file advising that the list of unit operations and the SEQUENCE statement do nomatch. These files may cause input processing problems if read into earlier versions of PRO/II.

ng he Spreadsheet Tools

Tools/Spreadsheet menu item can beof c rrently installed tools will appear in

used to start a spreadsheet tool. The lis Spreadsheet tools are Excel template files and macros that can read information

the PRO/II in


the-spot calculations. They can also update data in the simulation database itself

RO e used to properties or component flowrates or generate a dist Exp ard

ort part or all of the flowsheet drawing to the Clipboard. You can en paste this drawing into other Windows applications.

export the entire flowsheet drawing to the Clipboard:

Choose File/Export from the menu bar. PRO/II displays the Export window (Figure 3-10).

Choose the Flowsheet Drawing option. Click OK.

export one page of the flowsheet to the Clipboard:

Select the page to export by clicking on its edge on the PFD. Choose File/Export from the menu bar. PRO/II displays the Export

window (Figure 3-10). Choose the Selected Page of Flowsheet Drawing option. Click OK.

Exporting Stream Property Table Data You can export the information in a stream property table to an ASCII file for importing into spreadsheet and word processing applications. To export data from a stream property table:

Select the stream property table to export on the PFD. Choose File/Export from the menu bar. PRO/II displays the Export

window (Figure 3-10).

using data from an Excel spreadsheet. Note: You must have Microsoft Excel installed on your system to Use these tools. P /II comes preinstalled with some default spreadsheet tools. They can b

create tables of streamillation report.

orting the Flowsheet Drawing to the Clipbo

You can expth To

To


Choose the Stream Pro Click OK. The Export F Enter a name for the Output File. Select the desired file format (tab-delimited or com

Save File as Type drop-down list box. Click OK.

perty Table option. ile Filter window will be displayed (see Figure 3-11).

ma-delimited) from the

Figure 3-11: Export File Filter Window

PRO/II then generates the ASCII file. To import this file into your spreadsheet orword processing program, follow the instructions included with that application.

opying Stream Property Table Data to the Clipboard Youtable ca r Windows application.

o copy a stream property table to the Clipboard:

Select the stream property table on the PFD. Choose Edit/Copy from the menu bar.

C

can copy the information in a stream property table to the clipboard. This n then be pasted into any othe

T


Copy/Paste Stream Data in an Excel Sheet Use this option to copy and paste the stream data to and from an Excel sheet. This will enable the user to enter and analyze the data with much ease.The feature has been implemented to all dialog boxes, where the data is represented in XY grid. XY grid has the following properties:

• The grid origin is numbered 0.0. • The X and Y axis divide the grid into 4 quadrants. • Display any grid variable as a distinct value per cell or smoothly varying. • No duplicate values are allowed.

Note: Ctrl+C, Ctrl+V, Ctrl+X can be used a shortcut to COPY, PASTE and CUT respectively.

ou wing as an AutoCAD .DXF or Encapsulated Pos

isplays the Export

pt

Exporting the PFD to an AutoCAD or PostScript File Y can export your flowsheet dra

tScript (.EPS) file:

Choose File/Export from the menu bar. PRO/II dwindow (Figure 3-10).

Choose the Flowsheet to AutoCAD .DXF or Flowsheet to Post-Scrioption.

Click OK. The Save As window appears. Enter a name for the .DXF or .EPS file.


Chapter 4 BThis chapter describes how to construct a flowsheet. It begins by describing the various defaults that may apply to your simulation on a global, simulation, or unit level. This chapter also includes instructions for placing unit operations, connecting units, and drawing objects that enhance the presentation of your flowsheet without affecting calculations. Setting Simulation Preferences PRO/II enables you to set global defaults for problem descriptions information,

ms. These global defaults apply to all de them either for a particular simulation

r unit operation. On a simmeasur lation level settings override global defaults. In addition, youoverride

etting Problem Description Global Defaults

ults printout as a heading and e Problem Description itself appears on the first page. All simulations use the

o set problem description global defaults:

Choose Options/Simulation Defaults from the menu bar. e

uilding a Flowsheet

units of measure and thermodynamic systesimulations unless you specifically overrio

ulation level, you can set problem-specific input and output units of e defaults. Simu

can change units of measure settings for a specific unit. This setting s both simulation and global defaults.

S The Problem Description Information (Project Identifier, Problem Identifier, User Name, Date, Site) appears on each page of a resthglobal problem descriptive information unless you override the defaults for a particular simulation. T

Choose Problem Description. The Global Default for Problem DescriptivInformation window appears.

Chapter 4 BUILDING A FLOWSHEET 47

Figure 4-1: Global Default for Problem Descriptive Information

Complete the window. Click OK.

Overriding the Global Default Problem Description Before laying down your flowsheet, you may want to update the problem description for the current simulation. PRO/II uses the global defaults for all

imulation.

o

simulations, unless you specifically override the data for a particular s T override the global default problem definition:

Click Problem Description or choose Input/Problem Description fromthe menu bar. The Problem Descriptive Information window appears.

enter up to ten problem description lines (80 characters each), that will on the first page of a results printout.

You can

ppear

Setting Units of Meas ults By default, PRO/II uses the English units of measure set for all input data and for output r These defaults apply to tions. You can override the default set for either input data or output reports (or both) for all new simulations. PRO/II maintains a library of units of me that yo and dd to.

a

ure Global Defa

eports. all new simula

asure sets u can select froma


To set the unit of measure global defaults:

Choose Simulation Defaults from the Options menu.

Choose Units of Measure. The Default Sets of Units of Measure window appears.

Figure 4-2: e Sets

esired default units of measure set for entering simulation ce is ENGLISH-SET1, i.e., the data input will be in

Select the desired default units of measure set for generating the first t

any ch rt will no ng sure

et for the second output report will be disabled.

RO/II sets English units as the default for units of measure. You can override thisaddition its of measure for a particular simulation

roblem.

Global Units of Measur

Select the d

data. The default choiEnglish units.

output report. The default choice is Same as Input, i.e., the first outpureport will be printed in the default English units.

If oice other than the default is selected, the second output repo

er be available, and the list-box for selecting the alternate units of mealos Select the desired default units of measure set for generating the second output report. The default choice is None, i.e., no second output report in alternate units will be generated. Setting Units of Measure Simulation Defaults P

default, setting the global units of measure for all new simulations. In , you can override the default un

p


To

Click Input Units of Measure

set the units of measure for the current simulation:

or choose Input/Units of Measure from the menu bar. The Default Units of Measure for Problem Data Input window appears.

Figure 4-3: Default Units of Measure for Problem Data Input Window

Select different dimensional units for data input for each individual

category or choose Initialize from UOM Library... to automatically fill in the defaults from another set.

Click Standard Vapor Conditions... to enter the Problem Standard Vapor Condition window. The default temperature and pressure basis are shown in the data entry fields and may be replaced or the standard vapor

II default values are: volume per mole may be replaced, not both. PRO/

Temperature Pressure Vapor Volume

English 60°F 14.696 psia 379.48 ft 3 /lbmol

Metric 0°C 1.0332 kg/cm2 22.414 m3 /kgmol

SI 273.15 K 101.32 kpa 22.414 m3 /kgmol


The asis) is shown in a data entr . The PRO/II defa

current atmospheric pressure (Pressure Gauge By field and may be replaced with another value as desiredult value is 14.696 psia or the metric equivalent.

Click TVP and RVP Conditions... to select the Problem TVP and RVP

list box on this window. Choices are:

y,

ntains the names of the dimensional unit sets currently ts: English

Conditions window. The temperature for true vapor pressure specifications may be replaced in this window. The PRO/II default for TVP calculations is 10 °F. The calculation method for Reid vapor pressure may be selected in a drop-down

API Naphtha (the default) API Crude ASTM D323-73 ASTM D323-82 ASTM D4593-91 ASTM D5191-91 ASTM D323-94

Click OK .

Units of Measure Library A library of dimensional unit sets which may be used for data entry or report writing is maintained with this feature. To add a new set to the library or to edit anexisting set:

Select Options/Units of Measure List from the menu bar. The Units of Measure Library window appears and may be used to create, copedit, rename, and delete dimensional unit sets. The Units of Measure Set Name

nd Description list box coain the library. The program provides three initial dimensional unit se(the default), Metric, and SI. To create a new set:

Click Create... on the Units of Measure Library window to get the Create Units of Measure Set window.


Figure 4-4: Units of Measure Library

Supply a name for the new set in the data entry field provided, and select

the basis for the set with the appropriate radio button: English, Metric, or SI.

Figure 4-5: Create Units of Measure Set Window

Click OK to continue. The units for the standard dimensional unit sets in PRO/II are assigned to the new set and the edit feature may be used to customize the set. Note: An alternate way to create a new set is to highlight an existing set in the Units of Measure Set Name and Description list box and click Copy on the Units


of Measure Library window. The name for the new set is then entered in the opy Units of Measure Set window. The Edit feature may be used to customize

To

of Measure Set Name and Description list box. Click the Delete, Rename, or Edit button on the Units of Measure Library

window.

A d t reports may be edited in two places in PRO/II:

Cthe set.

delete, rename or edit a set:

Select the set in the Units

Editing the Dimensional Unit Sets for Output Reports

imensional unit set for outpu

1. Library sets are edited with the Edit... feature in the Units of Measure Library

. The set being used for the current problem is edited in the Default Units of rt which is accessible from the PFD main

indow by:

he dimensional unit set for the output report is initialized from the global set, as reviously explained. However, a different set may be chosen from the units of easure library while in the Default Units of Measure for Problem Output Report

window. 2Measure of the Problem Output Repow

Selecting the Output menu on the menu bar. Selecting the Report Format from the Output menu. Selecting Units of Measure from the Report Format menu.Editing of the

dimensional items is identical for these two windows.

Tpmwindow. To use a different dimensional unit set:

Click nitialize from UOM Library... The Initialize Units of Measure fUOM Library window appears.

rom

Select the desired set from the drop-down list box. Click OK to continue. This set now becomes the output report set. The

newly selected output report set may be edited in this window as desired. The edited set is saved with the problem.

The Print Option for output reports may also be selected using the Output Report(s) to be Printed drop-down list box where options are: One Output Report in Input Units (the default): When this option is selected, an output report based on the units of measure used for the problem data input will be generated. The currently specified input units of measure will be displayed for informational purposes, but they cannot be changed. With this option, the


output units of measure can only be changed by selecting the Units of Measure option from the Input menu. One Output Report in Output Units: When this option is selected, an output report based on the output units of measure specified will be generated. The currently specified output units of measure will be displayed, and they can be changed if desired. Two Output Reports, one in Input Units, one in Output Units: When this option is selected, two output reports will be generated, one each, based on the input and specified output units of measure will be generated. The currently specified output units of measure will be displayed, and they can be changed if desired. For the second and third cases discussed above, the displayed output units of measure set can be copied from the specified input units, or initialized from one of the units of measure sets stored in the units of measure library.

ed for the output report, o to the previously specified

put units:

on the Default Units of Measure for Problem

e set from a units of measure set

To copy the input units of measure set to be usto reset the explicitly specified output units

r

in

Click Copy from Input UOMOutput Report window.

Click OK to continue. To initialize the output units of measurtored in the units of measure library: s

Click Initialize from UOM Library... on the Default Units of Measure for

Problem Output Report window. Click OK to continue.

the results of a previously executed simulation must be printed in a different set gh this

Ifof dimensional units, it is only necessary to select the required units throufeature and generate a new report. The entire simulation need not be executedfrom the start just to obtain the output results in a different set of dimensionalunits.


Setting Thermodynamic System Global Defaults

stem global defaults:

dynamic

o set the thermodynamic syT

Choose Simulation Defaults from the Options menu. Choose Thermodynamic System. The Global Default Thermo

System window appears.

Figu

Note: This global default will not become effective until the next time File/New is

etting General Drawing Defaults

RO/II allows you to change the appearance of your workplace through the ,

te for s and you may never need to make changes in this window.

re 4-6: Global Default Thermodynamic System Window

Complete the window. Click OK .

selected. S PGeneral Drawing Defaults window. You can set the snap and move toleranceszoom and pan increments, the PFD palette icon, icon fill, unit snapping, and delete confirmation. The defaults, shown below in Figure 4-7, are appropriamost scenario


To make changes to the general drawing defaults:

Choose Options/Drawing Defaults/General... from the menu bar.

Figure 4-7: General Drawing Defaults Window

hanging Delete Confir By oto chan

onfirmation off:

eet Tolerances

ptable margins of error and criteria for atisfyin

toleefault s are satisfactory for most problems.

C mation

default, PRO/II pr mpts you to confirm each delete operation. You may want ge this default setting.

To turn delete c

Within the General Drawing Defaults window, uncheck Confirm Deletesto turn the option off.

etting Global FlowshS

Use this option to identify the acces g certain numerical methods. Some flowsheet tolerances, such as the

rance for flash calculations, are internal and are not user-definable. The flowsheet toleranced


To set the tolerance for this flowsheet:

Choose Input/Flowsheet Tolerances on the menu bar.

Figure 4-8: Default Unit Specification Tolerances

lacing a Unit on the Flowsheet The PRO/II main window is your drawing board. PRO/II supplies a floating PFD alette and drawing objects that help you draw your problem quickly.

ws icons for each unit operation that you can select to place

P

p

he PFD palette shoTon the flowsheet. The PFD palette appears automatically when you open a new or existing file, or when you import a keyword file. To close or open the PFD palette:

Click Palette on/off , or select the View menuwindow. Check the Palettes/PFD option on or of

on the main PRO/II f.


Selecting a Unit from the PFD Palette To select a unit icon and place it on your flowsheet:

Choose the icon from the PFD palette (see Chapter 9 for unit descriptions).

Position the cursor where you want the unit icon to appear and click the left mouse button.

Figure 4-9: Placing a Unit

Sna

hen connecting two units with a stream PRO/II will adjust or “snap” the unit e connecting stream. By default, units you add to or

ove in the PFD main window snap to an invisible grid. You can turn grid

To

Choose Drawing Defaults from the Options menu. Select General. Select Unit Snapping. The

pping

Wicon positions to straighten thmsnapping off.

turn grid snapping off:

disappears from the Unit Snapping check box.


Placing Multiple Unit Icons

ou can place a series of unit icons in succession. To pla

, click on the PFD main window to place the icon.

While still holding down <Shift> click on the PFD main window to place

t

the flowsheet:

Y

ce more than one unit at a time:

Select the desired unit from the floating PFD palette. Press <Shift>, and while holding down <Shift>

the second icon. Repeat for each additional placement of this icon.

Canceling Unit Placemen To cancel unit placement:

Click the right mouse button. Deleting a Unit To delete a unit already on

Click on the unit icon you want to delete.

Click delete on the toolbmouse button and select Delete.

ar, or press <Delete>, or click the right

cific unit:

elabeling a Unit R

PRO/II automatically labels each unit icon you place on the PFD main window. You can change the label for a unit by modifying the label on its data entry window. By default, the label consists of a character and a one-digit auto incrementing number. To relabel a spe

Double-click on the unit you want to rename. The data entry window for that unit appears.


Figure 4-10: Unit Data Entry Window

y out the connections between units and feed and roduct st matically appear when you

dep are red, while optional ro ons, an entire side of the unit will

e the Streams mode or display ports:

Type over the default name for Unit. Click OK.

rawing Streams D

Streams mode is used to lap reams. The product ports for each unit auto

ress the Streams button. Required product ports pb

duct ports are green. For some unit operatie red or green denoting multiple connections to that port.

o usT

Select Streams on the PFD palette.


Figure 4-11: Streams Button Down

The cursor changes to an arrow witisplays the product ports for each unit i

h a small S to indicate Streams mode. PRO/II n the layout. To display feed ports,

o draw a feed stream:

Click on an unoccupied area of the PFD main window.

wing Pr

To draw a product stream:

Click the left mouse button on a product port. Click the left mouse button again where you want the stream to end.

ddepress the left mouse button while the Streams button is depressed. Drawing Feed Streams T

Click the mouse on the feed port you want the incoming stream connected to.

Dra oduct Streams


Drawing a Connection To connect units:

Click the left mouse button on a port to anchor or start a stream. The ports and port colors for some unit operations change depending on the port you selected.

Click the mouse again at the other unit you want to connect. PRO/II draws an orthogonal line to connect the ports.

Figure 4-12: Feed, Product, and Connection Streams Layout

Can nection To cancel a stream connection:

Click the right mouse button or press <Esc>.

hanging a Connection

celing a Con

C


To change a connection:

Click the end (port) of the stream and hold down the mouse button. Drag the end of the stream to a new port. Release the mouse button.

ms When One Unit is Not Visible

In o ding unit for the stream segment must be visible in the PFD main window. You may open another viewport window of the same simulation and move to the end port you wish to view. Alternately, you can also use the scroll bars, the Pan View window, Search for Unit, or Search for Stream tool to display the end port. Labeling a Stream PRO/II automatically labels each stream you place on the PFD main window. By default, the label consists of an S followed by an auto incrementing number. You can change the label for a stream by changing the label on its data entry window. To relabel a stream:

m you want to relabel. The Stream Data window appears.

his ; other streams retain the original

enever you

o

Dra

ace.

Connecting Strea

rder to complete a stream connection, the en

Double-click on the strea

Type over the default name for Stream. Choose OK.

Tla

stream will now show the new labelbeling scheme.

Moving Streams

ou can change the route of the stream between two connections whYwish. T move a stream:

Click on the end of the stream you want to move.

g the stream to the new location.

Release the mouse button to drop the stream in pl


Rer As y oute calcmay nobstructed, orthogonal path for elected streams.

o reroute a stream:

e stream(s) you want to reroute. Choose Reroute from the Edit menu.

RO/II calculates the best route for these streams and automatically reroutes them Sea

streams you have placed on the by name. The Stream List identifies

ach stream by name. Goi To

outing Streams

ou add new connections, PRO/II automatically performs a stream rulation. When you move a stream or a unit operation icon, this calculation no longer be valid. You can recalculate an u

s T

Select th

P

.

rching for a Unit or Stream PRO/II builds two lists that identify the units and flowsheet. The Unit List identifies each unite

ng to a Unit

search for a unit:

Click Go to Unit or select View/Unit List. The Search for Unit dialog box appears, showing the names of all units currently placed on the

the

To

to Stream

flowsheet diagram. Select the unit you want to go to. The unit appears at the center of

PRO/II main window. Going to a Stream

search for a stream:

Click Go or select View/Stream List. The Search for Stream dialog box appears, showing the names of all streams currently

the flow diagram. stream you want to go to. The stream appears at the center of

placed on Select the

the PFD. Note: These search tools are only available on the toolbar if the Standard

oolbar is active. T


Changing the Flowsheet Layout

PRO that change the look of your pro template uses a different algorithm for calculating

e ot have to execute a simulation in order to change its layout.

ayout of your diagram:

Choose Lay Out Flowsheet from the View menu. A cascading menu the right of the View menu.

Choose one of the following layouts:

/II provides a variety of layout templates

cess flow diagram. Eachthre

position of unit operations and stream connections. You do n

To change the l

appears to

Single Line Multi-line Type 1 Multi-line Type 2

Figure

Single l

4-13: Sample PFD

ine format lays units in a single line from left to right.


Figure 4-14: Single Line

Drawing Freehand Objects PRO/II provides six objects that you can place on the flow diagram, to customize the look and increase understanding of the flow diagram without interfering with simulation data. These objects are:

Text Line Polygon Rectangle Ellipse Page

Entering Text You use the text option to include notes on your drawing. Once you choose text mode, you remain in text mode as long as you continue to choose the OK or Cancel button on the Draw Text window; choosing Cancel exits text mode.


To place text:

Choose Draw/Text from the menu bar.

Figure 4-15: Draw Text Window

Optionally, choose a font size for the text. The default is 50 pixels.

Dra Youwith sim O/II provides an orthogonal polyline feature.

o draw a line:

Choose Line from the Draw menu. Click and hold the mouse button on the PFD main window to anchor the

line. Press <Space> to set each anchor point for drawing in a new direction. Release the mouse button to complete your line.

To draw orthogonal connected lines:

Choose Line from the Draw menu. Click and hold the mouse button on the PFD main window to anchor the

line. Press <Ctrl>, and while holding down <Ctrl>, drag the cursor. Press <Space> to set each anchor point for drawing in a new direction. Release the mouse button to complete.

Enter the text you want to appear on the diagram.

Choose OK .

wing Lines

use the line option to add connected lines to the diagram without interfering ulation data. PR

T


Drawing Shapes You can draw shapes to enclose figures on a diagram without interfering with simulation data. To draw a polygon:

Choose Polygon from the Draw menu. Click and hold down the mouse button on the PFD main window. Press <Space> to each anchor point for drawing in a new direction. Release the mouse button to complete your object.

To draw an orthogonal polygon:

Choose Polygon from the Draw menu. Click and hold the mouse button on the PFD main window. Press <Ctrl>, and while holding down <Ctrl>, drag the cursor. Press <Space> to each anchor point for drawing in a new direction. Release the mouse button to complete your orthogonal polygon.

Choose Rectangle or Ellipse from the Draw menu.

square or circle:

Choose Rectangle or Ellipse from the Draw menu. Click and hold down the mouse button on the PFD main window.

d release the mouse button to complete your

r ges can be individually printed or copied to the clipboard (see

hapter 3, Managing PFD Files).

To

the PFD.

To draw a rectangle or ellipse:

Click and hold down the mouse button on the PFD main window. Drag and release when you see the desired size rectangle.

To draw a

Press <Ctrl> then drag ansquare.

Drawing Pages You can divide your PFD into “pages” and define separate page setup options foeach page. PaC

add a page:

Choose Page from the Draw menu. Click on


Drag and release the mouse button to the desired size. The page name is automatically given as PG followed by an auto incrementing

ree-digit number. th

Figure 4-16: Pages

To change the page setup options:

Page

Select your page setup options.

Afte cell in a grid

o resize the page:

Click near the page outline to highlight the page. Click and drag the sizing box.

Double-click anywhere along the page border. This brings up the

Setup window.

Click OK to continue.

r you have set up a page, you can resize it or make this page one of pages.

T


To move the page:

Click and drag the page outline to a new location. To make a grid of pages:

Select the page by clicking near the page outline. Double-click the left mouse button to display the Page Setup window. Click on the radio button labeled Grid in the Change Page Parameters

group box. In the Page/Grid group box, select the radio button for Multiple Pages. Change the number of rows and columns to make a grid of pages on the

PFD. The page you started with will be the upper left cell of the grid. The grid can be resized and moved on the PFD in the same manner as a single page.


Chapter 5 Objects

This cts on the ove, resize, rotate, or flip them. In addition,

is chapter describes how to edit and align text.

gle object, multiple (noncontiguous) objects, or a group of bjects. Objects or groups of objects include units, streams and drawn objects.

rformed on selected objects.

Sel

To

ct.

de as

Manipulating

chapter describes how to select unit icons, streams, and other objePFD main window and how to m

th Selecting Objects or Groups of Objects You can select a sinoAll manipulations (delete, rotate, move) are pe

ecting Multiple Objects You can select a set of noncontiguous objects.

sel f individual objects: ect a set o

Click on the first obje Press <Shift>. While holding down <Shift>, click on each object you want to inclu

part of this set.

Chapter 5 MANIPULATING OBJECTS 71

-1: Multiple Unit SFigu

r the set of objects. For example, although five objects appear art of this set (Figure 5-1), when you move the selection, the

re 5 election Handles

Handles appear fo

be selected as ptofourth and fifth objects (the valve and the compressor) do not move with the set (Figure 5-2).


Figure 5-2: Move Multiple Objects

lecting a Group of Objects

u can gather a group of contiguous objects by dragging a selection rectangle und them.

select a contiguous group of objects:

Click on an unoccupied area of the PFD adjacent to one of the items you want to select and begin dragging the cursor by moving your mouse.

Drag the cursor until all desired objects are inside the selection rectangle outline.

Release the mouse button to end the selection. Handles appear for the selected group of objects.

Selecting all Objects You can select all objects on the flowsheet with one command. Once selected, you can then move or delete the entire selection.

Se Yoaro To


To select all objects on the flowsheet:

Choose Select All from the Edit menu. Deselecting Objects If you change your mind after selecting objects, you can reverse any selection. To deselect or unselect all objects in the layout, do one of the following:

Choose Select None from the Edit menu. Click on another item or on an unoccupied area of the PFD.

Resizing an Object You can change the height, width, or overall size of any object or a group of objects on your flowsheet. Changing the Size of a Selected Object When changing the width of a group of objects, you change the absolute distance between the objects and maintain the relative distance. To change the size of an object:

Click and drag the cursor until the object is the desired size. Release the mouse button.


Figure 5-3: Resize Column

ote: Condensers andN

s reboilers shown on distillation or side columns are fixed in

ge the size of the column.

estoring Unit Icon Size

r icons and objects n your flowsheet) you can quickly return the icon to its default size.

o restore an icon to its original size:

it menu. You can also click the right mouse button on a selected icon, and then choose Restore Icon

Rea O s of Objects You rotate or flip a unit ic

ize. They do not resize when you chan R If you don’t like how your resized icon looks (relative to otheo T

Choose Restore Icon Size from the Ed

Size from the Icon pop-up menu.

rranging bjects or Group

can move objects to a different area of the flowsheet. You can alsoon so it fits into the flow of your diagram.


Moving Selected Objects

position on the flowsheet.

position. Release the mouse button.

Set Movdefa

, then General.

he desired value over the default Move Tolerance. Choose OK.

Rot

ou can rotate a selected object(s) on its axis by 90, 180 or 270 degrees.

Choose 90, 180, or 270.

otating an Icon

e button on a unit icon, then choose Rotate from e Pop-up Unit menu to display the rotation degrees.

lipping Selected Objects

e am.

You can move an object to a new To move a selected object:

Click and drag the object or group of objects to a new

ting Move Tolerance

e Tolerance controls the incremental distance for any object you move. The ult is 5 pixels.

To change move tolerance:

Choose Drawing Defaults from the Options menu The General Drawing Defaults window appears.

Type t

ating Selected Objects Y To rotate a selected object:

Choose Rotate from the Edit menu. The Rotate degrees cascade menu appears to the right of the Edit menu.

R You can also click the right mousth F You can flip a selected object(s) horizontally or vertically to better orient thobject(s) relative to other objects of the diagr


To

(s).

Flipping an Icon

so click the right mouse button on a unit icon, then choose Flip from e Pop-up Unit menu to display the flip options.

diting Text

ou can change the text, size and or rotation of any text object you placed on the

To

ant to change. The Draw Text

red and choose OK.

ght or center of the box

Select the text you want to align (you must select at least two) by clicking

ign Text from the Edit menu. The align menu pop-up appears to the right of the Edit menu.

flip a selected object:

Select an object Choose Flip from the Edit menu. The Flip options menu appears to the

right of the Edit menu. Choose Horizontal or Vertical.

You can alth E YPFD main window.

edit text:

Double-click on the texwindow appears.

t object you w

Edit as desi Aligning Text

ou can align text in two or more text boxes to the left, riYthey are drawn in. To align text:

on the first text box, then click on the other box(es) while holding down the <Shift> key.

Choose Al

Choose Left, Center or Right.


Chheet Contents

ls that aid you in viewing your flowsheet contents:

hange the visible portion dow.

l feature of PRO/II that enables you to nd use a bounding box in the

a.

crolling the PFD

u can scroll the PFD left, right, up, or down using the horizontal and vertical roll Bars. Both bars enable you to scroll in small or large increments or to scroll a general location.

You can change the actual value for the scroll increments by altering the Pan Increment value on the General Drawing Defaults window. Zooming You can access the PRO/II zoom features from the View menu, using the zoom buttons on the toolbar, or using the keyboard. To zoom in or out, do one of the following:

Click

apter 6 Viewing Flows PRO/II offers a variety of too

Horizontal and vertical scroll bars allow you to cof the process flow diagram in the PFD main win

You may open additional viewport windows of your current flowsheet to display different views of your simulation. The Pan View window is a specia

see a thumbnail of the entire flowsheet athumbnail to move the visible are

This chapter describes how to use the PRO/II scroll, pan, and multiple viewport features to display portions of your flowsheet diagram in the PFD. S YoSco t Setting Scrolling Increments

on the toolbar. Choose Zoom In or Zoom Out from the View menu. Choose <PgUp>or <PgDn> to Zoom in or Zoom out the PFD.

Chapter 6 VIEWING FLOWSHEET CONTENTS 79

Zooming in on a Selected Area You can specify the exact area of the flowsheet that you want to zoom in on. To zoom in on a specific area of the flowsheet:

Click on the toolbar or choose Zoom Area from the View menu. Click and drag the mouse to encompass the desired area within the

selection rectangle outline. Release to complete the zoom area operation. The selected area fills the

PFD. Zooming to Show the Full Flowsheet You can quickly display the entire flowsheet in the PFD. To use zoom to show the full flowsheet, do one of the following:

Click on the toolbar. Choose Zoom Full from the View menu. Press <Home>.

Setting the Zoom Increment You can change the increment PRO/II uses to zoom in or zoom out within the General Drawing Defaults window. The default small zoom increment is 5 pixels and the default large zoom increment is 20 pixels. Opening Multiple Viewport Windows You can open multiple viewports of a single simulation problem to display different views of the flowsheet. To open an additional viewport of the current simulation problem, do one of the following:


Click Multiple Viewpo on the toolbar or choose New View on the

d on your toolbar, ar menu.

rtsWindow menu.

Note: If the multiple viewports button is not displayeheck the Standard menu option from the View/Toolbc

Figure 6-1: Multiple Viewports

edraw the Simulation

You can u raw to clear extran d dots from the PF To redraw the diagram, do one of the fo

Click

R

se red eous lines an D.

llowing:

on the toolba Choose Redraw u. Press <Shift+Home>.

Panning

r. on the View men


You can pan the content ind ow or the Small Pan or Large Pan options on the View m The Pan View window is a thumbprint of the entire nding box identifies the area of the flowsheet currently visible w. You move the bounding box o an portion of the flowsheet you see in From the View menu, yo sma n, left, or right. You can change the settings for the pan incr awing Defaults window. Displaying and Hiding t To display the Pan View window:

Click

s of the PRO/II main w ow using the Pan windenu.

flowsheet. A bouin the PFD main windo

r change its size to chthe PFD.

ge how much or what

u can pan in large or ll increments: up, dowement in the General Dr

he Pan View Window

on the toolbar or choose Pan Vi dow menu.

ew from the Win

Figure 6-2: Pan View Window

Panning - Using the Pan View Window


Use the bounding box to change the visible portion of the flowsheet in the PFD indow by moving, enlarging or reducing the bounding box in the Pan View

g box.

To move the bounding box:

Drag to a new location. The area enclosed fills the PFD.

Note: For a large flowsheet, use the Pan View window to quickly switch from one

ha To ch

Click and drag the bounding box border handle to enlarge or reduce the bounding box. The area enclosed fills the PFD.

Panning - Using the Menu Options You can pan the image in the PFD up, down, left, or right using the panning options on the Zoom menu. To pan the image a large or small amount:

Choose Large Pan or Small Pan from the View menu. The pop-up menu appears.

Choose Left, Right,Up, or Down. Setting Panning Sensitivity You can change the increment PRO/II uses to pan. The default small pan increment is 5 pixels and the default large pan increment is 20 pixels.


wwindow. The flowsheet in the PFD view changes to match the area encompassed by the boundin Moving the Bounding Box

Click the mouse inside the box.

area of the flowsheet to another. C nging the Size of the Bounding Box

ange the size of the bounding box:


C eata Entry Windows

for entering the data ssociated with your PRO/II simulation. There are a number of libraries from

these

e current simulation. PRO/II identifies which nits are missing data by putting a red border around the unit icon (on the

ation string for

Def op

Defining the simulation problem Selecting the components for the simulation Setting the thermodynamic methods for the simulation

e: Chapter 8, Specifying Component, Thermodynamic and Stream Data and hapter 9, Unit Operations and Utility Modules provide explicit details on the use

duced in this chapter.

hapt r 7 D PRO/II offers a wide variety of data entry windowsawhich you can extract sets of data. This chapter provides an introduction todata entry windows. Defining the Simulation You can use the data entry window buttons on the toolbar or the options on the Input menu to define the scope of thutoolbar). For units that are missing product streams, the identific

at unit appears in red (on the PRO/II main window). th

ining the sc e of the simulation involves:

NotCof the data entry windows intro A summary of the Data Entry Window buttons available on the PRO/II toolbar is provided below.


Problem Description Enables you to describe the current simulation

project.

and relate it to a specific

Units of Measure Enables you to set units of measure specific to this simulation. Each new simulation extracts defaults from the default

nit of Measure Set.

U

Chapter 7 DATA ENTRY WINDOWS 85

Component Selection Enables you to specify

the components and pseudocomponents you want to uscurrent sim

e in the ulation

Component Properties Enables you to supply

component properties.

Thermodynamic Data Enables you to select

thermodynamic methods for the current simulation.

Assay Characterization Enables you to modify

TBP Cutpoints and characterization options for the generation of pseudocomponents from Assay streams.

Procedure Data Enables you to supply or te

calculations without the

FORTRAN code fkinetic reaction ra

need for compilation and linking.

Case Study Specification Allows you to perform

studies on a base case solution by altering parameters selectively and rerunning.

Reaction Data Enables you to define reactions and provide heat of reaction,

equilibrium, or kinetic data for reaction sets.

Calculation Sequence Enables you to specify a user-defined calculation

sequence.

Recycle Convergence Enables you to specify user-defined recycle convergence and

ns.

acceleration optio


Selecting Components

se this to select the components and pseudocomponents that you want include in this simulation.

To select components for use in this simulation:

Click

U option to

on the toolbar or choose Component Selection on the Input dow appears. menu. The Component Selection win

Figure 7-1: Component Selection

Select a component from the e

component. Each component s in the List of Selected Components box on the right side of the wind

available lists or type the name of th you select appear

ow.


Modifying Component Properties

ou can se this option to modify fixed component properties or use the Fill from tructures feature to fill in missing component data for library or user-defined

Y uScomponents. To modify component properties:

Click on the toolbar or choose Component Properties from the Input menu. The Component Property Modification window appears.

Figure 7-2: Component Property Modification

Selecting Thermodynamic Methods You use the thermodynamic data option to choose the thermodynamic methofor this simulation.

d(s)

o set thermodynamic calculation methods for this simulation:

Click

T

on the toolbar or choose Thermodynamic Data on the Input menu.


Figure 7-3: Thermodynamic Data

tion methods.

Select a category of predefined systems. PRO/II displays the predefined

You can specify a predefined system of thermodynamic calcula

systems for this category in the Primary Method list box. Select a predefined system from the Primary Method list box. Choose Add-> to define the calculation method.

Selecting Assay Data You use this option to modify the data obtained from the selected Assay Set. To select assay data for this simulation:

Click on the toolbar or choose Assay Characterization on the menu.

Input


Figure 7-4: Assay Cutpoints and Characterization

PRO/II always supplies the Primary TBP Cutpoint set. You can modify the rimary set or define a new cutpoint set or set characterization options.

Specifying Reaction Data You use this option to define reactions and enter heat of reaction, equilibrium, or kinetic data for reaction data sets. To specify reaction data sets for this simulation:

Click

p

on the toolbar or choose Reaction Data on the Input menu.


Figure 7-5: Reaction Data

ecifying Procedure Data

e this option to create procedure blocks to calculate kinetic reaction rates. You e able to supply FORTRAN code for the reaction rate calculations without the ed for compilation and linking.

o select procedure data for this simulation:

Click

Sp Usarne T

on the toolbar or choose Procedure Data on the Input menu.

Figure 7-6: Procedure Data


Specifying Multiple Simulations for Case Study Use this option to make changes to input data and then examine the effect of those changes on the values of calculated data or functions of calculated data. To select case study data for this simulation:

Click on the toolbar or choose Case Study Data on the Input menu. Check the Define Case Study box.

Figure 7-7: Case Study Specification

Setting the Problem Calculation Sequence PRO/II performs a simulation by solving one unit operation at a time, following a certain calculation sequence to reach the problem solution. Use this option to specify the method to determine this calculation sequence for the current problem. To select calculation sequence for this simulation:


Click on the toolbamenu.

r or choose Calculation Sequence from the Input

igure 7-8: Problem Calculation Specification F

Specifying the Recycle Convergence You use this option to override the recycle loop sequence determined by PRO/and to specify acceleration methods and convergence tolerances for individual loops.

II,

select the SIMSCI method for loops are determined automatically by this

ethod.

this simulation:

Note: This window is not available if youCalculation Sequencing, since them

o select recycle convergence forT

Click on the toolbar or choose Recycle Convergence on the Input menu.


Figure 7-9: Recycle Convergence Options

Data Entry Windows for Unit Operations The data entry window for any unit operation can be accessed by highlighting the

try from the menu bar. Numerous are u pply numeric values and select

pin Buttons, Standard d, Combo Boxes, Drop-

s, Li ed Te

unit on the PFD and selecting the Input/Data Entypes of data entry devices sed to sucalculation options in PRO/II, including: Push Buttons, Radio Buttons, Check Boxes, Edit Fields, SList Boxes, Drop-Down List Boxes, Grid and X-Y GriDown Combo Boxe nk xt and Notes. Most main data entry windows provide Help, Overview, and Status buttons that enable you to access different levels of help text. In addition, some main data entry windows (and some subordinate windows) provide UOM, Define and Range buttons. Grayed buttons indicate that the feature is currently unavailable.

Button Description

Displays context-sensitive help for the active data entry field, or for the window itself (if there is no active field).


Displays the main help window for the data entry window.

consistency checks performed for the main window after you choose OK.

Displays the results of the data

Selects a units of measure set for the selected data entry field.

parameter value to another stream or unit parameter.

References one stream or unit

Displays the valid range of values for the active data entry field.

Displays the notes, associated with the unit.

rids and the X-Y Grid

f

ata for relational curves. The two-grid columns contain an independent variable

G Grids are used to supply data in tabular form. There may be several rows orelated data entries. X-Y Grids are a special type of grid that are used to supplyd(x) and one related dependent variable (y). The Column Tray Hydraulics window shown below is an example of a grid. Notice that it provides columns for the starting tray number, ending tray number, calculation type, and entry of tray data. Each row has a numbered click button which is used to select the row for toolbar actions. For this example, several

pes of data entry devices are used in the grid. ty The starting and ending tray numbers are integer edit fields, the calculation type is a drop-down list box, and the entry of tray data is a click button, which brings up the Column Tray Sizing window or Column Tray Rating window, depending on the calculation type that was selected.


-10: Column TFigure 7 ray Hydraulics Window

f e

ow, click the row number button and the Cut button.

Observe that four rows are provided in the initial grid corresponding to five sections in the column. This may be expanded by clicking a row number button and then clicking the Insert button. A row will be added below the selected row. When the number of rows exceeds five, a scroll bar appears at the right side othe grid to provide access to the rows not displayed. To deselect a row, click thnumber button of the previously selected row, or select a different row. To clear data entries from a row, click the row number button and then click Reset. To remove a r As another example, the Compressor Outlet Pressure Performance window shown below contains an X-Y grid for a user-supplied compressor pressure curve.


Figure 7-11: Compressor Outlet Pressure Performance Window

otice that two columns are used for the pN ressure curve. The first column is the

s in

esc grid exc d. A roclicking rowwhicinsert a Lin Linked ues, mathemsupplieddevice. hown in 12.

volumetric feed rate and the second column is the corresponding outlet pressure from the compressor. Four individual entries or cells corresponding to two rowthe table are marked with a red border as mandatory input. Optionally, more pairs of information may be provided. The initial grid displays four pairs of cells. Note that each row in the grid has a numbered click button which may be used to elect the row. s

he initial table may be expanded with the Insert button on the toolbar as T

d ribed in the previous example. When the number of rows in the X-Y eeds four, a scroll bar appears to provide access to rows not displaye

w may be deleted from the grid by clicking its number button and then Cut. To copy a row, first click its number button and then click Copy. The

is copied into the clipboard. Next, click the row number button for the row h will be just below the copied row. Complete the copy by clicking Paste to

copy of the row from the clipboard.

ked text

text is used to input information in a sentence format. Numeric valatical operators, stream or unit names, or various options may be as linked text. Linked text may serve to access another data entry The Feedback Controller data entry window containing linked text is Figure 7-s


Figu lay

Link fication and Variable. Note that you must click thes lt tolerance is gre

pti re-mentioned te

blue indicating a user-supplied value.

upply is now displayed in blue numbers instead of the value text trin

Clickingunit or s e

arame cing the

re 7-12: Feedback Controller Main Data Entry Window - Initial Disp

ed text is used on this window to define the Speci the Parameter and value link texts are red, denoting thate strings and provide data entries. The text string the defau

en, denoting a default value.

O onally, a different tolerance may be provided by clicking the afotext string to open the Specification Tolerance window, where the appropriaradio button may be clicked to select a new tolerance type, i.e., relative tolerance. Click OK to return to the Feedback Controller window. Notice that the elative tolerance text string becomesr

When the value text string is clicked, a floating point entry field for the specification value is displayed with a red border signifying mandatory input. The alue you sv

s g.

the Parameter text string retrieves the Parameter window in which the tream and its parameter are defined. The unit or stream identifier and thter for the specification are now displayed in blue, replap

Parameter text string.


Figu

re 7-13: Feedback Controller Data Entry Window - Final Display


Chapter 8 pecifying Component,

ic and

you

00 omponents and are adequate for nearly all simulation models. The AIChE

SThermodynamic and StreamData This chapter describes several types of optional component, thermodynamstream information which may be supplied for PRO/II. In many cases, the default values are satisfactory and it may not be necessary for you to visit these sections. Component Data General Information PRO/II provides considerable flexibility in the definition of component data. Nolimit is set on the number of components which may be used for any problem. Furthermore, component data may originate from a variety of sources such as SIMSCI databanks, user-prepared databanks, user-defined components, and components derived from petroleum assay data for feed streams. Moreover, may stipulate a preferential search order when multiple databanks are used. The SIMSCI databanks, SIMSCI and PROCESS, contain more than 17cDIPPR databank is also available as an add-on to PRO/II. User databanks of thermophysical data can be created, using SIMSCI LIBMGR and DATAPREP programs, and maintained through PRO/II graphical user interface. SIMSCI REGRESS is also fully supported in PRO/II, allowing you to carry out regression of experimental thermo-physical data to model equations. Selecting Library Components You may select library components, from both SIMSCI and user-supplied databanks, through the Component Selection main data entry window. To open this window from the PRO/II main window:

Click on the toolbar, or select the menu bar item Input/ComponSelection. The Component Selection window appears.

ent

Chapter 8 SPECIFYING COMPONENT, THERMODYNAMIC AND STREAM DATA 101

If you know the library access name for a component, you may enter it directly into the data entry field. Click Add-> or press <Enter> to retrieve the component

om the component databank and add it to the List of Selected Components. If frthe component cannot be located by the name you have entered, a warning will recommend that you use the Select from Lists… feature to locate the component in the SIMSCI and PROCESS databanks:

Click Select from Lists… on the Component Selection main data entry window to open the Component Selection -List/ Search window.

Select a Component Family from the like-named drop-down list box. A . A

ost Commonly Used: Approximately 100 components representing all of the monly encountered in natural gas and petroleum

ll Components: Every component in the SIMSCI and PROCESS databanks. Fam ie

cids Electrolyte Components

ed Derivativesus c Hydrocarbons

n D rivativ s rbons alts and Minerals Silicon Derivatives

may define

, alias, or chemical formula as the search tring. As components are located, transfer them to the Additions to Component

f

large number of component families are provided to speed the searchbrief description is given below:

Mpure components com

rocessing. p Hydrocarbon Lightends: Light gases commonly reported on analysis for oil refinery streams. A

il s of Specific Chemical Type: Twenty families in alphabetical order:

Additional AAlcohols Aldehydes Amides Amines

romatic Hydrocarbons Elements AEsters Ethers Halogenat Ketones Miscellaneo NaphtheniOther Nitroge e e Paraffinic HydrocaSSulfur Derivatives Unsaturated Hydrocarbons For all families listed above, except for Hydrocarbon Lightends, you specific search criteria by selecting radio buttons and entering a search string. Use part or all of the component namesList box. When you have located all the components, click OK to return to the Component Selection main window and to transfer the components to the List oSelected Components. The priority order for databanks may be defined by pushing the Databank Hierarchy button on the Component Selection main window to access the Component Selection – Databank Search Order window.


This window initially displays the default search order and may be modified tosearch the databanks in any order. Components are alwa

ys selected from the

rst databank in the search order in which they appear.

gnized

hen you

fi Note: The newly added libraries and databank names in TDM can be recoin this dialog box by Library Name:Databank Name. Entering User-defined Components You may want to enter a component as a user-defined component wwish to use a component that is not in the PRO/II library.

Enter user-defined components by clicking User-defined… on the window to access the Component Definition -

User Defined window.

me of the user-defined omponent in the database. Next, you must supply the properties for the

s.

efining Petroleum (PETRO) Components

Component Selection main

Type in the name of the user-defined component in the ComponentName entry field.

Click OK to commit the new component name. Note: At this point, you have only entered the naccomponent by the steps described below in Modifying Component Propertie D Define PETRO components by clicking Petroleum… on the Component Selection

it to

and molecular weight for each component. Names

ter, when missing.

d from the

not possible to enter data for assay pseudocomponents (which are h this window. All properties for

are automatically defined by PRO/II. The omponents are also added to the component list by PRO/II.

main window to access the Component Selection – Petroleum Components window. You may define any number of PETRO components in a single visthis window by using the tabular input provided. You must supply at least two of the three correlating properties, normal boilingpoint, standard liquid density, may be optionally provided or will be supplied by PRO/II as NBP XXX where XXX is the component normal boiling point. PRO/II uses internal correlations to estimate the third parame All necessary physical and thermodynamic properties are computethree correlating properties. Molecular weight is the most difficult property to predict accurately from generalized correlations and should be supplied when possible, for the most accurate characterization for a PETRO component. Note: It is based on stream assay information) witcomponents derived from assay datac


Defining Solid Components You can enter inputs for solid characteristics directly into PRO/II. You may pecify stream properties, the particle size distribution, and the particle

ws you to input experimental solids solubility data. sproperties. PRO/II also allo To add a solid component to the flowsheet:

Click or select Input/Component Selection from the menu bar to open the Component Selection window.

Click Component Phases…. Ensure that the components that may be solid have the solid phase enabled. For example, if you enter NaCl for use in a dissolver, make sure that its component phase designation is “liquid-solid”.

If the flowsheet will include unit operations that require particle size distributions (e.g., Cyclone, Dissolver, Crystallizer), Input/Component Property Data from the menu bar. In the like-named window, click Particle Size Distribution… to open the

evant

f bution Ranges entry fields to enable the UOM button in the toolbar at

ents.

he name of component in the List of Selected Components. Click Delete .

o rename a component for printout purposes:

Highlight the component.

Particle Size Distribution for Solids window. Enter PSD cutpoints for all relsolid components. Particle size grades are bounded by the cutpoints that are entered here. Grades will not be created on the open ends of the first and last cutpoints (i.e., if the cutpoints are 10 and 20 microns, there will be one grade of 10 to 20 microns, not three grades of less than 10, 10 to 20, and greater than 20 microns). To change the units of measure for the particle size distribution, click in any ohe Distritthe top of the window. Deleting and Renaming Component Properties Currently, actions on components that appear in the List of Selected Components in the Component Selection main window are limited to deletion or renaming of compon To delete a component:

Highlight t

T


Click Rename… to open the Rename a Component window. ta entry field.

fy properties for any component entered through the Component election main data entry window via the Component Property window. To reach

this

Enter the new name in the da Modifying Component Properties You can modiS

window:

Select Input/Component Properties... from the menu bar or click onthe main toolbar.

The Component Properties window is the master navigation point for changing all component properties.

Note: Component properties cannot be defined before the component names have been entered. There are three methods available for component property modification: Method 1: Specifying Fixed Properties Click Fixed… to open the Components Properties-Fixed Properties window.

ere, you can modify fixed component properties such as molecular weight, ay components, all

omponents can be modified via this window. For those properties having UOMs,

:

Hcritical temperature and NBP. With the exception of asscall data is displayed with the UOMs of the current problem. Starting from this window, use the appropriate button to modify other properties

Click Critical Properties… to specify critical temperature, critical pressure, critical volume and critical compressibility factor.

Click Molecular Constants… to specify properties such as DipoleMoment, Radius of Gyration, van der Waals Area parameter and van deWaals Volume parameter.

r

Click Heats of Formation… to specify Enthalpy of Formation and GibbsEnergy of Formation. In this entry, reference phase designation is a required input. The reference phase can be vapor, liquid or solid. Vphase is the default.

apor

Click Miscellaneous Properties to specify Acentric Factor, Solubility Parameter, Rackett Parameter, Liquid Molar Volume, Heat of Vaporization, Heat of Fusion, Normal Melting Point, TripleTemperature, Triple Point Pressure, Heat of Combustion, Gro

Point ss Heating

cy Value, Lower Heating Value, Carbon Number and Hydrogen DeficienNumber.


For PRO/II library components, the values in the database will appear in the

se properties.

m

ts from

supply data in the Component Properties –

y data

urce Selection window, choose the

ose the Correlation Coefficients option, you may display the form of the d drop-

Select one of the correlations and supply coefficients as required.If the

ility.

various property windows. In cases where there is no library value to serve as the default, the default displayed will be the text “Missing.” You may reassign values for any of the Method 2: Specifying Temperature-dependent Properties You may enter or override default data for properties that change with temperature, such as density and viscosity, for the vapor, liquid or solid phases of the pure components in your simulation. You may supply new data in the forof tables or as correlation coefficients of one of 29 different equation types.

lick Temperature Dependent to open the Component Properties –Temperature CDependent Properties window. All the library and user-defined componenthe current problem are displayed. To enter or modify data for a property of acomponent, click on the corresponding push button for that component. For properties that may apply to more than one phase, you will first be required to elect the phase for which you are tos

Phase window,

Click VP to enter or modify liquid or solid vapor pressure data Click H to enter or modify vapor, liquid or solid enthalp Click Cp to enter or modify solid heat capacity data Click ∆Ην to enter or modify latent heat data Click ρ to enter or modify liquid or solid density data Click µ to enter or modify vapor or liquid viscosity data Click κ to enter or modify vapor, liquid or solid conductivity data Click σ to enter or modify liquid surface tension data

the Component Properties - Data SoIn

method of data entry. You may enter data either in tabular form or as coefficientsfor one of as many as 29 equations. f you choIequation by selecting the appropriate Correlation Number in the like-namedown list.

form of the equation is logarithmic, you may select the base of the logarithm. You may change the units of the equation and may imposemaximum and minimum temperatures of applicab

Note: The full range of equations can be found in the online PRO/II Reference Manual accessible via the Help system. If you choose an equation that is not


standard, a message to that effect appears, and the border of the drop-down listbox will be yellow.

s industry.

BMGR – For managing user-defined pure component and binary

ta

n of PRO/II has been integrated with Thermodynamic Data tion will provide the following advantages to all

ity

tiple databanks. TDM encompasses DATAPREP and REGRESS functionality.

If you choose the Tabular Data option, the Component Properties –Tabular Data window appears.

Enter temperature and property data. You must enter at least one data pair.

PRO/II and TDM Integration Physical and Thermodynamic data of a chemical component has a profound

pact on the design and operation of a unit operation in a procesimPrevious versions of PRO/II use component information from DATAPREP and LIBMGR database. PRO/II in turn retrieves data from these libraries through library names and alias.

LIlibraries

DATAPREP – For reviewing and modifying pure component data REGRESS – For generating pure and binary interaction parameter da

from experimental information Reporting – For publishing and archiving component and binary data

urrent versioC

Manager (TDM). This integraRO/II users. P

PRO/II will pick up the data from both TDM-defined libraries and edlib.lb. PRO/II users can launch TDM GUI in different modes to define new

library/Databank. PRO/II users will now use DATAPREP and REGRESS functional

within TDM, which is already a part of TDM program. Apart from the above, working with TDM will provide the following advantages to PRO/II users.

TDM allows the user to build a customized library containing pure component data as well as unary and binary thermodynamic parameters.

TDM allows you to generate and display a variety of temperature-dependent graphical plots of tabulated data results.

Availability of mul


In the keyword input file, the newly added libraries and databank names in TDM an be recognized by Library Name:Databank Name.

ote: Use Thermo Data Manager user’s guide for detailed explanation on its

Κ

correlations and chniques. Joback (1985) significantly expanded the work of Lyderson (1955) in

oup contribution method for the prediction of critical roperties, boiling point, freezing point, ideal gas capacity, enthalpy and Gibbs

ally

c In Component Selection and Thermodynamic Data - Databank search order dialog box, the newly added and existing libraries and databank names in TDMcan be viewed. Users can select and add the libraries for the current simulation. Nfunctionalities. Method 3: Specifying Fill From Structure The Fill from Structure button opens the Components Properties – Fill fromStructure window. The Available Components list on the left side contains library and user-defined components from the current problem. You may add or remove components to be filled from structure to the like-named list on the right. Click Οto have the properties of the selected components filled from structure. PRO/II predicts properties from structure using establishedtethis area providing a grpheat of formation. Joback used a4 large database of components to statisticdetermine group parameters for 42 different functional groups. SIMSCI has extended this work to include several missing parameters. To complete the Fill from Structure procedure, click UNIFAC Structures… on the

omponent Properties window to display the like-named window. A UNIFAC CStructure entry is mandatory for all components for which Fill from Structure has been requested. Click UNIFAC Structures… adjacent to the component of

the UNIFAC group number directly. interest to open the Define UNIFAC Structure window where you may choose from families of components or from


Assay Data General Information

from another type of laboratory

m Hg basis, PRO/II has for other laboratory pressures.

amic properties may be estimated from

options n

For many petroleum-based streams, the composition is not fully known in terms of defined components. These stocks must be characterized by pseudocomponents for which the necessary physical and thermodynamic properties have been estimated. PRO/II has extensive procedures for the translation of petroleum stream laboratory assay data into pseudo components. Pseudocomponents are based on boiling point or “cutpoint” ranges on the true boiling point (TBP) distillation for the stock. The normal boiling point for a pseudocomponent is defined as the weighted average temperature of its cutpoint ange. The TBP distillation must often be derivedr

distillation, using a conversion procedure. PRO/II accepts the following types of laboratory distillations: TBP, ASTM D1160, ASTM D86, and ASTM D2887. While aboratory distillations are usually reported on a 760 mlprocedures to correct distillations Estimated values for the standard liquid gravity and molecular weight for each pseudocomponent are also needed for the characterization process. The standard liquid gravity for each pseudocomponent is derived from the gravity curve for the stream, in similar fashion to the normal boiling point. The gravity curve for the stream is often not available, and it must be estimated, based on the average stream gravity and the distillation curve. The molecular weight curve is seldom available, and the molecular weight for each pseudocomponent is usually predicted from its normal boiling point and standard liquid gravity. All

ther required physical and thermodynothe normal boiling point, standard liquid gravity, and molecular weight. The use of assay data in PRO/II is divided into two logical steps. The first step involves the definition of the cutpoint ranges and selection of the characterization options used in development of the pseudo components.Characterization include distillation curve fitting and conversion methods, gravity curve generatioprocedure, methods for prediction of molecular weight, and methods for stimation of critical properties and ideal gas enthalpies. If the default cutpoint e

ranges and methods furnished by PRO/II are acceptable, this step may be omitted. The properties for all pseudocomponents derived from the same cutpoint set are averaged, based on the stream flows, to develop a common set of blend components. This technique provides reasonable results when the streams have similar chemical natures. For example, all of the assay specifying streams are products from the crude distillation unit. However, when assay streams are dissimilar chemically, such as virgin materials and cracked materials, there may


be serious errors in the characterizations for the streams when a single set of lend components is used.

or this reason, you are allowed to define additional cutpoint sets. For example,

number

nd is iscussed in the Stream Data section of this chapter.

w may be reached from the PFD main window in

• Click

b Fan additional cutpoint set may be defined to represent the products from an FCCreactor. Note that it is not necessary or desirable to define a separate cutpoint set for each assay stream. Similar streams may be grouped by using the samecutpoint set without a serious loss of accuracy. This also minimizes the of components in the simulation, keeping calculation times smaller. The second step is supplying the petroleum stream laboratory assay data to PRO/II. This step is accomplished in the setup of initial feed streams ad TBP Cutpoint Sets TBP cutpoint sets are defined in the Assay Cutpoints and Characterization main data entry window. This windotwo ways:

with the distillation pseudocomponent curve on the toolbar, or

Primary Cutpoint Set is always provided as a default by PRO/II. ing cutpoint definitions:

select the menu bar item Input, then select the menu item Assay Characterization.

AThis set has the follow Cutpoint Range, Deg F Cutpoint Range, Deg C No of Cuts 100 - 800 38 - 427 28 800 - 1200 427 - 649 8 1200 - 1600 649 - 871 4 The default cutpoint ranges are usually reasonable for crude oil problems. They may be modified in the Assay Data Primary TBP Cutpoints Definition window which is accessed by clicking Modify... on the Assay Cutpoints and Characterization main data entry window. A convenient tabular form is provfor editing of the primary cutpoint set. Additional or Secondary cutpoint sets may be added to the problem by clicking

ided

Define New Cutpoint Set... on the Assay Cutpoints and Characterization maidata entry window to a

n ccess the Assay Data Secondary Set of TBP Cuts. A

window and a tabular entry form is provided w is also used to modify existing

cutpoint set name is supplied on this for definition of the cutpoints. This windosecondary cutpoint sets and is accessed by clicking Modify on the Assay Cutpoints and Characterization main data entry window and highlighting a


secondary cutpoint set in the Defined Secondary Sets list box, on the Assay Cutpoints and Characterization main data entry window. Highlighted secondary cutpoint sets in the Assay Cutpoints and Characterization main data entry window may be deleted by clicking Delete.... This action

r which a cutpoint set is not pecified. Initially, it is defined as the Primary Cutpoint Set by PRO/II. After one

en defined, the default cutpoint set may Assay Cutpoints and

e

s are shown in this window, with all options selectable with

line (default), Quadratic Polynomials, or Probability

urve Fit: Improved Fit or Ver 6 Fit

removes the secondary cutpoint set from the problem. The Default Cutpoint Set is used for all streams fosor more Secondary cutpoint sets have be

e changed via the drop-down list box on the bCharacterization main data entry window. It is convenient to define the cutpoint set which is used the most often as the default cutpoint set. Assay Characterization Options Assay characterization options are selected on the Assay Characterization Options window which is reached by clicking Characterization Options on thAssay Cutpoints and Characterization main data entry window. Several

roupings of optiongradio buttons. The option groups are as follows: Criticals, Ideal-Gas Enthalpy: SIMSCI (Twu) method (the default), Cavett method, or Lee-Kesler method. Molecular Weight: SIMSCI (Twu) method (the default), Old (1967) API method, or Extended 1980 API method. Gravity Curve Generation Method: Constant Watson K from TBP Curve (default), or Constant Watson K from D86 Curve. Distillation Curve Interconversions: API 1987 (the default), API 1963, API 1994, or Edmister-Okamoto. Fitting Procedure: Cubic SpDensity Function (PDF). Distillation Boundaries: Initial Point and End Point percentages. Include in PDF: Include Initial Boiling Point in fit, and/or include End Point in fit. Calculation of NBP for Cuts: Liquid Volume Average (default) or Temperature Midpoint. C


The characterization options are explained in greater detail in the PRO/II help nce Manual accessed via the Help menu.

s. The

ms are used to determine the energy q

anoGibhea Tramet d vap ort prop rigosiev ns. Transport properties are also reported in the strerepo In Pconmetvap ltiple ther ple, a defa for i A fa efined met may

lso e supplied.

text and the online PRO/II Refere Thermodynamic Data General Information The selection of appropriate thermodynamic methods is an important and necessary step in the solution of flowsheet problems. PRO/II provides a widerange of methods to allow solution of the wide variety of systems which occur in the chemical process industries. Thermodynamic properties are an integral part of the flowsheet calculation

LE) are used to determine the phaseequilibrium K-values (both VLE and Leparations. The enthalpies for the streas

re uired to take a system of components from one set of thermal conditions to ther. Entropies are used in the calculation of the isentropic operations and the bs free energy minimization reactor. Liquid and vapor densities are used in t transfer, pressure drop, and column tray sizing.

nsport properties are selected in conjunction with the thermodynamic hods in PRO/II and are comprised of liquid and vapor viscosities, liquid an

anspor thermal conductivities, and liquid diffusivities. While not strictly a trerty, liquid surface tension is also included. Transport properties find use in

s, pressure drop determination, and column rous heat transfer calculation tray and packing calculatioe

am properties reports and may be requested in Heating/Cooling Curves rts.

RO/II, the selection of thermodynamic methods has been simplified by the cept of the method set. Method sets consist of predefined thermodynamic hods for K-values (VLE and LLE), liquid and vapor enthalpies, entropies, r fugacities, and densities. Numerous predefined sets are provided. Muo

modynamic method sets may be selected for each flowsheet. For examult set may be specified for the overall flowsheet and other method sets used

ndividual units.

cility is also provided to modify the thermodynamic methods in the predod sets. Certain parameters for some of the thermodynamic methods h

ba


Selecting Predefined Method Sets

dow which may reached from the PFD main window in o ways:

Selection of thermodynamic method sets is accomplished via the Thermodynamic Data wintw

Click with the phase diagram on the toolbar or select the menu baitem Input/Thermodynamic Data.

r

ilibrium K-values, for each method set in the selected ategory appears in a drop-down list box and may be selected to add the

r the problem.

For convenience, several Categories of method sets can be selected in the list box on the Thermodynamic Data window. The Primary Method, i.e., the method

sed for calculation of equuCmethod set to the Defined Systems fo The Defined Systems appear in a list box and each may be selected for further action by highlighting the desired method and clicking Modify..., Delete..., and Rename... on the Thermodynamic Data window. The method set for which actionis to be taken is selected (highlighted) in the Defined Systems list box. Delete removes the selected method set from the problem. The Rename option is used

change the name of the selected

method set. This is useful when it is desired

ay be used for a wide variety of

UNIFAC.

culate all thermodynamic

Redlich-Kwong (SRK), SRK-Kabadi-

nson (PR), PR-Huron-Vidal (PRH), PR-anagiotopoulos-Reid (PRP), PR-Modified-Panagiotopoulos-Reid (PRM), BWRS WRS), Lee-Kesler-Plöcker (LKP), and Uniwaals (UNIWAALS).

toto use a method set more than one time in a problem, perhaps with different parameters. Modification of method sets is discussed later in this section. The following Categories of method sets are provided: Most Commonly Used: These method sets mproblems. Nearly all gas processing and oil refining calculations are handled satisfactorily. Method sets in this category are: Soave-Redlich- Kwong (SRK), Peng-Robinson (PR), Grayson-Streed (GS), Braun K-10 (BK10), Ideal, NRTL,

NIQUAC, and U Equations of State: Equations of state are applicable to wide ranges of

mperatures and pressures. They can be used to calteproperties, using the ideal gas state as the reference state. The cubic equations, in particular, are able to accurately predict critical and supercritical conditions. Equation of state method sets are: Soave-Danner (SRKKD), SRK-Huron-Vidal (SRKH), SRK-Panagiotopoulos-Reid (SRKP), SRK-Modified-Panagiotopoulos-Reid (SRKM), SRK-SIMSCI (SRKS), SRK-Hexamer (HEXAMER), Peng-RobiP(B


Liquid Activity: Liquid activity methods use liquid phase activity coefficient odels to represent the liquid mixture in phase equilibrium calculations. This

olution behavior.

Q s a u u i -ep- C 3

and Ideal.

zed Correlations: Generalized correlations predict K-values with semi-s equa yson- d and Chao-S r correlations u Kwo quatio vapo citie em l rela ships for the

ugacities. Braun K-10 is based on the convergence pressure concept. A of other correlations are used to predict the other properties, i.e., es, pies, and densities. Gener d correlations are: Brau

rayson-Streed (GS), Improved-Grayson-Streed (IGS), Grayson-Streed-SE ao-Se r (CS), o-Se E), a deal (IDEAL).

ac es: Sp l pack s are gned to solve a particulaial ap n. Special packages in PRO/II are: Alcohol (GLY Sou r (SO

MI d C PEN

ary ds: ateg f t ary thermod c are listed above. User-added Methods: This category includes all of the

5 user-added method sets that may be defined by the user.

O/II online help texts provide application guidelines for the various ethod sets, as well as a brief description for each method. More detailed

ay o e M abTable 8-1 at the en e e il o

amic methods u each predefined method set.

odifying Predefined Method Sets

ethod sets are modified via the Thermodyna c Data cation

mapproach is useful for modeling strongly nonideal liquid sMethods available in PRO/II include: NRTL, UNIUNIFAC, UNI

UAC, WilFAC TD

on, van L1, UNIFAC T

ar, MargDep-2, U

les, RegNIFA

lar Solutp-

on, FloryUNIFAC Fr

Huggins, ee TDe ,

Volume, Generali

rigorouRedlichliquid fvariety

tions. The Gng e

ran for

Streer fuga

eadepirica

se the s and tion

enthalpi(BK10), G

entro alize n-K10

Erbar (G

), Ch ade Cha ader-Erbar (CS nd I

Special Pindustr

kag ecia age desi r plicatioCOL),

(ALCOHOL), WATER), and Glycol r Wate UR), GPA Sour Water (GPS

Amine (A

NE) an APE-O .

All Primsets that

Metho This c ory includes all o he prim ynami

1

he PRTminformation m also be f und in the

of this sPRO/II R

ion givference

a detaanual (ald list of

so availe comp

le online). thermodyn

dsed for

ct s e th site

M Predefined m mi -Modifiwindow whichwindo

is ssed cking Modify... on the Th dyn Dataw.

d thermodynamic methods for the various thermodynamic ay t e cha in th dow by following the st iven

on thod own ox c pon to thperty

the replacement thermodynamic method.

acce by cli ermo amic

The preselecteproperties mbelow:

hen b nged is win eps g

Click the Current Me drop-d list b orres ding e Pro

Select type.


Any or all of the thermodynamic methods may be changed for the method set , g: K (VL val ), nt , vap

ropy, liquid density, vapor density, and vapor ere ble)

wly a d librarie k nam n be recogg box rar :Da N

rty-s data lso pplie /or fied is wi

being modifiedenthalpy, liquid entropy, vapor ent

includin -value E), K- ue (LLE liquid e halpy or

fugacity (wh Note: T

applica .

he nein this dialo

dde by Lib

s and dy Name

atabantabank

es in TDM caame.

nized

Some prope pecific may a be su d and modi in th ndow for the theData fie

rmodynamic me Enter Data... Property-spey met use sp ao difie tric f , et iorit ch a

efined for the selection of these parameters from more than one thermodynamic atabank. Note that thermodynamic databanks are supplied by SIMSCI and may

a he h th SC R m

pec c data wh ch apply only to the liquid activity methods include: fill ssing parameters, Henry’s Law options, and Poynting correction

s. For the liquid activity methods, a vapor fugacity method may also be

rty cific d which may be modified inc the nsione rection r amines DGA and M and key (

components in each liquid phase for K-value (LLE) methods. Key ent se on is o nal and PRO/II will determine them when not

owever, conve ce time nce s g the key s.

oper redict

s g da e “fi un er ms . Fen the comp ope a activity coefficient value t

finite dilution are known for some pair of species, you can use this option to redict missing activity coefficient values at intermediate concentrations.

LE and LLE K-value parameters for liquid activity coefficient methods may be stimated by the UNIFAC, Temperature-Dependent UNIFAC, Regular Solution, r Flory-Huggins methods, or they may be obtained from an azeotrope bank. The hoice of fill-in property prediction is entered on the Binary Data Fill Options

thods by clicking in the cific ld. Man

interaction fact of thers, mo

hods d acen

ecific pactors

rameters, such as c. A pr

binary order my sear y be

ddalso be prep

red by t user wit e SIM I LIBMG progra .

Property-soptions for miption

ifi i

oselected. Other prope -spe ata lude dime less residence timdominant)

cor factor fo DEA the or

componsupplied. H

lecti ptiorgen may be enha d by pre electin

component Fill-in Pr

ty P ion

PRO/II allowexample, wh

missin ta to bosition of an a

lled in”zeotr

der sevnd

al circu tances or s a

inp Veocwindow, which is reached by clicking the corresponding Enter Data... button on

e Thermodynamic Property Modification-Property Specific Data window. hecking the box will fill in missing data from the azeotrope databank. A method r filling in missing binary parameters (using the UNIFAC, modified UNIFAC, egular Solution, or Flory-Huggins methods) may be selected by choosing the ppropriate radio button.

thCfoRa


Equation of State Alpha Data

he form to be used for equation of state alphas may be specified on the Alpha TSelection w Thi w is ed by clickin pp Eindow. s windo reach g the a ropriate nter Data... butto T p i

The source of the alphas to ation of state may nated by selecting the appropriate radio button.

s La

enry’s sed cify whether or not He aw is to be conju with a liquid-activity K-value meth ow is b ght

n on the hermodynamic Pro erty Mod fication-Property Specific Data windobe desig

w. be used in the equ

Henry’

w

The Hused in

Law window is u to spe nry’s Lnction od. This wind rou

up by clickin r D n th o ic P y M icatiop ata w. C g the box on the Hen w

Henry’s Law to be used to determine the solubility of certain components. te nent eith det d b ro r

xplicitly by choosing the appropriate radio button. If the solute are to be designated explicitly, the desired solute components must

e selected from the list box on the Henry’s Law window.

g Co

ng Correction window is used to specify the use of the Poynting ctor for liquid-phase fugacities. The Poynting Correction window is

g Ente ata... o e Therm dynam ropert odif n-Property Scauses

ecific D windo heckin ry’s Law indow

Designationselected eomponents

of solu compo s may er be ermine y the p gram o

cb Poyntin rrection The Poynticorrection fabrought up by clicking the appropriate Enter Data... button on the

m per fica ope ecific Data w Th e ons g th ting tio

Th ice s th Po or will be used only if gacity method is chosen. ynting Corre Li cti rr

hasting C tion: n rrecti

e first two options is selected, then the molar volume calculation may b cted he g c : S d ( ol

ckett One-Fluid, or Library Density Correlations. The default method (2 olu

Resid ime ctio tor

ine Residence Time Correction window is available only for the Amine data p e th nam thod for K-values. It is accessedEnter Data... on the Thermodynamic Property Modification-Prope y Data window, then clicking LLE KeyComponents... on the LLE K-values

. A va the ce rre ctor for syst nt

Thermodyna ic Pro ty Modi tion-Pr rty Sp indow. ere arthree opti

to usin e Poyn correc n:

1. Default: a vapor fu

is cho specifie at the ynting c rection

2. Use Po ction to quid A vities: Use the Poynting co ection factor for the l3. Do Not Use Poy

iquid pn

e fugacity. orrec Do not use Poy ting co on factor.

If either of thmethodRackett, Ra

e sele from t followin hoices tandar 25°C) V umes,

is Standard

5°C) V mes.

Amine The Am

ence T Corre n Fac

special clicking Specific

ackag ermody ic me by rt

window lue for residen time co ction fa ems co aining


aminesfactor is 0.30.

MDEA or DGA may be entered in this window. The default value for this

y Components

y nts ow acce r an L K- l by c Ent ... Therm ynam

odification-Property Specific Data window, then clicking LLE Key ponents... on the LLE K-value window. Both the light liquid phase and the

heavy liquid phase can either be Determined During Calculations or User-specified by selecting the appropriate radio buttons. When the User-Specified radio button is chosen, a component must be selected in the associated drop-down list box. This drop-down list contains all available liquid-phase components. One component may be selected for each key. Note: The newly added libraries and databank names in TDM can be recognized in this dialog box by Library Name:Databank Name. Binary Interaction Parameters A number of methods in PRO/II allow the entry of binary interaction parameters. These include equations of state for many properties and liquid-activity-coefficient models for K-values. These parameters are entered on the Binary

LLE Ke The LLE Ke

ethod is seComponeected,

windlicking

can beer Data

ssed wheneveon the

LEic Prop

Valueerty m od

MCom

Interaction Parameters window, which is reached by clicking Enter Data... n next to Binary Interaction Parameters on the Thermodynamic Property Modification-Property Specific Data window. For each column of the grid, the two components for which the data is being entered must first be selected from the drop-down list boxes in the first two rows of the grid. Depending on the thermodynamic method set which has been selected, one or more parameters characterize the interaction between the two components. When the Binary Interaction Parameters window is initially brought up, the box at the top of the window must be checked in order to enable the grid where individual binary interaction parameters are entered. For the NRTL and UNIQUAC methods, there are several different forms of the binary interaction equations. For the NRTL method, the 5-Parameter equation is the default form. For the UNIQUAC method, the default is the 4-Parameter form of the equation. For these two methods, a different equation form may be selected for each component pair from the Equation Format drop-down list box, in order to enter the data in the most convenient form. Depending on the selection in the Equation Format list box, the appropriate rows in the grid become active. For most equation formats, many active parameters have default values of 0.0, except for the SRK-Modified Panagiotopoulos-Reid, PR-Modified Panagiotopoulos-Reid, Glycol, Sour, GPA Sour Water, and Amine methods, where the default value for parameters cij and cji is 1.0.


User supplied K-values A number of methods in PRO/II allow the user to overwrite the primary method K-values. The user supplied K-values are entered for all related components on the Thermo Properties - User supplied K-values dialog box.This dialog box is opened by clicking Enter Data... next to User supplied K-values on the Thermodynamic Property Modification-Property Specific Data window. The K-values are supplied through Thermodynamic Data - User supplied

-values dialog box by selecting either the correlated or tabular form.

User needs to supply K-value for at least 2 temperature points for

odification window can also overwrite the entire KVLE/KLLE method.

mic method, an excess enthalpy method may be Mixing window. This window is accessed by clicking

K Correlation Coefficient : Antoine equation is used as a default correlation with 1 atm as reference pressure. The coefficients have default values of 0.0.

abular Data : Tall the relevant components. Detailed information on default correlations is available in PRO/II Reference Manual. Selecting the “User Supplied” option for KVLE/KLLE in the Thermodynamic

roperty MP Heat of Mixing Data For the ideal thermodynapecified on the Heat of s

Enter Data... beside liquid enthalpy on the Thermodynamic Property-ModificatiData window, checking the check box and then clicking Enter Data on the Thermodynamic Property-Modification-Liquid Enthalpy window beside the Heat of Mixing data item. C

on

hecking the box on the Heat of Mixing window activates ree radio buttons, and the excess enthalpy calculation method may be selected

y choosing the desired radio button. If either of the Redlich-Kister Excess the Redlich-Kister binary parameters may be

ntered in the Binary Redlich-Kister Parameters window, which is accessed by

thbEnthalpy methods are chosen, theneclickany comdefault v .

ser-added Thermodynamic Data

added methods from the drop-down list box in the Primary Method field on the

ing Binary Data.... When entering the Redlich-Kister binary parameters for ponent pair, the Aij field is required and the other parameters have alues of 0.0

U To select a user-added thermodynamic method, select one of the fifteen user-


Thermodynamic Data window. The User-added Parameters window allows the input of parameters for user-added thermodynamic subroutines. For each row of

e grid, the parameter number (from 1 to 2600) is entered in the first column and the the second column.

Note: The User-added Subroutines supplement (an add-on to the stan-dard PRO/II package) is required for user-added thermodynamic methods. Contact your local SIMSCI office for more information. CAPE-OPEN Property Package The PRO/II CAPE-OPEN thermodynamics capability enables users to add third party CAPE-OPEN property packages to perform thermodynamic property calculations for streams on flowsheet. CAPE-OPEN standards are the uniform standards for interfacing process modeling software components developed specifically for the design and operation of chemical processes. These standards allow integration of different software components like Unit Operations and Thermodynamic Property Packages from different vendors into a single simulation. Selecting the CAPE-OPEN Property Package To install a new CAPE-OPEN Property Package, execute the install program provided by the vendor. The install program should perform all actions necessary to copy the files to your computer and set up the required entries in the Windows Registry. After installation, you can launch PRO/II and immediately use the new CAPE-OPEN software components. When a CAPE-OPEN is selected in the

e control filled with s. User must

rmation, components supported, the particular property package,

elect the CAPE-OPEN property package and click View. Property package and streams.

Pro

hen a Prop is selected for stream calculations or unit operation

thparameter value is entered in

“Category“ list box, a dialog will be displayed with a trestered CAPE-OPEN property packages and thermo systemregi

select property package. To view the vendor infoproperties supported and phase supported forsthermo system can be selected for unit operations

perty Calculations

erty Package Wcalculations, thermo properties like transport properties,enthalpy, entropy etc. will be calculated from the property package. For flash calculations, CalcEquilibrium will be called on property package. But, if the function CalcEquilibrium to propertypackage fails, flash algorithm of PRO/II will be used with properties like fugacity oefficients from property package. c


Defining Transport Properties Transport property methods are selected in the Thermodynamics –Transport Properties window which is accessed by clicking Transport Properties... on the Thermodynamic System –Modification window. Transport properties, i.e., viscosities, thermal conductivities, liquid surface tension, and liquid diffusivitiemay be selected on a global basis

s via radio buttons as: specify individually, pure-

mponent averages, petroleum-based correlations, the TRAPP method, or P method does not predict liquid

urface tension and the petroleum method is used to predict this property when

Vapor viscosities: None, pure-component average, petroleum correlation, d.

, iscosity,

Lohrenz-Bray-Clark, Twu viscosity w/Twu Bull mixing rule, API viscosity d), Medium Woeflin

od),

Vapor thermal conductivities: None, pure-component average, petroleum

Liquid thermal conductivities: None, pure-component average, petroleum i correlation, API 96 Procedure 12A3.2, ure), CAPE-OPEN, user-added.

ent average, petroleum re 10A3.2, CAPE-OPEN, user-

couser-added methods. Note that the TRAPsTRAPP is selected. Drop-down list boxes may be used to replace any of the global methods, with these options for the properties:

TRAPP correlation, Bromley-Wilkey correlation, CAPE-OPEN, user-adde Liquid viscosities: None, pure-component average, petroleum correlationTRAPP correlation, API correlation, SIMSCI correlation, kinematic v

w/Twu Bull mixing rule, Tight Woeflin (petro metho(petro method), Loose Woeflin (petro method), Tight Woeflin (pure method), Medium Woeflin (pure method), Loose Woeflin (pure methCAPE-OPEN, user-added.

correlation, TRAPP correlation, CAPE-OPEN, user-added.

correlations, TRAPP correlation, LatinAPI 96 Procedure 12A4.1 (High Press Liquid surface tension: None, pure-componcorrelations, Parachor/Tacite, API 82 Proceduadded. Liquid diffusivity: None, Wilke-Chang, User-supplied diffusivity data

Note: The None option for the methods above is available only if the Specify Individually option is selected for the Transport System. Liquid diffusivity: None, Wilke-Chang.


Note: A user-added method is not allowed for liquid diffusivity calculations. To select a user-added transport method, choose the User-added Subroutine ption from the Transport Properties window and select one of the five methods

otePROlocal SI The

anspo und in the PRO/II

at a

two-liquid erformed.

is

ofrom the drop-down list. N : The User-added Subroutines Supplement (an add-on to the standard

/II package) is required for user-added transport methods. Contact your MSCI office for more information.

PRO/II online help text provides additional information about the variousrt property methods. More information may also be fotr

Reference Manual. Specifying Water Decant Options When a method set which supports two-liquid phase calculations is selected via the Thermodynamic Data window, the Thermodynamics -Liquid- Liquid Optionswindow appears. Radio buttons on this window may be used to specify thsingle liquid phase only be used in the calculations (the default) or that

hase calculations be pp For method sets that support water decant, the user may optionally select to decant water as a pure phase. The methods used for the decant water calculations are selected via radio buttons in the Water Options window whichreached by clicking Water Options... on the Thermodynamic System-Modificatwindow. The following options are available: Calculation of Water Solubility in Nonaqueous Phase: SIMSCI Method (the

efault), Kerosene correlation, Compute from Equation of

ion

State (SRK and PR

,

ven in the online help text and in the l.

dmethods only). Calculation of Decanted Water Properties: Vapor-Liquid Saturation ValuesSteam Tables and IAPWS-IF97 Steam Tables. Optionally, the user may also check a check box to use GPSA Data Book values for calculating the water partial pressure.

ore details on decant of free water are giMPRO/II Reference Manua


Table 8-1: Predefined Thermodynamic Method Sets MC

ost Vapor ommonly

Used: Primary Method (K-value)

Enthalpy

Enthalpy

Entropy

Entropy

Density

Density

Fugacity

Liquid Vapor Liquid Vapor Liquid Vapor

SR

oave- SRK SRK SRK SRK SRK API NONEedlich-

Kwong (SRK) PR

eng- PR PR PR PR obinson

(PR)

PR API NONE

Grayson-Streed (GS)

CP CP CP CP SRK API NONE

Braun-K10 BK10)

JG JG CP CP IDEAL API NONE (NRTL (NRTL)

IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIQUAC (UNIQUAC)


UNIFAC (UNIFAC)


Note: CP= Curl-Pitze

or acity

r method, JG = Johnson-Grayson method, API= API Method Equations of State: Primary Method (K-value)

Liquid Enthalpy

Vapor Enthalpy

Vapor Entropy

Liquid Entropy

Vapor Density

Liquid Density

VapFug

BWRS (BWRS) BWRS BWRS BWRS BWRS BWRS BWRS NONE Peng-Robinson

R) PR PR PR PR PR PR

(PNONE

PR-Huron-Vidal (PRH)

PRH PRH PRH PRH PRH API NONE

PR-Panagiotopoulos-Reid (PRP)

PRP PRP PRP PRP PRP API NONE

PR-Modified- PRM PRMPanag.-Reid (PRM)

PRM PRM PRM API NONE

Soave-Redlich-Kwong (SRK)

SRK SRK SRK SRK SRK API NONE

SRK-Kabadi-anner (SRKKD)

SRKKD SRK D

KD SRKKD SRKKD SRKKD API NONE

SRK-Huron-Vidal SRKH SRKH SRKH SRKH SRKH API NONE


(SRKH) SRK- SRKP SRKPPanagiotopoulos-Reid (SRKP)

SRKP SRKP SRKP API NONE

SRK-Modified- SRKM SRKM SRKM SRKM SRKM API Panag.-Reid

NONE

(SRKM) S(S

RK-SIMSCI SRKS SRKSRKS)

SRKS SRKS SRKS API NONE

SRK-Hexamer (HEXA)

HEXA HEXA HEXA HEXA HEXA API NONE

Lee-Kesler-Plöcker

LKP LKP LKP LKP LKP API NONE

Uniwaals (UNIW) UNIW UNIW UNIW UNIW UNIW UNIW NONE

eneralized Vapor Liquid Vapor GCorrelations: Primary Method (K-value)

Enthalpy

Enthalpy

Entropy

Entropy

Density

Density

Fugacity

Liquid Vapor Liquid Vapor

B(B

raun-K10 JG JG CP K10)

CP IDEAL API NONE

Chao-Seader (CS)


Chao-Seader- CP CP CP CP SRK Erbar (CSE)

API NONE

Grayson-Streed (GS)


Grayson-Streed-Erbar


(GSE) Improved-Grayson-Streed (IGS)


Ideal (IDEAL) IDE AL IDEAL NONE NONE IDEAL IDEAL NONE


Special Vapor Liquid Vapor LiquPackages: Enthalpy Enthalpy Entropy

id Entropy

Vapor Density

Liquid Density

Vapor Fugacity

Primary Method (K-value)

Alcohol SRKM IDEAL SRKM SRKM SRKM (NRTL)

IDEAL IDEAL

Amine MINE)

SRKM AMINE SRKM SRKM (A

SRKM IDEAL NONE

Glycol (GLYCOL)

SRKM SRKM SRKM SRKM SRKM API NONE

Sour Water SRKM IDEAL SRKM SRKM SRKM IDEAL NONE (SOUR) GPA Sour Water (GPSWAT)

SRKM IDEAL SRKM SRKM SRKM IDEAL NONE

Liquid Activity: Primary Method (K-

Vapor Enthalpy

Liquid Enthalpy

Vapor Entropy

Liquid Entropy

Vapor Density

Liquid Density

Vapor Fugacity

value) NRTL (NRTL) IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIQUAC IDEAL (UNIQUAC)

IDEAL NONE NONE IDEAL IDEAL IDEAL

UNIFAC NIFAC)

IDEAL IDEAL NONE NONE (U

IDEAL IDEAL IDEAL

Wilson (WILSON)

IDEAL IDEAL NONE NONE IDEAL IDEAL NONE

van Laar (VANLAAR)

IDEAL IDEAL NONE NONE IDEAL IDEAL IDE

AL

Margules IDEAL IDEAL (MARGULES)

NONE NONE IDEAL IDEAL IDEAL

Regular IDEAL IDEAL NONE NONE IDEAL IDEAL IDEAL Solution

(REGULAR) Flory-Huggins (FLORY)


UNIFAC TDep-1 UNIFAC

IDEAL IDEAL NONE NONE IDEAL IDEAL

Dep

IDEAL

(T -1) UNIFTDep-2 (UNIFAC TDe

IDEAL AC IDEAL IDEAL NONE NONE IDEAL IDEAL

p-2) UNIF IDEAL AC IDEAL IDEAL NONE NONE IDEAL IDEAL


Dep-3 T(UNIFAC TDep-3) UNIFAC Free Volume (UNIFAC


Free Volume) Ideal (IDEAL) IDEAL IDEAL NONE NONE IDEAL IDEAL NONE


Stream Data General Information This section of data is used to specify the thermal conditions and compositions for all feed streams in the flowsheet. It may also be used to furnish initial estimates of the composition and thermal conditions for recycle tear streams to enhance recycle convergence. Supplied data for tear streams or any other streams which are products from unit operations are used as estimates only and always replaced by the next calculated set of values. Finally, Referenc

ay be defined to eliminate thermal recycles. e streams

o types: composition fully defined in terms of efi

assapar Compo r volu ide both a lstre weight curves may optistrea The stredefinedliquid. F

ntering Stream Data

appears contains any data you previously entered (as well as default values) for m.

:

m

ompositional streams may be of twCd ned components, or pseudocomponents to be generated from petroleum

y data. Reference streams are always assigned the composition of the ent stream.

sitions may be defined on a mole, weight, standard liquid volume or vapome basis, corresponding to typical laboratory data. It is necessary to prov

aboratory distillation and stream average gravity for petroleum assay ams. Light ends analyses, gravity curves, and molecular onally be furnished to improve the characterization of petroleum assay

ms.

am thermal conditions may be specified in a variety of ways including: temperature and pressure, bubble or dew point conditions, or fraction or reference streams, only the temperature and pressure may be defined.

E You can enter data for a stream on the flowsheet. The data entry window that

the selected strea To enter data for a stream

Double-click on the stream or right-click on the unit icon and select Data Entry... or select the stream and choose Input/Data Entry... from the menu bar.

Select the desired stream operation.

he stream name automatically assigned bTu

y the program is displayed in the pper le m ft hand corner of this window and may be edited as desired. If the strea


is an intermediate or product stream, a check box appears on this window so that for the stream. an initial estimate may be supplied

Select the Stream Type.

Figure 8-1: Stream Data Entry Window - Feed Stream

Spe s Within t

Composition Defined radio button.

ad basis as: Total Fluid Rate,or

d

Theon a monot defined a ed zero flowrates. If the total fluid rate was not given, the

cifying Composition Defined Stream

he Stream Data main data entry window:

Select the Click Flowrate and Composition to access the Flowrate and Composition

window. R io buttons are used to select the stream flowrate Individual Component Flowrates. A data entry box adjacent to the Total Fluid Rate button is used to enter the total stream flow in mole, mass, standard liquiolume, or standard vapor volume units. v

stream composition is supplied in a drop-down list box, and may be supplied

le, mass, standard liquid volume, or standard vapor basis. Components re assign


flowdisplays or the composition as it is entered.

hen the total fluid rate is supplied and the composition does not sum to that ing composition percentage or

action) an error is signaled. Optionally, a check box is provided to normalize the com ignaled for the above condition.

st be entry window. Two specifications must

is selected as Temperature or Pressure via e First Specification drop-down list box and the value entered in an adjacent

data The cification drop-down list box as: Pre , or Liquihave an data entry field. Thus, the thermal condition may be:

w point (pressure defined, temperature calculated). Bubble or dew point (temperature defined, pressure calculated).

d, pressure calculated).

sed.

ithin the Stream Data main data entry window:

troleum Assay radio button. the Flowrate and Assay window.

The ata entry field provided as

eight or liquid volume units. The cutpoint set for the blend may be selected by

cluded in. This option is the default and includes the seudocomponents generated for the stream in the assay blending for the utpoint set. The excluded from option is used when the assay stream is a

recycle estimate and the effect of its estimated pseudocomponents on the assay

rate for the stream is taken as the sum of the stream composition. PRO/II a running total f

Wrate or a rate of 100.00 ± 1.0 or 1.00 ± 0.01 (indicatfr

position based on the specified total fluid rate, in which case no error iss Specifying Stream Thermal Condition The thermal condition for all supplied streams except reference streams muspecified on the Stream Data main databe supplied. The first specificationth

entry field.

second is chosen from the Second Spessure, Bubble Point, Dew Point, Liquid Mole Fraction, Liquid Weight Fraction

d Volume Fraction. The pressure and the liquid fraction specifications adjacent

Defined temperature and pressure. Bubble or de

Liquid fraction (pressure defined, temperature calculated). Liquid fraction (temperature define

The temperature and pressure may optionally be specified for a reference stream. If not specified, the thermal conditions for the parent stream are u Specifying Petroleum Assay Streams W

Select the Pe Click Flowrate and Assay to enter

flowrate for the assay stream is entered in the dwclicking the hypertext string default set of TBP cutpoints to retrieve a list of the problem cutpoint sets. The pseudocomponent blending option is selected by clicking the text string inpc


blend es is not wanted. Entry of the various assay data is discussed below. More ihelp text and Laboratory D

propertinformation on the various laboratory tests is given in the PRO/II the PRO/II Reference Manual.

istillation

Click en r labora

Selec(TBP), ASTM D86, ASTM D1160, or ASTM D2887.

Weight. Liquid

f the laboratory pressure in the data field provided. For

m Therequi o points are givequa

oints f distillations. PRO/II needs the entire distillation curve om zero percent to one hundred percent and extrapolates and interpolates as

tions outside of PRO/II, sing their knowledge of the stream being characterized.

dow as: API Gravity, Specific Gravity, or Watson K-Factor. The stream verage value must be supplied in the data entry window provided. Optionally, a

Define/Edit Assay... on the Petroleum Assay Stream window to te the Assay Definition window. This window is used to enter the

tory assay data for the petroleum stream. t the type of distillation via radio buttons as: True Boiling Point

he basis for the distillation may be chosen as: Liquid Volume or T

Volume is the default for all distillations except the ASTM D2887 which is defaulted as weight. Note that gravity and molecular weight curves must be on the same basis, volume or weight, as the distillation curve. The distillation data for TBP, ASTM D86, and ASTM D1160 are assumed to be at a pressure basis o4.696 psia. If not, enter 1

ASTM D86 distillations, a Correct for Cracking check box is provided for application of the API Data Book cracking correction to the distillation te peratures.

distillation data are entered in the table provided. At least two points are red when the cubic spline fitting method is used. When only tw

n, PRO/II uses a probability density function to fill in the curve. For the dratic fitting option, at least three points must be given for TBP’s and five

or other types ofpfrnecessary. Wise engineers perform their own extrapolau Gravity Data The type of gravity data is denoted by radio buttons on the Assay Definition winagrawindow Gravity Curve window which provides a convenient tabu

olecu

vity curve for the stream may be given by clicking Gravity Curve... on this to access the Assay

lar form for entry of the gravity curve.

M

lar Weight Data

A molecular weight curve may be optionally given by clicking Molecular Weight... n the Assay Definition window to access the Assay Molecular Weight Data o


win eight urve. Optionally, the stream average value may also be supplied in this window.

dow. This window provides a tabular form for entry of the molecular wc Lightends Data Lightends data may be optionally provided by clicking Lightends... on the Assay Def nds Data window. The lightends comstandar ponent that Several l lightends flow. These choi re:

re kept in the same proportions as the upplied composition (the default).

s rate is a specified fraction of the total stream

s composition does not

Per rate volume or weight may also be selected in the Basis drop-

selected, the basis for the distillation curve is s composition does not 0.01 (indicating

omposition percentage or composition fraction) an error is signaled.

se Compositions as Actual Rates: The supplied composition is assumed to

t add n

tal which does not equal fraction, percent or a supplied rate and does not add

inition window to access the Assay Lighteposition may be entered on a mole, mass, standard liquid volume, or

d vapor volume basis. Any library component or petroleum com was defined as a PETRO component may be designated as a lightend.

choices are available for specification of the totaces are selected via radio buttons and a

Match to TBP Curve: The lightends rate is determined such that the normal boiling point for the mid percent of the highest boiling lightend exactly matches the TBP curve. The lightend components as

raction of Assay: The lightendFrate. A basis of liquid volume or weight may also be selected in the Basis drop-down list box. If no basis is selected, the basis for the distillation curve is

ssumed. When this option is chosen and the lightendaadd to the specified fraction or to 100.0 ± 1.0 or 1.00 ± 0.01 (indicatingomposition percentage or composition fraction) an error is signaled. c

cent of Assay: The lightends rate is a specified percent of the total stream

asis of liq. A b uid down list box. If no basis is assumed. When this option is chosen and the lightendadd to the specified percent or to 100.0 ± 1.0 or 1.00 ±c

Ube component flows, not fractional composition or percentage composition. Lightends Rate: The lightends rate is supplied directly in the data entry field provided. When this option is chosen and the lightends composition does noto 100.0 ± 1.0 or 1.00 ± 0.01 (indicating composition percentage or compositiofraction) an error is signaled. Optionally, a check box is provided to normalize the composition based on the specified total lightends rate, in which case no error is signaled for a composition toto 100.0 ± 1.0 or 1.00 ± 0.01.


Stream Thermal Conditions The thermal conditions for petroleum assay streams are specified in the same fashion as that already discussed for compositionally defined streams.

lculations as needed. For many problems, the default techniques are

be

etting Recycle Convergence Options

ence options are entered in the Problem Recycle Convergence nd Acceleration Options window which may be reached from the PFD main

Specifying Recycle Streams The PRO/II calculation engine recognizes recycle loops and automatically sets up loop casatisfactory. For complicated flowsheets with nested recycle loops, the user may prefer to define the loop calculation details. Acceleration techniques can alsoapplied to speed closure of the recycle tear streams. S Recycle converga

window by clicking on the toolbar. The following Recycle Convergence ptions can be selected with radio buttons:

t streams

indow. These tolerances are used

m one iteration

o

her.

le fraction to test for convergence may be hanged from the default value of 0.01 by clicking on the linked text numeric

value. Note that for some problems such as amine plants, this threshold must be lowered to test the residual acid gas components in the recycle amine solution.

O

onverge all Streams: Convergence is not attained until all flowsheeCare converged within the recycle tolerances. This is the default. Converge only Tear Streams: Convergence is reached when all tear streams are converged. This is the option used by the SIMSCI PROCESS Simulation

rogram. P

lobal recycle tolerances may be set in this wGfor all loops except user specified loops in which tolerances are supplied. Tolerances may be specified as relative or absolute via drop-down list boxes. Tolerances are: Component: Permissible change in a stream component rate froto another. The default is 0.01 on a relative basis. Temperature: Allowable change in a stream temperature from one iteration tanother. The default is ±1.0°F or equivalent. Pressure: Allowable change in a stream pressure from one iteration to anotThe default is 0.01 on a relative basis. The smallest stream component moc


Frequency of intermediate printed results for recycle calculations may be selected by clicking the underlined value in the print statement: Print recycle tream composition every 0 recycle iterations.

licking the underlined value in the trials statement: Set default

tion): This is the default.

llowing additional options may be chosen with Wegstein by clicking underlined defa firsaccele and App When this opti ing the u

s The number of recycle trials to allow before nonconvergence is signaled may be

ntered by cemaximum number of trials for each recycle loop to 20. Note that this is a global value which may be superseded for a user specified loop.

cceleration options are chosen via radio buttons: A

irect Substitution (No AcceleraD Apply Wegstein Acceleration: Use the Wegstein acceleration method. The fo

ult values: t iteration to accelerate (default is 2), iteration interval for ration (default is 1), Wegstein lower and upper factors (defaults are -5.00

0.00)

ly Broyden Acceleration: Use the Broyden acceleration method. on is selected, the first iteration to accelerate may also be supplied by click

nderlined (linked text) default value of 2.

Ordinarily, all recycle tear streams are accelerated. Click Accelerated Tear Stretwo Accelerate All Tear Streams:

plied to these tear streams in the

s, the user must first select the Alternate or n sequence methods in the Problem

alculation Sequence window.

User-specified Recycle Loops on the Problem Recycle vergence and Acceleration Options window to reach the User-

ams... to access the Accelerated Tear Streams window. This window has options available:

This is the default. Accelerate User-specified Tear Streams: When this option is selected, tear streams are selected in a drop-down list box and moved to the Accelerated

treams list box. Acceleration is only apSAccelerated Streams list box. User-specified Recycle Loops To select user-specified recycle loopExplicitly Defined by User calculatioC

ClickConspecified Recycle Loops window.

Then, click the check box beside User-specified Recycle Loops.


A tabula line in the table has

r form is used to supply recycle loop information. Each drop-down list boxes which are used to select the Starting Unit and the

Ending clicked to enter add Informa ich may be entered in this window includes:

umber of Trials: Number of iteration trials before nonconvergence is signaled.

the l

pplied in this window.

t Substitution, Wegstein Acceleration,or tear by

lickitera ctors (defaultalso

Unit for each loop. The adjacent Enter Data... button is itional recycle information via the Individual Recycle Loop Data window.

tion wh

NIf not supplied, the global value is used. Recycle Stream Convergence Tolerances: Tolerances may be supplied for Component, Temperature, and Pressure changes. A threshold component levemay be supplied by clicking the underlined (linked text) default. Note that the lobal defaults are used when values are not sug

cceleration Options: The DirecA

Broyden Acceleration methods may be selected for acceleration of the stream. The following additional options may be chosen with Wegstein c ing highlighted default values: first iteration to accelerate (default is 2),

tion interval for acceleration (default is 1), Wegstein lower and upper fas are -5.00 and 0.00). For Broyden, the first iteration to accelerate may

be supplied by clicking the highlighted default value of 2.


Sca Ge Sca the flowbe d t the exact q ith differenincl

o use the scaling feature:

ain

scaled from the Stream Name drop-down list

n

ed to the total of all components in

the scaled product stream, either the total stream or a specified nge of components, is supplied in the data entry field provided. The Units of

Measure feature

ling Product Streams

neral Information

ling provides an easy way to ratio all of the results in a simulation such that of one of the products is equal to a specified flow. For example, it may

esired to build a plant which produces a specified quantity of product, buuantity of feed required is not known. Instead of making multiple runs wt feed rates, one run may be made and the complete result scaled,

uding the feed rate such that the desired product rate is achieved.

T

Select the menu option Output from the menu bar of the PRO/II mwindow.

Select Report Format from the Output menu. Select Miscellaneous Data from the Report Format menu to access the

Miscellaneous Report Options window. Click Product Stream Scaling to display the Product Stream Scaling

window. Click the check box beside Scale Stream Flowrate. Next, pick the stream to be

box in the Product Stream Scaling window and select the stream components on which the scaling rate is based, with the radio buttoprovided. The default is All Components.If the Range of Components isselected, the starting and ending components are chosen in drop-down list boxes and the scaling rate is applithis range.

The rate for ra

may be used to supply the scaling rate as moles, mass, d liquid volume units, or standard vapor volumstand

Nons Som are dep d pressurthe pipescaling followin

ar e units.

leable Unit Opca erations

e unit operation results are not scaleable, that is, the calculated resultsendent on the absolute flow through the unit. For example, the calculate

e drop through a pipe of specified diameter depends on the flow through and may not be directly scaled for other flowrates. PRO/II disables the option when unit operations are present which are nonscalable. The g unit operations are nonscalable:

Column Hydraulics, Rigorous Heat Transfer, Pipe, Depressuring, PlugFlow Reactor.


Specify

refere tream is a stream of identical composition to its parent stream. h th

referencThis co

ret veReferenOptionarate of t Optionastre . hermal conditions of the parent stream are used. Copying Stream Data PRO/II allows you to copy the thermal and composition data for a selected st m.st m another Creatin In the PRO/II main

Select the desired stream to copy by clicking on the stream label with the mouse.

Choose Copy on the Edit menu. Click the left mouse button on an unoccupied area of the PFD main

win d stre

T at lows:

The cur all “s” visible to indicate that the PFD is n

lable exit ports for a

unit icon.

ing Reference Streams

nce sAW en e composition of the parent stream changes, the composition of the

e stream is immediately updated to be the same as the parent stream. ncept is very useful in eliminating thermal recycles in flowsheets.

Reference streams are designated by double-clicking the stream on the PFD to

rie the Stream Data main data entry window, selecting the radio button ced to Stream, and choosing the parent stream in the drop-down list box. lly, a rate may be supplied for the reference stream. If not supplied, the he parent stream is assumed.

lly, a temperature and pressure may be specified for the reference If not specified, the tam

rea Process data for a selected stream can be copied to a new flowsheet rea or can be used to replace (overwrite) the currently existing data in

selected stream.

g a New Stream from an Existing Stream

window:

dow or choose Select None on the Edit Menu to deselect the selecteam.

he d a for the selected stream can now be copied to a new stream as fol

Choose Paste on the Edit Menu.

sor will change to an arrow with a smow in stream mode.

Create a new stream by clicking the left mouse button on an unoccupiedarea of the PFD main window or on one of the avai


Drag the mouse to the desired unoccupied area of the PFD or feed pof another unit.

ort

Release the mouse button to complete the creation of the stream. Create a

se button or press <Esc> to exit stream mode. T ew and des tream.

in In e

left mouse button.

on an unoccupied area of the PFD main

The datstreams

u. The tstream( riding any existing. For compositionally-defined streams ontaining calculated data, PRO/II allows the user to copy the calculated data

( or compos

Select the desired compositionally-defined stream to copy by clicking on

se Copy on the Edit menu. Select the desired destination stream(s) with the left mouse button.

You may choose to paste only the input data of the selected stream or paste the inp a n, or liquid

dditional duplicate streams if desired, or

Click the right mou

he n ly created stream(s) will have the same thermal conditions, composition,cription as the original source s

Copy g Data From One Existing Stream to Another Existing Stream

th PFD main window:

Select the desired stream to copy by clicking on the stream label with the

Choose Copy from the Edit menu. Click the left mouse buttonwindow or choose Select None on the Edit menu to deselect the selected stream.

a for the selected stream can now be copied to one or more existing as follows:

Select the desired destination stream(s) with the left mouse button. Choose Paste on the Edit men

da a from the original source stream will be copied to the destination s), over

ctemperature, pressure, and one of total composition, liquid composition, or vap

ition) into the designated stream(s).

the stream. Choo

Choose Paste Special from the Edit menu.

ut d ta and calculated data (using the total composition, or vapor compositio composition).


N

ams ream properties.

n the

Cop The Streata fro opy input stream data from one simulation database to another, you must use

ct File/Open menu to open the first database. g o

Link The acrosscalculat n database. When mod

Qui am

c Avo am data

eac To def

ng on it.

ote: • Copy/Paste of an assay stream on to the product stream changes

the blend option to XBLEND. This is because the product streare not involved in the calculation of new st

• The Paste Special option is not allowed if new pseudocomponents generate i.e., flowsheet resets. Again, Paste Special can be enabled by generating the calculated data.

• Pasting a calculated data of an assay stream using Paste Special (total composition, liquid composition, or vapor composition) otargeted stream will erase their assay composition data if a new pseudocomponent is generated anywhere in the flowsheet.

ying Input Stream Data Across Simulation Databases

am Data Link feature described previously will only transfer calculated m the source stream to the input data slots of the destination stream. Tod

cthe Windows Clipboard. To transfer input stream data from one database to another:

Sele Highli ht the stream of interest and copy the input data of this stream t

the Windows clipboard by using the Edit/Copy menu. Open up the second database using the File/Open menu. Paste the clipboard data into the destination stream using the Edit/Paste

Special menu.

ing Stream Data Across Simulation Databases

Stream Data Link feature allows for the transfer of calculated stream data PRO/II simulation databases. By using this feature, you can copy ed stream data from a source database to the input data of a destinatio

eling a large flowsheet, this practical feature enables you to:

ckly make use of stream data previously calculated in an upstrese tion of the plant

id possible simulation errors due to manual re-entry of streEasily model each section of the flowsheet as a separate simulation, with

h section connected by a stream data link.

ine a Stream Data Link:

Highlight the stream to be linked to a previous database by clicki


Select the Define Stream Data Link option from the Input menu.

ngs up the Define Stream Data Link window as shown in Figure 7-15. In dow you m

This brithis win ust select both the name of the previously-run database file, and

Browse button to select from a list of available database files.

se t from a list of available streams.

the stream from that simulation to be linked to your current simulation.

Click on the Define Link check box. Enter the name of the previously-run database file, or click on the

Enter the name of the stream from the previously-run database to be linked to the stream in your current simulation, or click on the Browbutton to selec

Click to return to the main PFD.

ote: You caN n link a stream in the current flowsheet to another stream in the m to

Upd You ma data link while defining that link, or you may update all defi To up

To upd

the two simulation databases, some carded during the data transfer. If the

n.

ord file and then re-import the keyword file.

same flowsheet. This includes linking the input of the currently selected streathe calculated output data for that stream.

ating Stream Data Links

y update a stream ned links at a later time via the Input menu.

date a Stream Data Link while defining that link:

Check the Update Now check box in the Define Stream Data Linkwindow.

Click Modify.

ate all defined Stream Data Links:

Select Update Stream Data Links menu option from the Input menu. Note: If the components are different inomponent rate information may be disc

source stream has rate information for a component which is not present in the second database, that rate information will be ignored. If the source stream contains assay pseudocomponents, no component data will be copied to thearget stream unless an identical assay exists in the current (target) simulatiot

Note: All stream data link information will be lost if you export the simulation data o a PRO/II keywt


Ref r ed Properties Refiner and User-defined Special Properties are available

PRO/II for calculating bulk stream properties. The stream values of the ance

Ref r n Properties comprises fifty-three predefined properties, com o ng and specifying unit operation perf ndex, sulfur content, pour point, kinematic iscosity.

e.

sing Refinery Inspection Properties and User-defined Special Properties

Refinery Inspection Properties and User-defined Special Properties are used in the following ways: Glo a Global pthe Comthe flowdescribe Through the Stream Data Window For streRefineryentered

hroug

re than one thermodynamic system in the flowsheet, some erties may be specified for use in one system and others in another.

Component data for each specified property can also be entered for each thermodynamic system. Any component data entered for a thermodynamic system will be used in preference to the data provided globally wherever that thermodynamic system is invoked.

ine y Inspection and User-defin

y Inspection Propertiesinproperties can be included in the PRO/II output and can be used in performspecifications.

ine y Inspectiom nly used by refineries for measuriormance. Examples are cetane i

v User-defined Special Properties can be defined for any other property for which component data or assay data can be provided. Possible examples include autoignition temperature, color, $/tonn Uin a Flowsheet

b lly Through the Component Properties Window

roperty data for each component in the flowsheet are entered through ponent Properties window. Values entered here are used everywhere in

sheet unless overridden through the Thermodynamic Data window, as d below.

ams that are to be defined in terms of assay curves, stream values of Inspection Properties and User-defined Special Properties can be

either as curves or as average values or both.

h the Thermodynamic Data WindowT The properties that are to be used are specified in the Thermodynamic Data

indow. If there is mowprop


Note: A property is available only if it has been specified for a thermodynamic stem through the Thermodynamic Data window and is available only in those it operations where that thermodynamic system is used.

rough the Component Properties

onent e in the

en through the Thermodynamic Data window.

efinery Inspection Properties

y:

syun Entering Global Data ThWindow Global component data are entered for each component through the CompProperties window of PRO/II. Values entered here are used everywherflowsheet unless overridd R To enter component refinery inspection property data globall

Click on the toolbar or select Input/Component Properties.... The Component Properties window ap

Click Refinery Inspection Propertiespears.

to bring up the Component Property s window. drop-down list box.

Selection for Refinery Inspection Propertie Select a property from the Property Name Click Enter Data... to enter global values. If the property is Kinematic

inematic Viscosity window will y for Refinery Inspection and ill open. lue or an Index value. For plicable and no index values

c Viscosity, enter values at

dividual component values

ection Properties for some ntered in the input. If no data hosen through the

al property data

Viscosity, the Component Data Entry for Kopen. Otherwise the Component Data EntrUser-defined Special Properties window w

For each component enter either a Data vasome properties the index method is not apmay be entered. If the property is Kinematitwo temperatures.

The stream property value is calculated from the inusing a chosen stream mixing method. Note: The SIMSCI databank contains Refinery Inspcomponents; these data will be used if no value is eare present for a component, a fill method can be cThermodynamic Data window (see below). User-defined Special Properties To enter component user-defined speciglobally:


Click on the toolbar or select Input/Component Properties... from the w appears. ess the Component Property window. the Property Name drop- the list.

menu bar. The Component Properties windo Click User-defined Special Properties to acc

Selection for User-defined Special Properties Enter the name of a new Special Property in

down list box or select a special property from Click Enter Data... to enter global values. The Component Data Entry for

Refinery Inspection and User-defined Special Properties window will open.

For each component, enter either a Data value or an Index value.

tering Assay Data through the Stream Data Window

r streams that are to be defined in terms of assay curves, stream values of efinery Inspection Properties and User-defined Special Properties can be tered either as curves or as average values.

efinery Inspection Properties

o enter assay data for refinery inspection properties:

Double-click on the stream on the PFD. The Stream Data window appears.

In the Stream Data window, click the Petroleum Assay radio button and then click Flowrate and Assay to access the Flowrate and Assay window.

En FoRen R T

In the Flowrate and Assay window, click Define/Edit Assay... to access the Stream Data - Assay Definition window.

In the Stream Data - Assay Definition window, first click the appropriate distillation method radio button and then click Refinery Inspection Properties to access the Assay Property Selection for Refinery Inspection Properties window.

Select a property from the Property Name drop-down list box. Click Enter Data... to enter global values. If the Property is Kinematic

Viscosity, the Assay Data Entry for Kinematic Viscosity window will open. Otherwise the Assay Data Entry for Refinery Inspection and User-defined Special Properties window will open.

Enter the property value(s) as either a stream average, curve against Percent Distilled or both. If the property is Kinematic Viscosity, enter values at two temperatures.

ser-defined Special Properties

o enter assay data for user-defined special properties:

U T


Double-click on the stream on the PFD. The Stream Data window appears.

In the Stream Data window click Flowrate and Assay to access the rate and Assay window. Flow

In the Flowrate and Assay window click Define/Edit Assay... to access the Stream Data - Assay Definition window.

In the Stream Data - Assay Definition window click User-defined Special Properties to access the Assay Property Selection for User-defined

new Special Property in the Property Name drop-

Special Properties. Enter the name of a

down list box or select a special property from the list. Click Enter Data... to enter global values. The Assay Data Entry for

Refinery Inspection and User-defined Special Properties window will open.

Enter the property value(s) as either a stream average, curve against Percent Distilled or both.

Ass d Special Pro The cified through the The thermodynamic system in th nd others i available only if it has been specified for a

ermodynamic system and only in those unit operations where that

omponent data for each specified property can also be entered for each

rties to a Thermodynamic

igning Refinery Inspection Properties and User-defineperties to Thermodynamic Systems

properties that are to be used in the simulation must be spermodynamic Data window. If there is more than one e flowsheet, some properties may be specified for use in one system a

n another. A property is ththermodynamic system is used. Cthermodynamic system. Any component data entered in a thermodynamic system will be used in preference to the component Global data wherever that thermodynamic system is invoked.

o assign refinery inspection propeTSystem:

Click or select Thermodynamic Data... on the Input menu bar iteThe Thermodynamic Data window appears.

Select the system for which modifications are to be made in the Defined Systems box.

m.

Click Modify... to access the Thermodynamic Data –Modification Window.

Click Refinery Inspection Properties. The Thermodynamic Method Selection for Refinery Inspection Properties window appears. This window has a table in which properties and associated parameters and


data will be entered. To eliminate the need to enter standard sets of properties repeatedly, predefined lists of properties have been set up.

To load the table with a predefined list of properties, select from the

s

• onent ns

i.

,

Predefined Lists list. Selecting None in this list removes all properties from the table. Select a property from the Property Name drop-down list box in the table.The available options and their default selections, determined by the property selected, are presented. Change these as required. The optionare:

Stream Method, which defines the method used to mix the compproperty values to produce a value for the stream. The available optioare:

Summation: The stream property value is determined by summing the product of the component property value and the component fraction. The fraction may be molar, weight or liquid volume and is calculated fromthe total stream dry composition except for kinematic viscosity when it is from the dry liquid part of the stream. Any Index data supplied for the property will be converted to property values before the summationusing the equation:

γ

Re

Index ValueReference Value ⎟

⎞⎜⎝⎛

×= Index ference ⎠

ii. t

e

Index: The stream property index is determined by summing the producof the component property index and the component fraction. The fraction may be molar, weight or liquid volume and is calculated from thtotal stream dry composition except for kinematic viscosity when it is from the dry liquid part of the stream. Before the summation, any supplied property values will be converted to index values using the equation:

γ⎟⎞

⎜⎛

×= Value

Index Reference Index ⎠⎝ ValueReference

he

a teger

.

This equation is then used to convert the stream index value to tstream property value.

iii. User-Formula: The stream property value is determined from the

equation in a user-added subroutine, which is linked into PRO/II. Datvalues may be entered for each component and up to 20 real and indata values may also be supplied


iv. User-Index: The stream property value is determined by a user-added subroutine, which is linked into PRO/II. The same data as for the Index

the user-added subroutine.

e

which specifies whether the component values will be ir mole, weight or liquid volume fractions.

b. No fill: This produces warning messages for missing data and set to 0.0. c. SIMSCI: This option estimates missing data by SIMSCI correlations for

n-hydrogen ratio.

PI: This estimates missing data by API methods for kinematic viscosity, pour point or refractive index.

smoke point.

re . The

y with no data is set to 0.0.

ose assays, which have data for this property.

method is available to

v. SIMSCI: This method is only available for cloud point and kinematic viscosity. It is an index method but uses specific index equations.

vi. API: API procedures may be used to calculate flash point, cetane index,

mean average boiling point, cubic average boiling point, molal averagboiling point or net heating value. The API method requires no component data.

vii. Nelson: This is an alternative correlation to calculate flash point and no

component data are required. viii. Stream Basis,

mixed using the

ix. Component Fill, which specifies the action to be taken when component values are missing for petroleum fractions in the stream. The availableoptions are:

a. Zero: This option sets the property value to 0.0.

kinematic viscosity, smoke point, hydrogen content, carbon content or carbo

d. A

e. Nelson: This option estimates missing data by Nelson method for

x. Component Blend, which defines the way in which missing data a

handled when calculating properties from blended assay streamsoptions are:

a. Zero: The property value for the cuts in the assa

b. Exclude: The property is calculated by blending only th


c. Missing: For this option, the blended property is not calculated and is reported as “Missing”.

Click Data... to enter data for this property, for this thermodynamic

system. If the Stream Method is defined as User-Formula, the User ula Data En . Otherw erty is

inematic Viscos ematic Viscosity Data Entry window will open and for other pro s, the Refinery Insp tion and User-defined

ial Propertie try window will In the Kinematic Viscosity Data Entry wind tion

and User-defined Special Properties Data r each component, enter either a Data value or a ach

onent, enter eithe Data value or an value tered, Refer x Data must als e

properties, the Index method is not applicanor Reference Index Data may be entered. If the property is Kinematic Viscosity, enter values at two temperatures.

e User Form ntry window, fo ter a Data value, which will be passed to a linke utine. Up to twenty real and integer values an also b ine. The meaning of the data are determined b routine.

User-defined Special Properties

user-defi ial propert namic System:

FK

orm try windowty, the Kin

opens ise, if the propipertie ec

Spec s Data En open. ow or the Refinery Inspec Entry window, fo

Index value. For encompis en

r a ence Inde

Index value. If an Index o be entered. For somble and neither Index values

In th ula Data E r each component, end User-added Subroe passed to the subrouty the calculation sub

To assign ned spec ies to a Thermody

Click or select Thermodynamic Data. m. The Thermodynamic Data window appear

Select the system for which modifications e in the Defined Systems list box.

.. on the Input menu bar ites. are to be mad

Click Modify... to access the Thermodynamic Data Modification Window. r-defined Prop ties. The Therm ction for

efined Pro indow appears. le in which properties, associated parameters a .

Enter the name of a new special property drop-down list box or select a special property f nge the available options r default selectio tions are:

• Stream Method, which defines the mcomponent property values to produce tream.

• Stream Basis, which specifies whethe ponent values will be mixed using their mole, weight or liquid

Click UseUser d

erperties w

odynamic Method SeleThis window has a tabnd data will be entered

in the Property Namerom the list. Cha

and thei ns as required. The op

ethod used to mix the a value for the sr the comvolume fractions.


• Component Blend, which defines the ing data are handled when calculating properties fr eams.

way in which missom blended assay str

Click Data... to enter data for this property mic system. If the Stream Method is defined a User Formula Data Entry window opens. Otherw ction and User-defined Special Properties Data

In the Refinery Inspection and User-define ta Entry window, for each component, enter e or an Index value. If an Index value is entered, Refere also be entered.

In the User Formula Data Entry window, fo r a Data value, which will be passed to a linked User-added to twenty real and integer values can also routine. The meaning of the data are determined b e.

Note: If you have assigned Refinery Inspection Pr ynamic method set, the standard Stream Data Report will Inspection properties.

g Refinery Inspection Properties and Us ecial s

ry Inspection Prop User-defined S n be

included in the PRO/II output reports.

Select Report Format from the Output menu. Next, select the

, for this thermodynas User-Formula, the

ise, the Refinery Inspewin Entry dow opens.

d Special Properties Daeither a Data valunce Index Data must

r each component, enteSubroutine.Up

be passed to the suby the calculation subroutin

operties to a Thermodinclude these Refinery

PrintinPropertie

er-defined Sp

Refine erties and pecial Properties ca

Miscellaneous Data... menu option. The Miscellaneous Report Options window appears.

In the Refinery Inspection and User-defined Special Properties box, check one or both of the following options: Include Input Data —for a printout or data that has been input and/or Input Program Data —for a printout of data generated by PRO/II.

For output of kinematic viscosity data:

Select Report Format from the Output menu. Next, select the Stream Properties... menu option. The Stream Property Report Options window appears.

Enter two temperatures at which the kinematic viscosity results are required.

BVLE (Validating Equilibrium Data) Tables and plots of binary equilibrium data for given pairs of components may be generated in order to ensure that they are valid in the required range of operation. Any thermodynamic VLE or VLLE K-value method may be used.


or liquid activity thermodynamic mF ethods (e.g., NRTL or UNIFAC), the following

d:

fficients, • Vapor fugacity coefficients,

nd

as equations of state or generalized orrelations, the following are determined:

licking ly available when at least two components and a

ate a BVLE plot or table:

are calculate

• K-values, • Liquid activity coe

• Vapor pressures, a• Poynting correction.

For non-liquid activity methods, suchc

• K-values, • Liquid fugacity coefficients, and • Vapor fugacity coefficients.

The validation is carried out in the PRO/II - Binary VLE/VLLE Data window which is opened by selecting the Binary VLE option from the Tools menu or by cBVLE toolbar. This window is onthermodynamic method have been selected. To gener

• Select from the Tools menu or click BVLE toolbar to bring up the Data window. PRO/II - Binary VLE/VLLE

• Click TDM Calculated BVLE to view x. Users can view all the comp

Component and Thermodynamic onents that has been used in the dialog bo

current flowsheet on the left-hand side of this dialog box. Use Diagram Tab to calculate and view BVLE plot and it’s associated data in the esheet format. Here, BVLE plots can be viewed similar to PRO/II, butplot uses TDM and Modthermo Data.

xcel this

the required components for the equilibrium calculations from the

• Next, select constant pressure or temperature operation and enter the

• Finally, click Calculate to generate plots (by default, all available plots will ted). If Excel is selected on the Plot Setup option, from the

Options menu, tabular data are available in the spreadsheet. Otherwise, only the plots are shown.

Note: For complete technical details, see the Utilities topic in the PRO/II Reference Manual.

• Select drop-down lists.

value.

be genera


Chapter 9 Unit Operations and Utility

eration models and the utility modules are r:

. . . . . . . . . . . . . . . . . . . . . 149

on . . . . . . . . . . . . . .190 olumn, Side . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .196

. . . . . . . . . . . .199 ontroller . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 204

Unit . . . . . . . . . . . . . . . . . . . . . . . . .218 issolver . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 223 xpander . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .224 lash . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 226 lash with Solids . . . . . . . . . . . . . . . . . . . . . . . . . . . 230 lowsheet Optimizer . . . . . . . . . . . . . . . . . . . . . . . . 231 eat Exchanger, LNG . . . . . . . . . . . . . . . . . . . . . .. .237 eat Exchanger, Rigorous . . . . . . . . . . . . . . . . . . . .239 eat Exchanger, Simple . . . . . . . . . . . . . . . . . . . . .249 eating/Cooling Curves . . . . . . . . . . . . . . . . . . . . . .253 ixer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 257 ultivariable Controller . . . . . . . . . . . . . . . . . . . . . .258 hase Envelope . . . . . . . . . . . . . . . . . . . . . . . . . . .261 IPEPHASE Unit Operation. . . . . . . . . . . . . . . . . . 263 ipe . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 267 olymer Reactor . . . . . . . . . . . . . . . . . . . . . . . . . . .272 rocedure Data . . . . . . . . . . . . . . . . . . . . . . . . . . . .274 ump . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 282 eaction Data . . . . . . . . . . . . . . . . . . . . . . . . . . . . .283 eactor . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 287 eactor, Batch . . . . . . . . . . . . . . . . . . . . . . . . . . . .301

Modules This chapter describes how to use unit operation models. Also described are the use of utility modules such as the Calculator, Controller, Flowsheet Optimizer and similar functionalities. For ease of reference, both the unit op

resented together in alphabetical ordep

alculator . . . . . . . . . . CColumn, Batch . . . . . . . . . . . . . . . . . . . . . . . . . . . . 170 Column, Distillation . . . . . . . . . . . . . . . . . . . . . . . . . 171

olumn, Liquid–Liquid ExtractiCCCompressor . . . . . . . . . . . . . . . . . . . CCrystallizer . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . .207

. . . . . . . . . . . . . . . . . . . . . . . . . . . 211 Cyclone . . . . . epressurizingD

DEFFFHHHHMMPPPPPPRRR


Solid Separator . . . . . . . . . . . . . . . . . . . . . . . . . . . .. 302 plitter . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . . 303 tream Calculator . . . . . . . . . . . . . . . . . . . . . . . . . . 305 PEC/VARY/DEFINE

d Uni. . . . . . . . . . . . . . 333

iped Film Evaporator . . . . . . . . . . . . .

SSS . . . . . . . . . . . . . . . . . . . . . . . . .308

. . . . . . . . . . . 321 User-addeValve . . .

t Operations . . . . . . . . . .

. . . . . . . . . . . . . . . . . . .

W

. . . . . . . . . . 334

Chapter 9 UNIT OPERATIONS AND UTILITY MODULES 149

Calculator

General Information

is a versatile utility module useful for a variety of purposes in may be retrieved from the flowsheet and

alculations performed using a FORTRAN-like language. Parameters may be e flowsheet for use by o for the lude:

special stream prating special processing

ining operating conditi Performing design calculations using flowsheet information

g special output values for reports Computing utility costs and economic functions

culating target values for C ctive functions for heet Optimizers

o means an exhaustive lis f this module is limited ingenuity of the user.

ll Calculators have two main sections: Setup and Procedure. In the setup d from the flowsheet, constants

ated results, a sequence table is set up

et component and stream information. Special subroutines are rovided for storing calculated results directly in flowsheet streams. Calculated sults may also be stored in the “Results” array, making them available to the

ther unit operations in PRO/II. A special solution “flag” is provided for use when Calculator models a unit operation.

he Calculator T

flowsheet simulation. Parameters creturned to th ther unit operations. Some usesCalculator inc

Calculating operties Simul units such as reactors Determ ons for other unit operations

Producin

Cal ontrollers or objeFlows

This is by n t; the usefulness oonly by the Asection, unit and stream parameters are retrieveare defined, names are assigned to calculfor the streams used for input and output, and the dimensions for the various working arrays may be expanded if desired. The Procedure section is where all calculations are performed, using a simple anguage based on FORTRAN 77. The language permits the use of lmathematical functions, branching and looping, and assignment statements commonly used in programming. Special intrinsic functions are available for etrieving flowsher

preoa


Calculator Setu

ng Edit/View Dec culator main data entry en the View Area:

p Start Setup by clicki larations on the Calwindow to op

Click Parameters… to retrieve e Calculator. These variables are accessed procedure as elements of array P. Click the Calculator p d text to open the Definition window where you can specify the stream or unit flowsheet parameter to

will find a list of the unit and stream

flowsheet parameters into th in the Calculatorarameter linke

be retrieved. The format for this window is identical to that used for the DEFINE and is described in the SPEC/VARY/DEFINE section of this chapter. In this window, youparameters that may be retrieved via DEFINE.

Click Constants… to enter the constant values. These variables are accessed in the Calculator procedure as elements of array C. Although you can enter constants directly in the procedure, this array provides a

that need to be updated occasionally into means for collecting constants a common location.

Click Results… to enter names for the Calculator results. These values are accessed in the Calculator procedure as elements of array R. Thenames will be used in the output report.

se

Click Stream Sequence… to define an ordered table of flowsheet streams. There are two functions for this table. First, it provides a necessary link between the procedure and the flowsheet streams for

the ms in

information flow. Second, a calculation loop may be performed inprocedure for a range of streams, using the positions of the streathe table to control the loop order.

Click Arrays… to declare the length of the storCalculator. These arrays include the P, C, R ar

age arrays used by the rays defined above, and

the IS array that is used to ho ariables. This array is described in the Calculator Procedure d ys appear here. In earlier versions of the had to reside in one of these arrays, V for r ow that any valid FORTRAN variable s are no longer needed. Nonetheless, they are still available so that older

arations to close the View Area.

ired and must end with a RETURN tatement.

ld stream viscussion. Two additional arra Calculator, all local variables

eal variables and IX for integers. N name can be used, these array

Calculators will work without rewriting.

Once Setup is complete, click Hide Decl Calculator Procedure Note: The PROCEDURE section is requs


The FORTRAN procedure is entered directly into the Procedure field on the alculator main data entry window. The procedure may be checked as is it

Procedure.

acters. The ampersand (&) at the end f a line denotes continuation of a statement on the following line. Note that an

ll lines of code except the PROCEDURE statement may be preceded by a

dollar sign ($) causes all following characters on the remainder of the line to be comment rather than as code. Unlike in FORTRAN, a ‘‘C’’ in

olumn one does not designate a comment statement.

arrays, ppear in the following table. Use a DIMENSION statement in the Calculator

ction to reset the number of elements in each array.

V, and R store values in floating-point form. Array IX stores integer ues. Forms of use include:

s any of C, P, V, R, or B and n is an integer indicating a single element ay.

(index)

here A is any of C, P, V, R, or B and (index) is an expression, such as (IX2 * 5). he parentheses are required. “A(n)” denotes the same element as “An”.

stead of, or in addition to the supplied V and IX arrays, standard FORTRAN ariables may be used. They may be up to 8 characters long and may not uplicate the names of any supplied variables; otherwise they follow the onventional FORTRAN rules. The introduction of this feature in PRO/II 5.0 eans that the V and IX arrays need not be used. If this is the case, the arrays

an be dimensioned to one word each to save memory.

Ccomposed by clicking Check The supported features of the language are discussed in the following sections. Elements of the Language Each statement may contain up to 80 charoasterisk (*) is not valid as a continuation marker, since it signifies multiplication. Aunique numeric label from 1 to 99999 (shown as ‘‘nn’’ in this manual). Ainterpreted as a c Predefined Variables Definitions of predefined variables, including default dimensions for asetup se Arrays C, P, val An where A if the arro

A wT Invdcmc


Array IS is normally used as the index of a DO loop to step through a sequence f streams in the order defined on the SEQUENCE statement.

may serve as the stream index in PRO/II intrinsic functions. The only form

s ISn. IS(index) is never valid

o

Itallowed i .

Predefined Variables

Variable Name

rm

Default Dimen(for arrays)

tion and ents

and Fo

sion DescrComm

ip

Cn or C(index) 1<=n<=50 nstant values defined in e setup section. Used only

on the right side of assignment statements

Coth

Pn or P(index) 1<=n<=50 Flowsheet parameters set by DEFINE statements. Used only on the right side of assignment statements.

Vn or V(index) 1<=n<=200 A floating-point work array used on either the left or right side of assignment statements. These elements are initialized to a large negative value and are not available outside the calculator.

Rn or R(index) 1<=n<=200 The array of calculator results, used on either side

flowsheet

of assignment statements. This results vector is available to other modules external to the Calculator. These elements are initialized to a large negative value.

IXn or IX (index) 0<=n<=9 An array of integer values. The form ioIX(index) is invalid on a DO statement. It may be used on either side of assignment statements.

ISn 0<=n<=9 An array of elements used as indices of DO loops for stepping through a series of


streams in the order defined on the SEQUENCE statement.

ISOLVE Th is variable indicates whether or not the

subsequent

has not yet executed (default) or has solved successfully. 1 The Calculator solved. 2 The Calculator did not solve, but continue flowsheet calculations within

4 The Calculator solved; but stop all subsequent flows heet calculations. This sets the flowsheet solution flag to ‘SOLVED’.

Calculator solved. It is initialized to 0 upon each entry into the calculation procedure. The user assigns allvalues using an assignment statement. 0 The Calculator

a recycle loop. 3 The Calculator did not solve, all calculations stop unconditionally.

MAXC Total number of

components in the problem.

MAXS Maximum number of streams in the problem.


FORTRAN Statements Procedure This statement marks the start of the Calculator. It is required.

FORTRAN-based procedure section of the

e. arated

cters long. Variables defined here may be changed the code. Variables not defined here are assumed to be real or integer

ords or predefined variables

EAL MASS

EAL REVENU(1990:1995), PROFIT(1990:1995),

A variable may only appear once in these statements. The following is

Bot REA

Declaration Statements REAL rname1, rname2(i), rname3(j,k) ... INTEGER iname1 , iname2(i), iname3(j,k) ... DIMENSION name1(i), name2(j,k) ... These statements are used to define local scalars and arrays for use in the codEach subscript may be an integer constant, or two integer constants sepby a colon to specify both the lower and upper array bounds. When defined by the DIMENSION statement, variables assume the normal FORTRAN convention that assigns names starting with I through N as integers, and all others as real. Name lengths may be 8 charainaccording to the first character. Variable names must not conflict with any reserved w(see table entitled Predefined Variables). Examples: DIMENSION A(20,20), B(20), X(20) RINTEGER COUNT, TAB(100) RLOSS(1990:1995)

ote: Nvalid in standard FORTRAN, but not in a Calculator Procedure: REAL MOLWT DIMENSION MOLWT(50)

h standard FORTRAN and the Calculator accept this equivalent form:

L MOLWT(50)


Ass nn variab The “exope 1. Expre2. F3. E4. Multip5. Addit With the calculations with the same precedence are valuated from left to right. Multiple exponentiations without parentheses to

ADVAL = A**B**C Note: T ay not appear on the left side of n assignment statement.

ntrinsic Functions

w can be used in

ignment Statements

le =expression

pression” is governed by standard FORTRAN conventions. The rations on a given statement are executed in the following order:

ssions within parentheses ( ) unctions xponential ( ** )

lications and divisions ( * ,/) ions and subtractions (+,-)

exception of exponentiation, eexplicitly specify the evaluation order are not permitted. For example, the following is invalid: B

he Calculator-supplied arrays Cand P ma FORTRAN I

ctions tabulated beloThe FORTRAN intrinsic funexpressions:


FORTRAN Intrinsic Functions Function Description Arguments Type of Result

Number Type

ABS

IM XP T

IN

IN

COATASINH COSTANH

Exponential e Truncation

Minimum Value

Sine (radians)

c Sine (radians)

ine

1 1

>=2

1 1

1

1

real real real real real real

real real

real

real

al real real integer real real real

real real

radian

real

Absolute Value Positive Difference

1 2

real reDEINLOG

OG10 Natural Logarithm Common Logarithm

1 1 L

MMAX MOD NINT

QRT

Maximum Value Remainder Nearest integer Square Root

>=2 2 1

real real real

real real integer

SSCOS TAN

SIN

Cosine (radians) Tangent (radians) Ar

1 1

real real

real real

AA S

N Arc Cosine (rad) Arc Tangent (rad) Hyperbolic S

1 1

real real

radian real

H Hyperbolic Cosine Hyperbolic Tangent

1 1

real real

real real

PRO/II The foll d ompon rties. In the table, “cno" represents an integer component

ction. Property values are retrieved in the UOM used for ro

Intrinsic Functions

owing table lists special functions that allow direct retrieval of stream anent propec

number which is an integer constant or variable, “sid” is a stream identifier or er must appear on the SEQUENCE statement to be used ISn value. This identifi

y a PRO/II intrinsic funbp blem input.


PRO/II Intrinsic Functions

nction Description of Property Fu

Pure Component Properties CMW(cno) CNBP(cno)

cno)CSPGR(CTC(cno

)

MEGA(cno)

Molecular weight Normal boiling temperature Specific gravity (60F/60F) Critical temperature Critical pressure Critical volume, cc/gm-mole Acentric factor

CPC(cno) CVC(cno) CO Properties of Components in Streams SCMF(cno,sid) SCWF(cno,sid)

VF(cno,sid)

Molar fraction of component in stream Weight fraction of component in stream Standard liquid volume fraction Molar rate of component in stream Weight rate of component in stream

ard liquid volume rate of component ard gas volume rate of component

SCSCMR(cno,sid)

WR(cno,sid) SCSCLVR(cno,sid) Stand

StandSCGVR(cno,sid) Stream Properties SMR(sid) SWR(sid)

d) SLVR(siSGVR(sid)

EMP(sid)

Mole rate of stream Weight rate of stream Standard liquid volume rate of stream Standard gas volume rate of stream Stream temperature Stream pressure

STSPRES(sid) Stream Property Storage Subroutines nn CALL SRXSTR(type, value, sid) A call to SRXSTR stores a Calculator vector element as a property of stream “sid”. Values being stored must be computed in the dimensional units used for data input. The resulting stream is flashed at the new conditions to determine its thermodynamic state. type This entry identifies the stream property to store. Available options are tabulated below.


Stream Properties Stored by SRXSTR

type= Description

SMR WR LVR

mole rate of stream weight rate of stream standard liquid volume rate standard gas volume rate of stream stream temperature stream pressure

SSSGVR

TEMP SSPRES value This argument supplies or identifies the value of the property to store. It an be a real constant or variable.

r

nt 14 from array R as the temperature of stream SR4.

lator array into a tream. The resulting stream is flashed at the new conditions to determine its

thermod

pe This entry identifies the component property to store in the stream.

tream Component Properties Stored by SRVSTR

c sid The sid entry identifies the stream in which to store the property. It may be any stream identifier listed on the SEQUENCE statement of the setup section, oan element of array IS in the form Isn. For example: CALL SRXSTR(STEMP, R(14), SR4) stores the value of eleme nn CALL SRVSTR(type, array, sid, i, j) A call to SRVSTR stores a range of values representing component stream properties from a Calcus

ynamic state.

tyAvailable options are listed in in the following table. Stype= Description

SS

CMR CWR

SCLVR SCGVR

weight rate of component in stream component standard of liquid volume rate component standard gas volume rate

molar rate of component in stream

array The initial element of a real Calculator array c

roperties of components in a stream. ontaining values to store as

j These two entries are component id numbers. They indicate the

p sid The sid entry identifies the stream in which to store the property. It may be any stream identifier listed on the SEQUENCE statement of the setup section, or an element of array IS in the form ISn. i,


first and last components, respectively, for which the property is stored. For example, the statement

tores elements V(12) - V(15) as the weight flowrates of components 2 through 5

e.

s to label m unconditionally. “GO TO” written as two words is also supported.

nd of a DO op. It performs no calculations.

ay not be one of the following:

NDIF

100 CALL SRVSTR( SCWR, V(12), FD1, 2, 5 ) sin stream FD1. Stream FD1 is reflashed using the new composition with the previous temperature and pressur Calculational Flow Control Statements nn GOTO mm This is the standard FORTRAN statement that branchem nn CONTINUE This statement serves as a branch destination or the elo IF Statements nn IF (expression) conditional clause.This statement allows logical branching during calculations and conforms to standard FORTRAN rules for “IF” statements. If the parenthetic expression is true, it executes the conditional lause. The conditional clause mc

EAL R

INTEGER DIMENSION IF ELSEIF ELSE EDO RETURN


The following table lists logical operators allowed in the expression.

Logical Operators in IF Statements Operator Description

.EQ. .NE.

ND. R.

equal to not equal to

both true either true equivalent not equivalent

.LT.

.GT.

.GE.

.LE.

less than greater than greater than or equal to less than or equal to

.A

.O

.EQV. EQV. .N

.NOT.

true/false toggle

nn IF (expression) THEN ELSEIF (expression) THEN ELSE ENDIF

hese statements conform to standard FORTRAN IF-THEN-ELSE statementT s, tructured b ELSE IF” and “END

also accepted. Block “IF” constructs may be nested.

iname= i, j ment defines the beginni ex ent label mm. “i j” are initial

l indices, respe he increment step “k”is option

id1, the begin ream p having a range m

iable id ring on the E statement. No incremental step index (comparabl

Statement

N(FILE=fileide, ACCESS=OVERWRITE orAPPEND) EN statement opens a file for CALCULATOR output. F

, the de is fileid.CAL, where fit file name. A uniqu n

necessary. It must, how ion. Underscore characters allowed (e.g., F oma

previously opened file.

allowing for swords are

ranching of code. “ IF” written as two

DO Loops nn DO mm , k - This state ng of a DO loop having a range tending through statem ” and “and fina ctively. T al and defaults to 1. nn DO mm ISn= s sid2 - This statement defines ning of a stDO loo extending through statement label m . ISn is a stream var , and sid1 and sid2 must be stream s appeaSEQUENC e to k) is allowed. OPEN nn OPEThe OP or PC, VAX, and UNIX platforms fault output name leid is the current inpu e filename of up to 12 characters, ca

ever, have a “.CAL” extensbe specified, if

are not ILE_01). Any OPEN statement aut tically closes the


WRITE and

FORsMAT Statemen

ormat) e pression, ... te

hese statements allow output using full FORTRAN format control. Output will be the file most recently opened with the OPEN statement. The WRITE statement

variables, expressions, or array names. Specifying an ments of the array to be written.

at.

Iw.d Output integer data

X Tab control P Scale factor S, SS, SP Control of sign output /, : Line control

n(...) Grouping OUTPUT Statement nn OUTPUT {R(i :j ),P(i :j ),C(i :j ),V(i :j ),IX(i :j ),IS (i :j )} This is a special OUTPUT statement provided with PRO/II. It outputs calculator-supplied arrays or portions of these arrays to the currently open file. Entries “i” and “j” refer to the first and last elements of the array to be output. If they are absent, the entire array will be output. DISPLAY Statement nn DISPLAY {R( i :j ),P( i :j ),C( i :j ),V( i :j ),IX(i :j ),IS(i :j )} The DISPLAY statement prints out calculator-supplied array values to the standard report file during calculations. Entries “i” and “j” are defined in the same way as the OUTPUT statement. TRACE Statement nn TRACE option TRACE statements control printing an historical trace as calculations proceed to facilitate debugging the code in the procedure. Options are: ON Prints line number, statement number, and (action taken/new variable value) as each statement executes. BRANCH Prints TRACE information only for branching statements such as IF, GOTO or DO.

ts

nn WRITE (*, f xpression, exnn FORMAT (item, i m, ...) Ttolist may include constants,rray name causes all elea

The WRITE statement refers to a FORMAT statement defining the output formThe following standard FORTRAN format items are supported. Format Items Function nnFw.d, nEw.dEe, nDw.d, nGw.dEe Output real data ‘xxxxx’, nHxxxxx Output character constants Tn, TLn, TRn, nk


OFF Turns off all TRACE options.

xamples: T E BRANCH Traces branching only.

RACE OFF No trace at all. TRACE ON Traces every statement.

alculation Termination Statements

last statement in the rocedure section. Only one RETURN statement is allowed. The solution flag for

nation of Flash Point

imate the flash point from D86 distillation sample shows how to calculate the flash points of

oints are in °F. The final results in °C are stored in R(1) through

r main data entry window by double-clicking the Calculator icon on the PFD.

Enter a number in the Parameter Number data entry field to enable the Calculator Parameter linked text. Click on the linked text to open the Definitions window.

Check the Set Up Definition for Calculator Parameter P(1) box to enable the “Calculator Parameter = Parameter” linked text.

E

RACT

C nn STOP - This statement stops all flowsheet calculations and proceeds directlyto the output report. The solution flag for the entire flowsheet is set according to the user-defined value of ISOLVE. nn RETURN The RETURN statement signals the end of the calculation procedure of the Calculator and must appear as thepthe Calculator is set according to the user-defined value of ISOLVE. RETURN always sets TRACE to OFF. Sample Calculator Procedures Example 1: Determi Use Nelson’s method to estharacterization data. This c

streams V1, V2, V3, V4, V5, and V6 using the formula: P= 0.64 * (D86(10)+D86(ip))/2.0 - 100.0 where the D86 p

(6). R Before entering the procedure FORTRAN code, it is necessary to specify the streams (V1 through V6) and establish the two pertinent parameters (the D86 0% and IBP temperatures) for each stream: 1

Open the Calculato

Click Edit/View Declarations to display the View Area box. Click Parameters to display the Parameters data entry table.


Click the Parameter… hypertext to open the Parameter window where you can specify whether the parameter will be a constant,a stream parameter or a unit parameter. The Constant/Stream/Unit list box displays a list with the options “Constant,” “Stream” and the various types of unit operations that have been placed on the flowsheet.

For this sample problem, select the Stream option and choose V1 from the tream Name: drop-down list box. Choosing a stream name enables

pertext. t to open the Parameter Selection data entry window.

86(10%) and D86(Initial Point) for the remaining

ARAMETERS TO LOCAL ARRAYS, F 32.

P = (D86AVG * .64 - 100.

2: Material Balancing with the Calculator

strates the use of the Calculator to compute the material drogen (component 2) about a recycle loop. We will set the solution

flag to indicate “unit not solved” if the hydrogen balance is not met to within 0.01% based on the overall feeds. This specification forces the recycle to

Sthe Parameter… hy

Click the linked tex For this sample, choose Distillation Curve from the options in the

Parameter window. The center window will now display the available distillation curve options. Select D86 from the distillation curve options and choose the desired cut point (here, 10%) from the Volume Percent Distillate drop-down list box.

This completes the parameter specification for the D86(10%) point of the first stream, V1. Repeat these steps to define the D86(Initial Point) for the first tream, V1, then define the Ds

five streams.

Enter the following code into the Procedure window (at this point, this window should still be outlined in red).

DIMENSION D8610(6), D86IP(6) DO10 I =1,6 $ $ COPY P$ CONVERTING TO DEG

8610(I) = P(2*I-1) * 1.8 +DD86IP(I) = P(2*I-1) * 1.8 + 32. $ $ EVALUATE FORMULA D86AVG = (D8610(I) + D86IP(I)) / 2. F$ $ CONVERT BACK TO DEG C AND STORE R(I) = (FP - 32.) / 1.8

CONTINUE 10RETURN

Commit the code by clicking OK.

xampleE This sample demon

alance of hyb


continue iterating, even if the flowing streams have changed less than the flowsheet stream tolerance. See the ISOLVE and ISn entries in the Predefined Variables table on page 152 for a listing of solution flags and for an explanation of the use of the Isn variable in SEQUENCE statements. Before entering the procedure code, we must:

Establish the Stream Sequence for the recycle loop. Provide a label for the Result.

Open the Calculator main data entry window by double-clicking the icon.

Click Stream Sequence to display two windows, one containing a list of

L in the given

the after the

hted in the Selected Streams

ab

Results to display the Result Number and Print Name data entry table.

he Result Number field of the first row to enable the Print Name entry field. This integer is stored in the first position of the R()

IN FEED STREAMS

Establishing the Stream Sequence: The streams pertinent to this example are a hydrogen feed stream (H2FD), two feed streams (FD1, FD2), a purge gas stream (PURG), and vapor and liquid product streams (PRDV, PRDL). To set up the stream sequence that will be used by the Calculator, carry out the following steps:

Calculator

Available Streams and the other a list of Selected Streams. Add the streams H2FD, FD1, FD2, PURG, PRDV and PRD

order. If you add the streams in the wrong order, you can easily change their sequence by removing the improperly positioned stream from Selected Streams window and reinserting it before or appropriate stream that you have highligwindow.

L

eling the Result:

When you have established the desired stream sequence, click

Enter “1” in t

array. For this sample problem, call the result “Relative MB.” Enter the following code into the Procedure window, which should still be

outlined in red at this point: $ SUM UP H2$ HYDROGEN IS THE SECOND COMPONENT IN THE COMPONENT LIST $ SCMR(2, n) IS THE MOLAR FLOWRATE IN THE nth STREAM $


H2FEED = 0.0

NDIF

(ABS(R(1)).LE.0.001) THEN

DO 10 IS1 = H2FD, FD2 H2FEED = H2FEED + SCMR(2,IS1) 0 CONTINUE 1

$ $ CHECK IF ANY H2 IN FEED. IF NOT, SET “NOT SOLVED” FLAG. $ IF (H2FEED .LT. 0.0001) THEN R(1) = 0 ISOLVE = 2 GO TO 99E$ $ SUM UP H2 IN PRODUCTS $

2PROD= 0.0 HDO 20 IS1 = PURG, PRDL H2PROD = H2PROD + SCMR(2, IS1) 20 CONTINUE $ CALCULATE IMBALANCE $R(1) = (H2FEED - H2PROD) / H2FEED $ $ CHECK IF IN BALANCE. IF SO, RETURN. $ IF NOT, SET “NOT SOLVED” FLAG. $ IFISOLVE =1

LSE EISOLVE =2 ENDIF $ 99 RETURN


CAPE-OPEN

eneral Information G The PRO/II CAPE-OPEN unit operation enables the users to add third party

ftware. deling software

omponents developed specifically for the design and operation of chemical dards allow integration of different software components

e unit operations and thermodynamic property packages from different vendors

nit Operation has access to the following:

hysical property calculations provided by PRO/II • Third party CAPE-OPEN property package.

SI units.

APE-OPEN interface descriptions and information are available at

the all d

and

CAPE-OPEN units. This will help the user to simulate and perform any type of calculation for a specific unit operation placed in a flowsheet. CO-LaN (the CAPE-OPEN Laboratories Network) is a neutral industry and an academic association promoting open standards in process simulation soCAPE-OPEN has uniform standards for interfacing process mocprocesses. These stanlikinto a single simulation. PRO/II supports both versions of 0.9.3 and 1.0 of the CAPE-OPEN interfaces. The CAPE-OPEN U

• Flash and P

Property values exchanged between PRO/II and CAPE-OPEN unit operation arein Chttp://www.colan.org/ Note: If transport properties are required in the CAPE-OPEN unit operation, you must select a suitable method in the Thermodynamic Data if PRO/II thermodynamics is selected. Installing CAPE-OPEN Unit Operations To install a new CAPE-OPEN unit operation or property package, executeinstall program provided by the vendor. The install program should perform actions necessary to copy the files to your computer and set up the requireentries in the Windows Registry. After installation, you can launch PRO/II immediately use the new CAPE-OPEN software components.


If the CAPE-OPEN unit operation does not have an installation program, follow the steps mentioned below to manually register the unit operation . 1. Identify the DLL file of the CAPE-OPEN unit operation.

LL of -OPEN Unit Operation.

of the CAPE-OPEN unit operation. The "progid" is a short xt string, such as "SimSci.Mixer" that Windows uses to identify the DLL.

PEN Unit Operation

PEN unit operation, as described above, and launch PRO/II to N software components. When the new CAPE-OPEN

op-lect

nit Operation may have multiple feed streams and use the data for various flash

isplay Unit Operation on PFD

o place a CAPE-OPEN unit operation, double-click the icon on the PFD. If the

ts.

2.Type "regsvr32 myunitop.dll", where "myunitop.dll" is the name of the Dthe CAPE 3.Identify the "progid"teContact the developer of the unit operation to determine the "progid". 4.From the command prompt, type "CapeRegister.exe progid". "CapeRegister.exe" is an utility available in the PRO/II "bin" directory. Selecting the CAPE-O Install the CAPE-Ose the new CAPE-OPEu

unit operation is laid down on the PFD, a dialog will be displayed with a drdown list box filled with registered CAPE-OPEN unit operations. User must seprogramid of the required unit. Feeds and Products Uand property calculations. PRO/II queries the unit operation for a required number of unit ports. The icon is automatically supplied with the required numberof ports with one stream allowed for each port. Note: Material type ports are handled while the energy and information type ports are not supported. D Tunit operation supports a custom GUI, the built-in GUI for the unit operation is displayed. If the unit operation does not support a custom GUI , PRO/II displays all parameters in the default data entry window. All values are displayed in SI uni


Saving the state of CAPE-OPEN Unit Operations

RO/II saves the state PEN unit operation by querying all input and output parameters ir values in the underlying PRO/II database.

delegated to

ay call PVf flashes(CalcEquilibrium) for input or output streams. The

PRO/II supports COM Persistence mechanisms through IStream, IStreamInit, IStorage and IPropertyBag interfaces. PRO/II creates a file named przname-uid.dat for storing state. CAPE-OPEN Unit does not support COM persistence, PIf

of the CAPE-Ond storing thea

Calculation During calculations, PRO/II calls the Validate() and Calculate() method of the

APE-OPEN unit operation. Property and flash calculations areCproperty package if property package is selected as unit thermodynamics. If PRO/II thermodynamics is selected for a CAPE-OPEN unit operation, it mTP,TH,PH,TVf andfollowing properties can be calculated using PRO/II thermodynamics. CAPE-OPEN identifier

Property meaning Phases Supported

vaporPressure Vapor Pressure only for Pure calc type Liquid surfaceTension Surface Tension Liquid compressibilityFactor Compressibility Factor Z= PV/RT Liquid, Vapor, Overall heatCapacity Heat Capacity Liquid, Vapor, Overall idealGasHeatCapacity Heat Capacity of ideal gas Vapor viscosity Viscosity Liquid, Vapor, Overall thermalConductivity Thermal Conductivity Liquid, Vapor, Overall fugacity Fugacity Liquid, Vapor logFugacityCoefficient Logarithm of Fugacity Coefficients Liquid,Vapor kvalues K factors of a pair of phases in Equilibrium Overall dewPointPressure Dew point Pressure at a given temperature Overall dewPointTemperature Dew point Temperature at a given Pressure Overall temperature Temperature Liquid, Vapor, Overall pressure Pressure Liquid, Vapor, Overall volume Volume Liquid, Vapor, Overall density Density Liquid, Vapor, Overall enthalpy Enthalpy Liquid, Vapor, Overall entropy Entropy Liquid, Vapor, Overall gibbsFreeEnergy Gibbs Free Energy Liquid, Vapor, Overall flow List of partial Molar(or mass) flows for each

component within a given phase Liquid, Vapor, Overall

fraction List of partial Molar(or mass) fractions for each component within a given phase

Liquid, Vapor, Overall


phaseFraction The fraction of the fluid that is in specified Liquid, Vapor phase

totalFlow Mass flow of a phase or whole mixture Liquid, Vapor, Overall molecularWeight MolecularWeight Liquid, Vapor, Overall boilingPointTemperature Only supported for “Pure” calc type

Report Generation

display a menu with “Produce

with PEN units.

If the custom reports is supported by CAPE-OPEN unit operation, select and right-click the unit operation. This action will Report” as one of the options. Select Produce Report to open a text file. If the custom reports are not supported, the menu will have “View Results” as one of the options. Select View Results to display all input and output parameters with their values. Note:The standard report of PRO/II will have all input and output parameterstheir values for CAPE-O


Column, Batch

General Information

rating atch Column unit may be run in a true batch simulation mode,

ck

ccumulator over some time interval. Batch distillation calculations may also be a steady-state process simulation.

he

ded

ystem

it hole or for selected trays. also allows the use of electrolyte

ds.

n model obtained from Koch-Glitsch. BATCHFRAC has een int II to handle reaction on trays for VLE, VLLE on all the

stag trays apart from Batch distillation.

etailed Information

n RAC® and Batch Column unit

The Batch Column unit operation models a wide range of column opescenarios. The Bwith the feedstock charged to the stillpot prior to distillation and products taken from the accumulator at various times, or in a semi-batch mode where feedstomay be introduced during distillation and products drawn from the column or aintegrated into The unit configuration automatically considers the presence of implicit holding tanks for continuous flow streams which provide the time-variant feedstock to tbatch unit. Implicit consideration of holding tanks for all product streams (as drawn from the accumulator at different times, or as drawn from the column during distillation) is also made because of the cyclic operation. A representation of the product continuous flow stream comes from the amount of product diviby the batch cycle time. Thermodynamic S The thermodynamic system for the Batch Column may be specified for the un

s a w Batch Column athermodynamic metho BATCHFRAC® This is a batch distillatio ®

b egrated with PRO/es and heat duty specification for

D For detailed i formation about the use of BATCHFoperations, consult the PRO/II Add-On Modules User’s Guide.


Column, Distillation

General Information

to simulate any distillation or liquid-liquid

to

next lower tray. There is no limit on the number

ay

ther a

struction in the

he Column unit operation may be usedT

extraction process. Liquid-liquid extraction units are described in the Liquid-Liquid Extraction Column section of this chapter. A column must contain at least one equilibrium stage or theoretical tray. For purposes of this discussion, the term “trays” is used to denote “equilibrium stages”. The trays are consideredbe linked with the vapor from each tray entering the next higher tray and the liquid from each tray feeding theof trays in a column model. The condenser, when present, is always numbered as tray one and the reboiler,when present, is assigned the highest tray number in the model. Any tray mhave a feed, product draw, or duty. The top and bottom trays must have eifeed or a duty. Dv

istillation columns may simulate vapor/liquid, vapor/liquid/water or apor/liquid/liquid equilibrium processes.

eeds and Products F

olumn feeds and products are added during the flowsheet conC

PFD main window. Click Column Feeds and roducts… on the Column main data entry window to open the Column Feeds and Products window.

eed tray numbers may be added or changed in this window. There is no limit on Fthe number of feeds a column may have. The feed flash convention to use for all feeds to the distillation column is selected with radio buttons as:

apor and liquid to be on the feed tray: The default. V Flash the feed adiabatically, vapor onto the tray above and liquid onto the feed tray. For this option, the vapor is placed on the feed tra

e column. y when it is the bottom tray of

th


For products, the product type, phase, tray number, and flowrate are supplied in is window. There is no limit on the number of products a distillation column may

may be withdrawn from any tray of the column. Product types clude: Overhead, Bottoms, Fixed Rate Draw, Total Phase Draw, and

-Out

he Sure algorithm may also have water draws from any tray. For y

ou must supply product rates for all fixed rate draw products in molar, mass, or

lways alue for the overhead or bottoms

te should be as accurate as possible to enhance convergence. You must use a

Define seudoproducts in the Column Pseudoproducts window which you may reach by

n

algorithm is the preferred option for most distillation roblems, especially those involving systems of hydrocarbons, because of its

speed and insensitivity to the estimated solution profiles.

thhave and productsinPseudoproduct. Every column must have an overhead product leaving tray one and a bottoms product leaving the highest numbered tray. The Sure, Inside(IO) and Enhanced IO algorithms may have a decanted water product from trayone (the condenser). Tvapor/liquid/liquid equilibrium (VLLE) processes, either of the liquid phases mabe drawn from any tray in the column. Yliquid volume units. You must also provide an estimated value for either the overhead or bottoms product. For total draw products, the supplied rate is aassumed to be an estimate. The estimated vraPerformance Specification to set a desired flow for the overhead or bottoms product. Pseudoproducts Pseudoproducts are used to create streams corresponding to column internal streams, making them available for flowsheet calculations.pclicking Pseudoproducts on the Column Feeds and Products window. The following types of pseudoproducts are available:

Net tray liquid or vapor flow Total tray liquid or vapor flow Pumparound liquid or vapor bypass flow Thermosiphon reboiler feeds and products

Thermosiphon reboiler streams are limited to the Inside-Out algorithm. Column Algorithm Select the solution algorithm from the drop-down list box, on the Column maidata entry window. The available algorithms are: Inside-Out (the default), Sure, Chemdist, Liquid-Liquid, Enhanced IO, and Electrolytic. Detailed informationabout the column algorithms is available in the online help. Inside-Out: The Inside-Outp


Sure: The Sure algorithm should be used for columns where free water exists on multiple trays. Chemdist: The Chemdist algorithm is well suited to highly nonideal systems anVLLE processes.

d

iquid-Liquid: The Liquid-Liquid algorithm is used to model liquid-liquid

Enhanc I IO column algorithm extends the capabilities of the default Insid anced IO allows zero flowrates, water decant off any tray t nd pumparounds. Electro ic method is used to model non-ideal aqueous electroly d s involving ionic species. Refer to the PRO/II Add-

n Modules User’s Guide for detailed information on this column algorithm.

tion (RATEFRAC® ) routines ss transfer on the stage, avoiding the need for

equilibrium stage model used in RATEFRAC® e.

wn list of the Column indow. Enter pertinent data in the Column – Reaction Selection window

Lextraction units described in the Liquid-Liquid Extraction Column section of this chapter.

ed O: The Enhanced e-Out algorithm. Enh

, to al draws from trays a

lyt : The Electrolytic tic istillation column

O RATEFRAC® Software: Rate-based distillarigorously calculates the actual macomponent efficiencies. The nonroutines uses fundamental heat and mass transfer to model a distillation stag Reactions Reactions in the column can be modeled by the Chemdist or Liquid-Liquid extraction algorithms found in the Algorithm drop-dowaccessible via the Reactions… button on the Column window. In the Column - Reaction Selection window, you can select and modify column reactions, specify

age-wise reacting volumes, designate non-condensible components, select r user-added subroutines or kinetic

roce-dures. The reactions specified here are limited in scope to the simulation

Column - Reaction Selection To d ts defined in Reaction Data, select the Include Reactions in

olumn Calculations check-box. All the reactions defined via Input/Reaction Data re now available to the column. Reactions can be selected from a drop-down list nder Reaction Set from Reaction Data, and a local set-name and description an be assigned. Moreover, the individual reactions can be modified in the eaction Definitions window by clicking Modify Data. ATEFRAC®

is a Registered trademark of Koch-Glitsch

stnon-volatile catalysts and specify data fopof reactive distillation and (reactive) liquid-liquid extraction.

mo ify reaction seCaucRR


The selected reaction sets can also be assigned to individual trays (or ranges of

yst for Boiling Pot window accessible from the Column - Reaction

s and kinetic procedures can be specified in

finitions window

trays) by selecting reaction sets from a drop-down list under Column Reaction Set and then entering a tray range, i.e., starting tray to ending tray. Note: Although you can modify a local copy of a reaction set in the column, the original reaction set specified in the ‘Reaction Data’ section remains unchanged. Reacting Volumes The user can specify volume available for reaction (effective volume) per stage for both liquid and vapor phase reactions in the Column –Tray Effective Reaction Volumes window accessible from the Reaction Selection window. A tabulation of tray numbers and the respective volumes is provided for data entry. This specification is used in calculating the rate of kinetic reaction. Nonvolatile Catalyst Components that catalyse a reaction without volatilizing can be selected and thequantity of their charge specified as an amount or a fraction in the Column - Non-

olatile CatalVSelection window. Noncondensibles Noncondensing components can be specified in the Column - Non-CondensingComponents window accessible from the Column –Reaction Selection window.

ubroutine/Procedure Data S Data used for user-added subroutinethe form of Integer, Real and Supplemental Data entries in the Column - User Subroutine and Procedure Data window accessible from the Column - Reaction Selection window via the Subroutine/Procedure Data button. See the Reaction Data and Procedure Data sections, in this chapter, for detailed information on the data requirements for these utility modules. Modify Data (Reaction Data) All data pertaining to a reaction (in a specified reaction set) can be modified xcept for reaction stoichiometry - in the Column-Reaction Dee

accessible via Modify Data… in the Column-Reaction Selection window. The calculation method for a reaction can be modified to follow a user-added subroutine, procedure or kinetic power-law expression. The reaction type can also be changed to Kinetic, Equilibrium or Conversion. All reaction data that


completely specify any of the above reaction types (except stoichiometry) can be changed in the data entry fields accessible via the Enter Data… button under the Additional Data column for the respective reaction. Instructions for entering data for the three types of reactions (Kinetic, Equilibrium

nd Conversion) are covered in detail, in the Reaction Data section of this

d Enhanced IO algorithms

n the Column

t r algorithms. A nonconvergence is flagged when this number of iterations

Profile

ll calculations s in the

achapter. Calculated Phases Select the appropriate phase system in the drop-down list box on the Column main data entry window. All distillation algorithms support the default phase system of vapor/liquid. The Sure and Chemdist algorithms also support theapor/liquid/liquid system. In addition, the Sure anv

support the phase system vapor/liquid/water that allows a free water phase on any tray of a column. Number of Trays Enter the number of trays in the model, in the data entry field provided on the Column main data entry window. Every Column must have at least two trays. There is no limit on the number of trays in a Column. Number of Iterations

upply the number of iterations in the data entry field provided oSmain data entry window. The number of iterations corresponds to the number of outer loop trials for the Inside-Out algorithm and the number of trial solutions for

e o hethis performed and the column equations are not satisfied within the tolerances. The default values are 15 for the Inside-Out algorithm, 10 for the Sure algorithm and 20 for the Chemdist algorithm.

ressureP The pressure for every tray in a column model must be defined. Are performed at the defined tray pressures. Define the tray pressurea

Column Pressure Profile window which you may reach by clicking Pressure Profile… on the Column main data entry window. Tray pressures may be upplied on an overall or tray-by-tray mode by choosing a radio button in this indow.

(tray two for columns with condensers) and either the pressure drop per tray or the total pressure drop aross the column. A default value of zero is supplied for the pressure drop per

sw For the overall mode, supply the top tray pressure


tray and the column pressure drop. All tray pressures are derived by linear pplication of the supplied pressure drop.

p

plied s method is useful for defining the pressure profile for columns with

regular pressure profiles such as refinery vacuum units.

he condenser is always a heat sink on tray one. It is defined in the Column

a Individual tray pressures are supplied for the tray by tray mode. Note that the toand bottom trays must be included when supplying a table of individual tray pressures. Missing pressures are determined by linear interpolation of supvalues. Thiir Condensers TCondenser window, which you may access by clicking Condenser… on the Column main data entry window. The top products from columns with condensers correspond to the products from the reflux accumulator drum. The

ressure for all types of condensers is supplied in this window.

net

is r

nser

e portion is returned as reflux to tray two, the other portion is ithdrawn as the “Overhead” product from the column. An optional estimate for

ure may be supplied in the Column Condenser window. he condenser pressure and duty may also be supplied.

erature provided in this window. RO/II ascertains that the product is subcooled, and if, not, signals a

non propriate diagnostic message. The sub m the column. The con

ubcooled, Fixed Temperature Drop: This condenser is the same as the ubcooled type described above except that the degrees of subcooling below the roduct bubble point is defined, always resulting in a subcooled “Overhead” roduct. The duty and pressure for the condenser may also be supplied in this

arameter to vary, any supplied s an estimate.

p The condenser type is selected with the appropriate radio button from the following options: Partial: This condenser is an equilibrium stage and may or may not have aliquid product as well as vapor product. The net liquid product, if present, is defined as a “Fixed rate liquid draw” from tray one. The condenser temperature the dew point of the equilibrium vapor. An optional estimate for the condensetemperature may be supplied in the Column Condenser window. The condepressure and duty may also be supplied. Bubble Temperature: The tray two vapor is cooled to a bubble point liquid phase. While onwthe condenser temperatT Subcooled, Fixed Temperature: The tray two vapor is cooled below its bubble point as defined by a subcooled tempP

convergence condition with an apcooled liquid product is designated the “Overhead” product fro

denser pressure and duty may also be supplied. Ssppwindow, if desired. If the duty is designated as a pduty for any of these condenser options is used a


Subcooled Reflux Only: This option will be enabled only if you have selected

t

e

ilibrium liquid withdrawn as the ottoms” product.

r.

sponds to the case when the Column wn from a common sump.

the obaffles”

on

rculation rate. An estimate for the return fluid liquid fraction or circulation rate, as is applicable,

ay e nce convergence. The duty for the reboiler may also be sired. If the duty is designated as a

ty is used as an estimate.

Partial or Bubble Temperature under Condenser Type. Select the appropriate Temperature specification namely, Fixed Temperature or Temperature Drop thaneeds to be followed in the Subcooled reflux for the chosen condenser type. Column Reboilers Column reboilers are described in the Column Reboiler window which is entered via the Reboiler button on the Column main data entry window. The reboiler typis selected with a radio button on this form. The default type is the Kettle (Conventional) reboiler, which corresponds to a duty on the bottom tray of the column with the equ“B For both Inside-Out and Enhanced IO algorithm, following reboiler types areavailable to the user.

• Thermosiphon without Baffles, and • Thermosiphon with Baffles.

For other algorithms, only default type is made available to the use The thermosiphon without baffles type correottom product and reboiler feed are withdrab

Note: Thermosiphon reboilers with baffles in which the reboiler return flows into

reb iler sump and overflows to the product sump are equivalent to the “no type for simulation purposes and should be modeled as such.

One specification may be selected for thermosiphon reboilers by choosing the appropriate radio button and entering a value in the field provided. Choices include:

• Reboiler return liquid fracti• Return temperature • Temperature change across the reboiler • Reboiler ci

ms

b given to enhaupplied in this data entry window, if de

parameter to vary, any supplied du


Heaters and Coolers Side heaters and coolers may be supplied via the Column Side Heaters/Coolers window accessible via the Heaters and Coolers… button on the Column main data entry window. Side heaters and coolers that are associated with a

umparound are not entered with this window. A negative duty indicates cooling;

oolers.

ling for both phases iquid/Vapor).

must be provided: tray number appropriate algebraic sign.

lash Zones

n. Flash zones are associated with column heaters when a feed stream

ntering the column is heated in a separate furnace. The furnace is considered

below the flash zone could enter the flash zone or they can bypass it. Data entry fields for flash zones can be accessed through the like-nam n the Heater data entry window. Specification options include fired e , vapor and liquid by-pass fractions and transfer line

mperature drop.

are working with RATEFRAC® routines, this option is disabled.

Side k

oiler and n ak may

pa positive duty is used for heating. There are no limits on the number of side heaters/c RATEFRAC® routines supports heating and coo(L For each side heater/cooler, the following information

, a reference name, and the duty, with the

F The Flash Zone calculation models a fired heater added to a tray in an Inside-Outcolumeas an additional theoretical stage. Liquid from the tray above the flash zone or vapor from the tray

ed button o h ater efficiency

te Note: If you Column Heat Leaks Column heat leaks may be modeled by clicking Heat Leak on the ColumnHeaters/Coolers window to open the Column Heat Leak window. The heat lea

ay be designated as: m

• Overall, or, • By Individual Trays

® RATEFRAC is a Registered trademark of Koch-Glitsch. For the Overall option, the heat leak duty for all of the trays except the reb

eat le co denser is given on a per tray basis or total column basis. A hed for the condenser and the rebo er, if desired. also be provid il


For the , heat leak duties for ranges of trays are sup or trays no lie between trays with defined heat leaks, are etermined by linear interpolation.

is disabled. Pum a Column ut and Sur Column Pumparounds window, which is accessed via

By Individual Trays optionplied as tabular input. At least two values must be supplied. Heat leaks f

t given, but which d Note: If you are working with RATEFRAC® routines, this option

p rounds and Vapor Bypasses

pumparounds and vapor bypasses may be defined for the Inside-Oe algorithms in the

the mpumpar r a liquid or vapor, with vapor pumparounds more ommonly termed “bypasses”.

tries for each pumparound include: phase, pumparound name, draw ay, return tray, return pressure, and two specifications. Supply these pecifications in the Column Pumparound Specifications window which is

the two specifications hypertext string.

nabled for ay be the temperature or the temperature drop or

uty on: The duty and return condition fields are enabled for inpu T dition may be the temperature or the temperature drop or the ference name may also be supplied for the heater.

or the Sure algorithm only, the pumparound rate may be designated as n the

olumn and total vapor pumparounds (bypasses) must flow up.

Pu parounds… button on the Column main data entry window. A ound may be eithe

c Pumparounds are added and edited in a tabular form by clicking on hypertext strings. Entrsentered by clicking The following specification combinations are selectable via radio buttons: Rate and Duty: The rate and duty data entry fields are enabled for input. A reference name may also be supplied for the heater. Rate without Heater: The rate field only is enabled for input. Rate and Return Condition: The rate and return condition fields are e

put. The return condition minthe liquid fraction. A reference name may also be supplied for the heater. D and Return Conditi

t. he return conliquid fraction. A re

Fthe total fluid leaving the tray. Total liquid pumparounds must pump dowc RATEFRAC®

is a Registered trademark of Koch-Glitsch.


Initial Estimates All column algorithms use an iterative solution technique, starting from an initial estimate of the tray temperature, flow and composition profiles. The initial estimate may be produced internally using an initial estimate generator and/or rovided by the user as initial profile data. User-supplied profiles may also be

ly replace values produced by an estimate generator.

al balance. Temperatures are

mpositions. The compositions are used to estimate temperatures.

e.

umparound cooling circuits, and decanted water at the overhead accumulator. A s used for these

olumns. The user-supplied estimates for the product rates are used in the Adjustments in the profiles are made for side coolers.

e following trays: condenser, top tray, bottom tray of column, and er. You may also provide an estimate for the reflux rate or reflux ratio.

When no reflux estimate is provided by the user, PRO/II supplies a reflux ratio of 3.0 (which solves many columns). Any supplied data replaces values predicted by the estimate generator.

pused to selective Click Initial Estimates on the Column main data entry window to enter the Column Initial Estimates window. To use an initial estimate generator, select the generator method from the drop-down list box. Methods provided are:

imple: Profiles are determined by a simple materiSdetermined from estimated product compositions. This model is quick and adequate for simple column configurations. Conventional: A general method designed to produce an adequate estimate for most distillation problems. Shortcut calculations are used to estimate the productows and cofl

Internal flows are estimated by using the product flows and a reflux estimatThis method works best for conventional fractionators with condensers and reboilers in which classic Fenske techniques provide reasonable results. Special techniques are also included for absorbers and strippers. Refinery: This method is designed for complex refinery columns which have bottom steam instead of reboilers such as crude and vacuum columns, F.C.C. main fractionators, etc. These columns may also have side columns, pmulti-product shortcut technique developed by SIMSCI icshortcut model. Chemical: This generator should be restricted to highly nonideal chemical distillation problems. The method is time-consuming and uses successive series of adiabatic flashes up and down the column to establish the tray compositions. When using an estimate generator, you may optionally provide temperature stimates for the

reboil


When an initial estimate generator is not used, the minimum data which musupplied as input profiles are tray temperatures and flows, either vapor, liquida combination thereof. Note that the minimum data which may be supplied are the temthese a

st be , or

peratures and flows for the top and bottom trays for the column. While re the minimum data required, they are rarely adequate to produce an

cceptable initial estimate. It may also be desirable to provide solution profiles speed future calculations with a column model.

afrom a converged solution to Initial profiles are entered in tables accessed by clicking the following buttons on the Column Initial Estimates window:

• Net Vapor Rates… • Vapor Composition… • Liquid Composition… • Tray Temperatures… • Net Liquid Rate… • Mass Transfer…

Composition estimates may be helpful for highly non-ideal mixtures; however, they are rarely needed for most problems. RATEFRAC Initial Estimate:

or RATEFRAC® routines, Initial Estimate may be used to perform Initial

®

stimate. Option is also provided to include design specifications.

y default, the Perform Initial Estimate option is checked to provide the user to ave an estimate on Temperature and Reflux, etc.

heck Include Design Specs in Estimate to include design specifications to be onsidered during Initial Estimate.

olerance: Enter the Tolerance value.

iquid/Vapor Flow Transformation: Select the appropriate Liquid/Vapor Flow ransformation from the drop list.

• Standard • Square • Logarithmic

RATEFRAC® is a Registered trademark of Koch-Glitsch.

FE Bh Cc T LT


Performance Specifications Performance specificationsuch that product stream fl

or SPECs may be imposed on a column operation ows or properties, column internal flows, column tray

, s

ne VARYs for a column, click e or

ual

fully

Con r Conver Convergence Parameters, Convergence Tolerances,

om to rgence Specifications and Convergence History rintout options) for Column iterations. These data are entered in the Column

stemperatures, etc., are at desired values in the solution. For each SPEC, a degree of freedom or VARY must be calculated. For a column, a VARY may be a feed stream rate, heat duty, or the draw rate for a “fixed rate draw.” Furthermorefor convergence to be achieved, there must be a direct effect on all of the SPECby the collective set of VARYs.

o supply SPECs and defiTPerformanceSpecifications on the main Column data entry window to access thColumn Specifications and Variables window. SPECs and VARYs are entered edited by clicking on the hypertext strings. PRO/II requires that there be an eqnumber of SPECs and VARYs. Thus, whenever you add or delete a SPEC, you

re required to add or delete a VARY. a

PECs and VARYs use the general form in PRO/II and are discussed moreSin the SPEC/VARY/DEFINE section of this chapter. A list of the stream and column parameters which may be used for SPECs and VARYs is also given in hat section. t

ve gence Data

gence data includeo py Options for ConveH

(pConvergence Data winColumn main data entr

dow accessible via the Convergence Data… button on the y window.

nce when the convergence is oscillating. Refinery complex fractionators hould be given damping factors of 0.8. Chemdist columns may require more

rror Increase Factor: This factor limits the increase in the sum of the errors t

Sure algorithm.

Convergence tuning parameters Damping Factor: A damping factor of less than unity may be used to improve convergessevere damping. A default value of 1.0 is supplied by PRO/II. Damping cannot be applied to the Sure algorithm. Damping Cutoff: The damping factor cutoff value is used for the Chemdist algorithm. The damping factor is only applied when the sum of the errors is larger than this value. A default value of 10-8 is supplied by PRO/II. Efrom iteration to iteration. PRO/II supplies a default value of 1.0 for the Inside-Oualgorithm or 100 for the Chemdist algorithm. This factor does not apply to the


Component Averaging Factor: This weighting factor for update of compositions

used for the Sure algorithm. A factor of 1.0 gives equal weight to the current

rmally be specified by the user.

tions: The number of consecutive Sure owed without improvement in the solution. You can change

ired

on

oleranc y also be changed although this should e and never as a means to reach a converged solution.

aximum heat balance error for each tray. The default -3

p.The default is 10-3 . Not used for the RATEFRAC®

h

RATEFRAC®


isand last set of compositions; a factor of 2.0 gives double weight to the last set ofcompositions, and so forth. A default value of 0.0 is supplied by PRO/II. Key Component: In rare circumstances, specifying a key component can enhance the convergence for the Sure algorithm. The key component is nodetermined by PRO/II but may Stop if no improvement after 5 iteralgorithm iterations alla

the number of iterations by clicking on the hypertext string. Changing this parameter rarely, if ever, results in convergence. Note: The use of tuning factors usually results in an increase in the time requto solve a distillation problem. C vergence Tolerances

T es for the column equations mararely, if ever, be don

olerances are: T Bubble Point: The maximum bubble point error for each tray.The default is 10..

-3 Not used for the RATEFRAC® routines.

nthalpy Balance: The mEis 10 . Equilibrium K-value: The maximum allowable relative change in a component K-value generated in the outer loop of the Inside-Out algorithm versus the last alue used in the inner loov

routines. Component Balance: The maximum relative component balance error for eactray. Not used for the Inside-Out algorithm. The default is 10-3 .


Homotopy Options for Convergence on Specification

he homotopy option is an aid to converging simulations where the specification

ion re complex, but it may be used for any column

lgorithm.

ne example of the use of homotopy is to systematically increase tray volumes

e for t

f steps. The column is converged at each step.

e

motopy option may be used for a specification which is varied by a ontroller or Flowsheet Optimizer. If Initially is selected under the field entitled

. If Always is selected, the homotopy iterations will be carried out every me the column is reconverged after the specification has been changed. In this ase, the initial value will be the last converged specification value, not the

ting the

nce History Print Level • Print Column Profiles in Keyword Input File Form Format

C® routines Initial Estimate Print Level

rademark of Koch-Glitsch.

Tis difficult to meet by virtue of the value of the specification (as opposed to the type of specification). The homotopy option was designed for Reactive Distillatwhere convergence is moa Oto very large values, to determine the equilibrium compositions for reversible kinetic reactions. The homotopy option allows you to solve the simulation with an initial valuthe specification and then automatically move to the desired final value in a senumber o To use the homotopy option for any specification, you must supply the initial value of the specification and the number of intervals to use in moving from thinitial value to the final value. You cannot change the final value in this window. The hoCApply During Control Loop (the default), the homotopy iterations will be carried out to meet the given column specification. If the specification value is then changed by another unit operation, the column will solve without homotopy iterationsticsupplied value. Convergence History Printout of the column iterations is useful in the diagnosis of a convergence failure. History printout for the iterations may be requested by selecprintout level desired for the following options.

• Converge

• RATEFRA RATEFRAC®

is a Registered t


Tray Hydraulics

used to size new columns and to rate existing Tray hydraulic calculations may betray or packed columns. To perform sizing or rating calculations, click Tray and Packing Data… on the Column main data entry window. For sizing and rating purposes, the column is divided into sections of trays or packing on the CTray Hydraulics window. Enter tray/packing sizing and rating information in the Column Tray/Packing Rating or Column Tray/Packing Sizing windows accessibl

olumn

e via the Enter Data… button. The Glitsch valve tray method is used to perform the

ay calculations. The valve tray results are derated by five and twenty percent

ection is then selected and the entire section is rerated using the largest

. The lumns,

a variety of tray and downcomer arrangements.

Options

owing

d


trrespectively, to represent the performance of sieve and bubble cap trays. For packed columns, random or structured packings are available, as are varioustypes of metallic and ceramic rings and saddles. For sizing calculations, column diameter for each tray is sized independently to meet the specified or default flooding criteria. The largest diameter in each srequired standard diameter. For rating calculations, the percent of flood is calculated for each trayfeature of multiple sections of trays is useful in representing existing cowhich often have Column RATEFRAC® Tray Column RATEFRAC® routines tray options may be used to select the foll

• Vapor and liquid mixing characteristics • Correlation used to calculate Mass, Heat Transfer and Interfacial Area.

Base Segment: Enter the Tray number on which the characteristics need to be set. Base Segment will be made available to the user only if you have selectethe following in the Column – Tray Hydraulics dialog box:

• Internal – Tray • Calculation Type - Sizing

Liquid/Vapor Mixing: Select the appropriate Liquid/Vapor Mixing characteristicsfrom the drop list:

• Complete • Linear • Logarithmic

The options are explained below:

ATEFRAC®R


Complete – Select, if there is a complete mixing of liquid or vapor phase in the olumn. This corresponds to a flat concentration profile across a tray. It is the

s the

s

olumn ® Packing Options

elect the

urface Tension: Enter the Critical Surface Tension, if you have Packing under Internal in the Column - Tray Hydraulics dialog

tics

Logarithmic

AC Transport Calculation Methods is used to select a suitable orrelation for calculating Heat Transfer, Mass Transfer and Interfacial Area.

eat Transfer

ion and select the appropriate correlation name from the drop-own list to calculate Mass Transfer:

• Scheffe & Weiland (Internals - Trays and Sizing calculation type) • Chan & Fair (Internals - Trays and Rating calculation type)

RATEFRAC® is a Registered trademark of Koch-Glitsch.

cdefault value and for most cases provides good results. Linear – This option indicates that there is a linear concentration profile acrostray. Logarithmic – This option indicates that there is a logarithmic concentration acrosthe tray. C RATEFRAC

olumn RATEFRAC® routines Packing Options may be used to sCfollowing and enter the data required for calculation:

• Vapor and liquid mixing characteristics • Correlation used to calculate Mass, Heat Transfer and Interfacial Area

ritical SC

selected Randomox. b

Liquid/Vapor Mixing: Select the appropriate Liquid/Vapor Mixing characterisrom the drop list: f

• Complete • Linear •

User needs to enter the above-mentioned data for both Sizing and Rating alculation. c

®RATEFRAC Transport Calculation Methods

RATEFR ®

c HCheck Correlation and Select Chilton - Colburn Correlation from the drop-down list to calculate Heat Transfer. Mass Transfer Check Correlatd


• Rocha 1996 (Internals - Structured Packing and for both Sizing and Rating calculation type)

• Onda (Internals - Random Packing and for both Sizing and Rating

- Random Packing and for both Sizing and Rating calculation type)

• Bravo (Internals - Random Packing and for both Sizing and Rating calculation type)

the user-defined correlation is available for any of the parameters mentioned ove, check Subroutine and select the user-defined correlation from the drop- wn list.

ray Efficiencies All trays in a column model are treated as equilibrium stages or theoretical trays unless one of the tray efficiency models is used. This implies that the user must apply some type of tray efficiency to the actual number of trays in the column, to determine the number of theoretical trays to use in the model. Engineers typically use overall tray efficiency factors based on experience to convert actual trays to theoretical trays. This is almost always the best manner in which to model tray efficiency, since generalized correlations for overall tray efficiency are nonexistent in the literature. For the Inside-Out algorithm, PRO/II provides several tray efficiency models:

• Murphree • Equilibrium • Vaporization.

For the Chemdist algorithm, only the Vaporization model may be used. However, none of these models predicts the overall tray efficiency. All of the models use an equation or factor to adjust the equilibrium vapor composition leaving a tray. The models are useful for tuning a tray or a few trays in a Column model, but their general application to all trays in a column is not recommended.

calculation type) Interfacial Area Select any of the listed correlation to calculate Interfacial Area:

• Scheffe & Weiland (Internals - Trays and Sizing calculation type) • Chan & Fair (Internals - Trays and Rating calculation type) • Rocha 1996 (Internals - Structured Packing and for both Sizing and

Rating calculation type) • Onda (Internals

If abdo T


To use tray efficiencies, click Tray Efficiencies… on the Column main data entry window to enter the Column Tray Efficiency window.Select the efficiency model wi h a radio button and click Efficiency Data… to begin the tabular entry of tray

s may be given for all components on a tray or tray. An overall scaling factor may also be provided to

r unit

olumn. A finished Side Column.

n

the are

ithm merges a side column with the main column, for alculations. This simultaneous approach means that the SPECs and VARYs for

separate columns in recycle. This ppr ac for

the i The

tefficiencies. Tray efficiencieselected components on a be applied to all tray efficiencies. This factor may be adjusted by a Controlleto meet a desired SPEC. Side Columns A column using the Inside-Out or Sure algorithm may have attached Side Columns, where a Side Column is a stripper or rectifier. The Side Column draws

ed from the main Column and returns a product to the main Cfeproduct is withdrawn from the Side Columns are attached as part of the flowsheet construction in the PFD maiwindow. They may be completed and edited by double-clicking on the side column icon on the PFD. The side column data entry windows are identical toColumn main data entry windows with the exception that irrelevant featureseliminated. The Inside-Out algorcthe main column and side columns need not be balanced provided that the SPECs and VARYs for the total column configuration are balanced. The Sure algorithm solves side columns asa o h is more time consuming, and demands that the SPECs and VARYs

ma n column and every side column are balanced.

Ch algorithm does not permit side columns. emdist Print Options Click Print Options… on the Column main data entry window to enter the Column Print Options data entry window. Select the desired report options with the check boxes provided. To request plotted results, click Plot Column Results… and select the desired plots with the check boxes on the Column Plot Options data entry window.


RAT FOptionschecked ted report.

hermodynamic Systems

ay.

E RAC® Software Print Options: Click RateFrac… to bring up Print dialog box. By default, Calculated HETP for each segment option is . Check the other options to make the data available in the genera

T A thermodynamic system is required for the equilibrium calculations on each trThe thermodynamic system may be changed from the global default in the Column Thermodynamic Systems data entry window, which is reached by clicking Thermodynamic Systems… on the Column main data entry window. A single thermodynamic system may be defined for the complete columndifferent systems may be used in individual sections of the column. If a vapor/liquid equilibrium thermodynamic system is used for part of a column with the Chemdist or R

or

ATEFRAC algorithm, additional checks may be performed determine which trays have two liquid phases by clicking the Test for VLLE or

.

®

toVLE Trays check box. The thermodynamic system is then changed to a vapor/liquid/liquid system for those trays. If you are working with RATEFRAC® routines, Test for VLLE or VLE Trays can be performed by entering appropriate data in Column- VLLE Test Data window RATEFRAC is a Registered trademark of Koch-Glitsch.


Column, Liquid–Liquid Extraction

e Column unit operation may be used to simulate any distillation or liquid-liquid traction process. Distillation columns are described in the Distillation Column ction of this chapter. Although liquid-liquid extraction (llex) columns are nerally not trayed, the distillation column nomenclature is used and the term y denotes an equilibrium stage. A Liquid–Liquid Extraction Column must ntain at least two trays.

e trays are considered to be linked with the light-liquid phase moving up the lumn and the heavy liquid moving down. There is no limit on the number of ys in a liquid-liquid extraction column model. Any tray may have a feed, oduct draw, or duty. There must be a feed to the top and bottom trays.

ote: Side columns may not be used with liquid-liquid extraction columns.

e following distillation column features are not applicable to LLEX columns and ill be disabled:

• Condenser and reboiler • Pumparounds • Tray hydraulics • Tray efficiencies.

eds and Products

olumn feeds and products are added as part of the flowsheet construction in e PFD. They may be accessed from the Column Feeds and Products window

General Information Thexsegetraco Thcotrapr N Thw

Fe Cthacw

cessible via the Feeds and Products… icon on the Column main data entry indow.

ed tray numbers may be added or changed in this window. There is no limit on e number of feeds a column may have.

r products, the product type, phase, tray number, and flowrate are supplied in is window. There is no limit on the number of products a liquid-liquid extraction lumn may have and products may be withdrawn from any tray of the column. oduct types include:

Overhead, Bottoms, Fixed Rate Draw, and Pseudoproduct. Every column must have an overhead product leaving tray one and a bottoms product leaving the

Feth FothcoPr


hiH

ghest numbered tray. The product phase may be Light Liquid (Liquid 1) or d 2).

roduct rates must be supplied for all draw products. Rates may be supplied in molar, mass, or liquid volume units. An estimated value must also be provided for either the overhead or bottoms product. The estimated value for the overhead or bottoms rate should be as accurate as possible to enhance convergence. It is necessary to use a Performance Specification to set a desired flow for the verhead or bottoms product.

seudoproducts

re

eavy Liquid (Liqui P

o P Pseudoproducts are used to create streams corresponding to column internal streams, making them available for flowsheet calculations. Pseudoproducts adefined in the Column Pseudoproducts window accessible via the Pseudoproducts… button on the Column Feeds and Products window. The following types of pseudoproducts are available:

Net tray light or heavy liquid flow heavy liquid flow

he solution algorithm is selected in the drop-down list box on the Column main re

uid-Liquid algorithm is selected, the phase system will automatically e set to liquid/liquid.

r of trays in the model is entered in the data entry field provided on n must have at least two trays.

a Column.

Total tray light or Column Algorithm Tdata entry window. The Inside-Out (default), Sure, and Chemdist algorithms afor distillation columns. To specify a liquid-liquid extraction column, select the Liquid-Liquid option. Calculated Phases When the Liqb Number of Trays

he numbeTthe Column main data entry window. Every Colum

here is no limit on the number of trays in T


Number of Iterations The maximum number of trial solutions is supplied in the data entry field provided

The default value is 30 for the Liquid-iquid algorithm.

on the Column main data entry window. L Pressure Profile The pressure for every tray in a column model must be defined. All calculations are performed at the defined tray pressures. The tray pressures are defined in the Column Pressure Profile window, which is reached by clicking Pressure Ps

rofile… on the Column main data entry window. Tray pressures may be

ode, the top tray pressure must be supplied and either the

re re

p

are determined by linear interpolation of supplied

d side coolers may supplied via the Column Side

upplied on an overall or tray by tray mode by choosing a radio button in this window.

or the overall mFpressure drop per tray or the total pressure drop aross the column. A default value of zero is supplied for the pressure drop per tray and the column pressudrop. All tray pressures are derived by linear application of the supplied pressu

rop. d Individual tray pressures are supplied for the tray by tray mode. Note that the toand bottom trays must be included when supplying a table of individual tray

ressures. Missing pressurespvalues. Heaters and Coolers Side heaters anHeaters/Coolers window accessible via the Heaters and Coolers… icon on the

rovided: tray number, a reference name, and the duty, with the appropriate

he Liquid-Liquid algorithm uses an iterative solution technique, starting from an fault,

e some or all of the values produced

Column main data entry window. A negative duty indicates cooling; a positive duty is used for heating. There are no limits on the number of side heaters/coolers. For each side heater/cooler, the following information must be palgebraic sign. Initial Estimates Tinitial estimate of the tray temperature, flow and composition profiles. By dethe initial estimate is produced internally using the initial estimate generator.

ser-supplied profiles may be used to replacUby the estimate generator.


Click Initial Estimates… on the Column main data entry window to enter Column Initi

the al Estimates window.

e

ou may optionally provide temperature estimates for the top and ottom trays which replace values predicted by the estimate generator, as well

estimate generator is not used, the data which must be supplied s input profiles are tray temperatures and flows, either light or heavy liquid, or a

e e these

estimate. It may also be desirable to provide solution profiles

When using the initial estimate generator, profiles are determined by a simplmaterial balance. Temperatures are determined from estimated product compositions. Ybas an estimate of the ratio of the liquid flows on tray 1. When the initial acombination thereof. Note that the minimum data which may be supplied are thtemperatures and flows for the top and bottom trays for the column. Whilare the minimum data required, they are rarely adequate to produce an acceptable initial from a converged solution to speed future calculations with a column model. Initial profiles are entered in tables accessed by clicking the following buttons on the Column Initial Estimates window: Net Vapor Rate… , Vapor Composition… , Tray Temperature… , Liquid Composition… and Net Liquid Rate… . Composition estimates are rarely needed for most problems.

ted. For am rate, heat duty,

or draw rate. Furthermore, for convergence to be achieved, there must be a direct effect on all of the SPECs by the collective set of VARYs. To supply SPECs and define VARYs, access the Column Specifications and

Performance Specifications

Performance specifications or SPECs may be imposed on a liquid-liquid extraction column operation such that product stream flows or properties, column internal flows, column tray temperatures, etc., are at desired values in the solution. For each SPEC, a degree of freedom or VARY must be calculaa liquid-liquid extraction column, a VARY may be a feed stre

Variables window via the Performance Specifications… button on the main Column data entry window. SPECs and VARYs are entered or edited via the hypertext strings. PRO/II requires that there be an equal number of SPECs and VARYs. Thus, when a SPEC is added or deleted, you are required to add or delete a VARY.

PECs and VARYs use the general form in PRO/II and are discussed more fully in the SPEC/VARY/DEFINE section of this chapter. A list of the stream and

uid-liquid extraction column parameters which may be used for SPECs and ARYs is also given in this section.

S

liqV


Convergence Data

Convergence data include algorithm tuning parameters, tolerances, and history printout options for Column iterations. Open the Column Convergence Data

window via the Convergence Data… button on the Column main data entry indow to enter these data. The tuning parameters are as follows:

amping Factor: A damping factor of less than unity may be used to improve

convergence when the convergence is oscillating. A default value of 1.0 is supplied by PRO/II.

rror Increase Factor: This factor limits the increase in the sum of the errors from iteration to iteration. PRO/II supplies a default value of 100.

he maximum liquid-liquid equilibrium tolerance (equal to the e point tolerance for VLE) for each tray. The default is 10-3 .

nthalpy Balance: The maximum heat balance error for each tray. The default

-3

on column iterations is useful in iagnosis of a convergence failure. History printout for the iterations may be

w

D

E

Note: The use of tuning factors usually increases the solution time. Tolerances for the liquid-liquid extraction column equations may also be changed although this should rarely, if ever, be done and never as a means to reach a converged solution. Tolerances are:

iquid-liquid: TLbubbl

Eis 10 . Component Balance: The maximum relative component balance error for each tray. The default is 10-3 .

rintout of the liquid-liquid extractiPdrequested by clicking Convergence Data… and selecting the printout level

esired. Print Options

d

Click Print Options… on the ColumPrint Options data entry wind

n main data entry window to enter the Column ow. Select the desired report options with the check

boxes provided. To request plotted results, click Plot Column Results… and ta select the desired plots with the check boxes on the Column Plot Options da

entry window.


thermodynamic system which supports liquid-liquid equilibrium is required for e equilibrium calculations on each tray. The thermodynamic system may be anged from the global default in the Column Thermodynamic Systems data

Thermodynamic Options A thchenC

try window which is reached by clicking Thermodynamic Systems… on the olumn main data entry window. A single thermodynamic system may be

defined for the complete column or different systems may be used in individual sections of the column.


Column, Side

General Information The Side Column unit operation models side strippers and side rectifiers associated with a main Column. The Side Column model is currently restricted tothe Inside-Out, Enhanced I/O and Sure algorithms. See Column Algorithm in the Distillation Column discussion (page 191) for further information on these methods. Side Columns always use the same distillation algorithm as the m

olumn. Mu

ain ltiple Side Columns attached to one main Column are possible and,

ce in the petroleum refining industry.

nd Products Side Columns are added to the flowsheet with the Side Column unit icon and attached to the main Column with the feed and product streams. Every Side Column has at least one external product which exits the complex column arrangement. Solution Methods

olution methods for Side Columns vary with the algorithm. The Inside-Out (and I/O) algorithm merges the Side Column with the main column and complex column arrangement simultaneously.

n.

both a D86 (5%) and a D86 side stripper product. To solve this same set of re method requires the use of a Multi-variable Controller

nit wrapped around the main column/side column units.

n and

Cin fact, are common practi Feeds a

SEnhancedolves thes

There are three benefits to this approach:

• The simultaneous method results in more precision in the solutio• The simultaneous solution is more efficient and uses less computing

time. • The simultaneous solution provides more flexible product specifications.

or example, the last benefit permits the use of F

(95%) specification for a specifications with the Suu The Sure method solves each side column separately from the main columuses recycle streams to relate the side column and main column. While special recycle logic is used to converge the column/ side column recycle problem, this method has three disadvantages when compared to the Inside-Out column simultaneous treatment:


• The solution is less precise since a recycle stream tolerance is used in on to the column equation tolerances.

• The recycle approach is much slower.

Add o Side tr front end volatility (flash point) of

uid products such as diesel, fuel and kerosene. The liquid product is drawn top tray of the side stripper, which

typically has ing medium (usually steam) is fed to the bottom tray of the side stripper to strip about ten percent of the liquid feed (the lightest material) which is then returned to the main column for further fractionation together with the stripping medium. The stripped liquid is withdrawn from the bottom tray of the stripper as a finished product. Steam side strippers ave an overall tray efficiency of about 25 percent and can be represented with

tage of this arrangement is a smaller stripped vapor return stream to the main column which reduces the vapor loading for the

rs have higher tray efficiencies than those hich use a stripping medium. Therefore, three to five theoretical trays are

odeling some unusual types of column configurations.

Additional Information on Side Rectifiers

ide rectifiers are used to remove heavy materials from vapor draw products by e vapor draw from the main column is fed to

the bottom tray of the side rectifier which may have a large number of trays. The

he overhead product from the side rectifier is removed as a finished product. The liquid from the bottom tray is returned to the main column for further fractionation.

additi

• Main column variables (except the main column draw rate) cannot be directly related to the side stripper products. This makes it necessary to use controllers to solve for more than one specification on a side product.

iti nal Information on Side Strippers

s ippers are widely used to control theliqfrom the main column and charged to the

6 to 10 actual trays. A stripp

htwo theoretical trays. A variation in side stripper design is the use of a reboiler on the bottom of the side stripper to "heat strip" the liquid feed. No stripping medium is used for reboiled side strippers. The advan

main column. Reboiled side strippewtypically used to model these strippers. Side strippers do not normally have any other items of equipment such as condensers, pumparounds, side heaters/coolers, etc. Only the Sure method permits the use of a condenser on a side stripper. This capability may find utility when m

Sproviding a rectification section. Th

side rectifier must have a condenser or cooling duty at the top to condense the liquid reflux which is used to rectify the vapor product. T


The side rectifier corresponds to the rectification section of a conventional distillation column. An overall tray efficiency of 45 to 55 percent is reasonable for many applications.

de rectifiers do not normally have other items of equipment such as mparounds, side heaters/coolers, etc. Reboilers are never used for these lumns.

Sipuco


Compressor

General Information The Compressor simulates a single stage isentropic compression. Outlet conditions and work requirements may be determined using either an adiabatic or polytropic efficiency. Optional tabular input may be used to determine

th

A compressor operation may have multiple feed streams, in which case the inlet pressure is assumed to be the lowest feed stream pressure. Compressors may have one or more product streams. The product phase ondition for units with one product stream is automatically set by PRO/II. For

performance from supplied curves for outlet pressure or pressure ratio, head,work, and/or efficiency. An optional aftercooler calculation may be included. BoVLE and VLLE calculations are supported. Multistage compressors may be modeled by linking single stage compressor units. Feeds and Products

ccompressors with two or more product streams, the product phases must be specified in the Product Phases window which is accessed by clicking Product Phases… on the Compressor main data entry window. Note that for compressors

ith aftercoolers, the products correspond to outlet conditions from the

,

apor and liquid products and is not allowed when four product streams are

The pressure, work, or head specification is selected from a drop-down list box in

Outlet Pressure: The outlet pressure from the compressor. Pressure Increase: The pressure rise across the compressor.

waftercooler. Product phases allowable include: vapor, liquid, decanted water, heavy liquidand mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vspecified. Pressure, Work, or Head Specification

the Compressor main data entry window. At least one specification must be supplied for every compressor. Options include:


Pressure Ratio: Compression ratio (absolute outlet pressure/absolute inlet ressure).

ork: Actual work for the compressor.

p W Pressure Curve: Click Enter Curve… to supply a curve relating volumetrrate to outlet pressure in the Compressor Outlet Pressure Performance Cwindow.

ic feed urve

Pressure Ratio Curve: Click Enter Curve… to supply a curve relating volumetric ed rate to compression ratio in the Compressor Pressure Ratio Performance

feCurve window.

Adiabatic Work Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to adiab

urve window. atic work in the Compressor Work Performance

C Polytropic Work Curve: Click Enter Curve… to supply a curve relating

volumetric feed rate to polytropic work in the Compressor Work PerformanceCurve window. Actual Work Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to actual work (efficiency has been applie

erformance Curve window. d) in the Compressor Work

P Adiabatic Head Curve: Click Enter Curve… to supply a curve relating volumetric

dow. feed rate to adiabatic head in the Compressor Head Performance Curve win

Polytropic Head Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to polytropic head in the Compressor Head Performance

urve window. C Actual Head Curve: Click Enter Curve… to supply a curve relating volumetri

ed rac

te to actual head (efficiency has been applied) in the Compressor Head

fficiency or Temperature Specification

selected from a drop-down list box in the Compressor main data entry window. Options are:

y: Compressor adiabatic efficiency in percent. This is e “isentropic” efficiency.

fePerformance Curve window. E An efficiency or outlet temperature specification may be

Adiabatic Efficiencsometimes called th Polytropic Efficiency: Compressor polytropic efficiency in percent.


Outlet Temperature: Compressor outlet temperature. The efficiency is alculated. c

Single Adiabatic Efficiency Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to adiabatic efficiency in the Compressor Efficiency

urve window. C Single Polytropic Efficiency Curve: Click Enter Curve… to supply a curve relating volumetric feed rate to polytropic efficiency in the Compressor EfficiencyCurve window.

Multiple Adiabatic Efficiency Curve: Click Enter Curve… to supply multiple

iency curves at designated Compressor inlet or outlet pressures, which relate volumetric feed rate to adiabatic efficiency in the Compressor Multiple EfficCurves window. Multiple Polytropic Efficiency Curve: Click Enter Curve… to supply multiple curves at designated Compressor inlet or outlet pressures, which relate volumetric feed rate to polytropic efficiency in the Compressor Multiple EfficiencyCurves window. Selection of an efficiency or tem

perature specification is

ptional, and if none is selected a default value of 100 percent adiabatic hat this corresponds to a perfect isentropic compression.

, and efficiency are usually based on a specific compressor speed. Therefore, they should be adjusted when the compressor is operated at a

oefficiency is used. Note t RPM Adjustment of Compressor Curves Curves for head, work

different speed. PRO/II performs adjustments for these curves when values aresupplied for the Reference RPM (curve basis) and the Operating RPM. Adjustments are based on the fan laws and are as follows:

[ ] 0.2referenceRPM / RPMrefHead Head =

[ ]3.0

referenceRPM / RPMref Work Work =

[ ]reference

RPM / RPMrefEfficiency Efficiency =


Aftercooler Option An aftercooler may be added via the Aftercooler… icon on the Compressor main

ssure drop the Compressor Aftercooler window.

estimate for the outlet temperature for the compressor may optionally be pplied in the Compressor main data entry window to speed convergence. Note

that this is not the same as the Outlet Temperature specification. Calculation Method The method used to calculate the Compressor head may be selected by clicking

data entry window and supplying the cooler outlet temperature and prein Outlet Temperature Estimate Ansu

Calculation Method… on the Compressor main data entry window to access the Compressor Calculational Mode window. The method may be chosen with the radio buttons provided, with choices as follows: GPSA Engineering Data Book: The GPSA Data Book equation is used to compute head. ASME Power Test Code 10: The ASME Power Test Code 10 equation is used to compute head. This method, the default, is the most rigorous. The compression ratio above which the head equation is used to compute the isentropic/ polytropic coefficient may also be supplied in this window. This entry only applies to the GPSA method, with a default value of 1.15 supplied. Below this compression ratio, the GPSA “temperature equation” is used to compute the isentropic/polytropic coefficients. Relative Convergence Tolerance for Work Specifications For compressors with Work specifications, a relative convergence tolerance may optionally be supplied in the Compressor main data entry window. A default value of 0.001 is used when no value is supplied. Maximum Outlet Pressure For compressors with Work specifications, a maximum outlet pressure may optionally be supplied in the Compressor main data window. The outlet pressure will be reset to this value when the supplied work results in a pressure exceeding this value.


Thermodynamic System

The thermodynamic system of methods to be used for compressor calculations y be selected by choosing a method from the Thermodynamic Systems drop-

Compressor main data entry window.

mdown list box on the

a


Controller

General Information

Controller simulates the action of a feedback The process controlled by adjusting an upstream flowsheet parameter to achieve a specified result for a process tream or unit operation. A controller must have one SPECification and one

d

or

tring Parameter i e Feedback Controller window. The Parameter w to designate the stream or unit parameter to use for

e VARY in a manner analogous to that used in selecting the SPEC above. The

will also find tables of the flowsheet variables that may be used for SP controller units. Limits and Step Sizes

sVARY, where the SPEC may be a stream flowrate or property, a unit operating condition, or a Calculator result. The control variable (VARY) must be a stream or unit operation flowsheet parameter that is otherwise at a fixed value in the flowsheet. Specification The SPECification is supplied via the appropriate underlined hypertext in the Specification field of the Feedback Controller main data entry window (accesseby double-clicking on the Controller flowsheet icon). By clicking the hypertext string Parameter, the Parameter window appears in which you can select the unit parameter or stream parameter to use as the SPEC. The SPEC may be a single parameter or a mathematical expression that relates two flowsheet parameters.You may next enter the value and the tolerance for the SPEC by clicking the appropriate linked text. See the SPEC/VARY/DEFINE section of this chapter ffurther details on the generalized SPEC form used in PRO/II. Variable The control variable (VARY) is selected by clicking the linked text s

n the Variable field of thindow is used

thSPEC/VARY/DEFINE section of this chapter gives more information on the VARY concept. You

ECs and VARYs in

Limits and step sizes for the control variable may be supplied by clicking Limits and Step Sizes… on the Feedback Controller window. A maximum value, minimum value, and/or maximum change in the control variable may be entered in the Limits and Step Sizes window. Optionally, you may supply a value for the


control variable for the second iteration by selecting the appropriate radio buttonto replace the default change o

f 2.0 percent of the initial control variable value.

You may specify a different percent or value for the second iteration.

Several par arding the operation of the Controller may be supplied on

• ns

• Flow ted. Print Results for Contro s The default ch controller iteration. To eliminate this printout, de edback Controller window.

Next Unit Calculated after Control Variable is Updated Ordinarily, this is the first unit operation in the calculation sequence that is affected by the control variable and is determined automatically (“calculated”) by PRO/II. You may specify a different return unit by using the drop-down list box on

e Feedback Controller window.

of Controllers

ntroller uses a Newton-Rhapson technique to search for the value of the ontrol variable that meets the specified flowsheet parameter result. Therefore, it

e cation. Control functions with discontinuities or

localized maxima and minima may fail to converge or converge to an undesired result.

or some cases, the limits and step sizes entries may keep the control function within a range of feasible solutions. Controllers ps

Parameters

ameters regthis section of the Feedback Controller window. You may change the maximum number of iterations from the default value of 10. Use the radio buttons may to select the action taken when the control variable exceeds the prescribed limits:

The value is set to the limit as a solution and flowsheet calculatiocontinue (the default), or

sheet calculations are hal

ller Iteration

is to print a summary for easelect the check box on the Fe

th Nonconvergence

The cocis important that there be a continuous and monotonic relationship between thcontrol variable and the specifi

F

and Recycle Loo Controllers always create a recycle loop in the flowsheet, from the downstream unit at which the specification is evaluated to the first upstream unit affected by the control variable.


When a controller is located within a recycle loop, PRO/II normally solves the controller as part of the loop, i.e., the controller iterations and the recycle iterations ar ly. Therefore, you must change the calculation order when it is desired to converge the controller within each iteration of the

verall recycle loop. Note also that it is important that the tolerance for the

e solved simultaneous

ocontroller be tighter than the tolerance for the overall recycle loop to insure convergence.


Crystallizer

General Information

he Crystallizer unit operatiT on simulates crystallization processes for the manufacture of organics, inorganics, fertilizers, biochemicals and polymers. The crystallizer transforms a supersaturated solution into a mixed solid/liquid crystal

allizer is modeled as a Mixed Suspension Mixed Product Removal

conditions. The model also assumes that breakage or

solu calculated from either the Van't Hoff equation or user-supplied

select Design or Rating calculations in the Crystallizer Calculation

T ips are expressed as power law expressions in the

nual.

The Crystallizer can have any number of feed streams. The inlet pressure is

Both an overhead and bottoms product must be specified in the Crystallizer

y vapor generated in the unit.

slurry.

he crystT(MSMPR) crystallizer or Continuous Stirred Tank Crystallizer (CSTC). These models assume ideal mixing in the unit and that the product conditions are theame as the bulk s

agglomeration of solid particles is negligible. A feed heat exchanger may be included in the model with recirculation if required. The crystallization process depends on phase equilibria as well as kinetic or nonequilibrium considerations. Solid-liquid equilibrium is defined in terms of

bility, which is solubility data. You mustMode window. In design mode, a specification is required and the volume is calculated. In the rating mode, the vessel volume is defined.

he formation rate relationshCrystallizer Growth and Nucleation Rates window. These relationships are similar to equations for power law kinetics used for chemical reactions. Full details of the calculation method can be found in the PRO/II Reference Ma

Feeds and Products

taken to be the lowest pressure of all the feed streams.

Products window. The bottoms contains the crystals in the solid/liquid slurry. The overhead contains an


Unit Specification

ecified by filling in the appropriate data variables r Solute and Solvent, Crystal Shape Factor, Calculation Mode, Design pecification (in Design Mode) and Growth and Nucleation Rates in the

ay be accessed through the Crystallizer ain data entry window that is accessed by double-clicking the Crystallizer unit

elect the solute and solvent components. The solute must be defined as a in the

imulation, a warning message is displayed prior to opening the Crystallizer main

election/ Component Phases.

A Crystallizer unit operation is spfoSappropriate data entry windows that mmicon. Crystal Shape Factor The shape factor defaults to 1.0 which indicates cubic crystals. A value of p/6 indicates spherical crystals. Solute and Solvent Sliquid-solid component. If there are no liquid-solid components availablesdata entry window. To specify a component as liquid-solid, select Input/Component S Calculation Mode Click Calculation Mode… to specify the Design or Rating calculation mode.

olume is calculated.

rystals in weight

otal solute in the

Xexit is the liquid phase mole fraction of the solute in the bottom product, and

In Design mode, a specification is required and the vessel vSpecification options are: Crystal Production Rate: Enter the production rate of the cunits. Fraction of Solute Crystallized: Enter the fraction of the tcombined feeds that is to be crystallized. Magma Density in the Bottom Product: Enter the density of the bottom product as weight of crystals per unit volume of slurry. Supersaturation Ratio: Enter the supersaturation ratio which is defined as: (Xexit-Xsat)/Xsat where:


Xsat is the saturation mole fraction of the solute in the bottom product. In Rating mode, the vessel volume is defined.

wth and Nucleation Rates Gro C

lick Growth and Nucleation Rates… to specify Growth and Nucleation Rates.

rystal Growth Rate: You must supply the Rate Constant for the rate equation ft/sec or m/sec. Growth rates are typically in the range 2.0x10-7 to 2.0x10-8 /sec. By default, the rate is directly proportional to the Supersaturation Ratio. u may change this by overriding the default Exponential Factor. Factors are ually in the range 0.0 to 2.5.

rystal Nucleation Rate: The Nucleation Rate is the number of crystals cleated per unit time, per unit liquid volume. You must supply the Rate

onstant for nucleation and specify its dimensional units. By default, the rate is rectly proportional to the Supersaturation Ratio. You may change this by erriding the default Exponential Factors. Typical values for the Supersaturation

atio Factor are in the range 0.5 to 2.5 for secondary nucleation and up to 10 for imary nucleation. If an exponent is specified for the Impeller Speed, you may ed to change the default value of 100 RPM.

perating Conditions

CinmYous CnuCdiovRprne O Click Operating Conditions… to specify Crystallizer Operating Conditions. By

fault, the crystallizer operates at the combined feed temperature and pressure ith no recirculation.

essure Specification: The pressure may be specified as a drop below the combined feed pressure or you may specify the pressure value directly.

cond Specification: If an option other than At Merged Feed Temperature is cted, the unit is assumed to include a feed heat exchanger. You may specify

either the crystallizer operating Temperature or the Duty of the exchanger.

ecirculation Flowrate: Some of the bottom product may be remixed with the feed and passed through the feed exchanger. To specify this option, you must

cify the recirculation Volumetric Rate or the Temperature Change ross the exchanger. A negative change denotes a temperature drop.

ternatively, instead of entering a numeric value for the parameters in this window, they may be referenced using the DEFINE system relative to any available unit operation or stream parameter calculated elsewhere in the

mulation. See the table of Crystallizer Parameters available for Cross-eferencing in the online help for more details.

dew Pr

Sesele

R

either speac Al

siR


rint Options P

Click Print Options… to access the Crystallizer Print Options window. Check the Include Crystal Size Distribution box to request additional output

cluding tables of fractions and population densities for the feed and product streams as functions of the crystal size distribution. in


Cyclone

General Information The Cyclone solid and ga e

s loadin c , particle size distribution, stream

et

.

t have a particle size distribution. nit or defined by the user.

alculations, and multiple cyclone configuration in the Gas/Solid yclone main data entry window that is accessed by double-clicking the Cyclone

he PFD.

in

unit operation models the separation of particulate solids from as stream. The particulate collection efficiency is determined by th

solidfl

g, omponent characteristicsowrate, and cyclone geometry. The Cyclone unit operation will calculate the

collection efficiency for every particle size range of each solid component as well as the pressure drop through the unit. The Cyclone is assumed to operate isothermally and mechanisms such as agglomeration and crumbling are discounted. Feeds and Products A Cyclone may have up to ten feed streams. Unless otherwise specified, the inlpressure will be taken as that of the feed stream with the lowest pressure. The feed streams may not contain a liquid phase, and there must be two product streams. The overhead stream will contain all the gas that comes in as well asany uncollected solids. The bottom stream will contain only the collected solidsAll solid components that enter a cyclone musThis distribution may be set by another u Unit Specification A cyclone unit operation is specified by filling in the appropriate real and integer data variables for operating mode, geometry, pressure drop calculations, efficiency cCunit icon on t Rating Mode If you select Rating Mode, you must supply the diameter of the cyclone. The other dimensions of the cyclone will be generated from the diameter. If you selectUser Defined Geometry, you must also enter all of the geometric ratios as described below. In Rating Mode, PRO/II will calculate: pressure drop, total efficiency, component efficiencies, grade efficiencies and weight percent solids the overhead stream.


Design Mode

output, Design Mode will calculate the number and size

of identical cyclones that are necessary to meet the specification. There may be systems that meet the specification. In all cases, Design Mode will

return the system requiring the fewest cyclones.

The model a system of identical cyclones that are arranged either in par l se of parallel cyclones, the feed streams are split eve a s. The overhead products from all cyclones merge into one e cts from all cyclones merge into one bottom

e first cyclone is the ead product

re

2. API (default) 3. Lapple

odel is based on a ratio of particle diameter to cut diameter

If you select Design Mode, you need not provide the cyclone diameter. Again, if you select User Defined Geometry, you must enter all of the geometric ratios as described below. In addition, you must specify a target for total solids collection (see entry for RPARM(13) below). You may also wish to override the default maximum pressure drop of 10 inches of water by entering a value in whatever input pressure units you prefer (see entry for RPARM(16) below). In addition tothe normal Rating Mode

many cyclone

Multiple Cyclones

Cyclone canalle or in series. In the canly mong the cyclone ov rhead and the bottoms produ

stream. In the case of series cyclones, the overhead from thed to the second and so on. The overhead product is the overhfe

from the final cyclone while the bottom product is the combined bottom product from all the cyclones in the system. Both product streams are at the outlet pressure of the final cyclone in the system. It is not possible to specify recycle streams inside the unit or to reference intermediate stage data from the flowsheet. For example, if you wish to set a specification on the second cyclonein a three-cyclone series or set a recycle from the second cyclone to the first cyclone, you should model the system as three separate units. Note that while increasing the number of identical cyclones will increase efficiency and pressudrop in a series system, it will decrease the efficiency and pressure drop in a parallel system.

teger Data for Unit In Calculation Mode (IPARM(1)) This input is optional. Options are:

1. Rating (default) 2. Design

Efficiency Model (IPARM(2)) This input is optional. Options for Rating and Design mode are:

1. Koch & Licht

The Lapple m


(the diameter of the particles which are collected with 50% efficiency). The API method is based on a ratio of particle diameter to critical diameter (the diameter of particles which would be collected at 100%). The Koch & Licht method is not

ased on a particle size ratio. Pressur M M(3)) This input is optional. Options for both Rating and Design mod

2. API If the cy n ssel, the API method allows values for the Inlet Width Ratio elocity (described later in the section titled Real Da fo

ed geometry

th ratio, cyclone dust outlet diameter ratio, cyclone gas outlet

diameter ratio, gas outlet tube length ratio, height of cylindrical section ratio, and total cyclone height ratio as appropriate for the calculation method used as shown. Inlet Vane Flag (IPARM(5)) This input is optional. Options for both Rating and

esign mode are:

(6)) This input is optional. Options for both

sign mode are: 1. No (default)

es

b

e odel (IPARe are:

1. Koch & Licht (default)

clo e is inside another veand the Superficial Gas V

ta r Unit) to be specified. Cyclone Geometry (IPARM(4)) This input is optional. Options for both Rating and Design mode are:

1. Stairmand (default) 2. High efficiency Swift 3. Lapple 4. General purpose Swift 5. Peterson & Whitby 6. User-defin

f the user-defined geometry is used, values must be specified for the inlet heightIratio, inlet wid

D1. No (default) 2. Yes

Shape of Gas Inlet Flag (IPARMRating and Design mode are:

1. Tangential (default) 2. Scroll or volute 3. Axial

Cyclone is inside Vessel Flag (IPARM(7)) This input is optional. Options for both Rating and De

2. Y


For a value of 2, the Inlet Width Ratio and the Superficial Gas Velocity must be specified. Dipleg Size is calculated if the value of 2 is entered. Efficiency Adjustment Due to Loading Flag (IPARM(8)) This input is optionalOptions for both Rating and Design mode are:

1. Adjust (default) 2. Do not Adjust

.

utomatically Switch Pressure Drop Model (IPARM(9)) This input is optional. de are:

2. Switch This entry allows changes to be made automatically in the pressure drop model between the Koch & Licht and API methods based on solids loading.

.

ht fraction of 0.20 in size range 20 to 30, the value for this ze range) and the value for a DEFINE statement

e first size range).

Number of the Component to be Specified (IPARM(13)) This input is optional and is for Rating Mode only. This optional input is the number of the component

cle size distribution data to be used in the design. The default is the first lid component with a PSD that the design mode may evaluate.

Maximum Number of Cyclones (IPARM(14)) This input is optional and is for esign Mode only. The value indicates the number of cyclones in parallel or ries as appropriate based on the value specified above for the Configuration of ultiple Cyclones Flag. The default is 20 for parallel and 3 for series.

Real Data for Unit

AOptions for both Rating and Design mo

1. Do not Switch (default)

Configuration of Multiple Cyclones Flag (IPARM(10)) This input is optionalOptions for both Rating and Design mode are:

1. Parallel (default) 2. Series

Number of Identical Cyclones (Series or Parallel) (IPARM(11)) This input isoptional and is for Rating Mode only. The default value is 1 cyclone. Number of Particle Size to be Specified (IPARM(12)) This input is optional and is for Rating Mode only. This and the following entry can be used together to specify the component and PSD size range whose weight fraction in the overhead will be output to RPARM(64). This latter value can be accessed by a Controller, MVC or Optimizer. For example, if a solid with PSD data: 10, 20, 30, 40 (in default input units) is

quired to have a weigreentry would be 2 (the second si

ould be 0.20. The default value is 1 (thw

with partiso

DseM


The cyclone geometry is input as the ratio of length divided by overall cyclone ody diameter, so that an inlet height of 0.1 meters on a cyclone of diameter 0.2

meters would have an inlet height ratio of 0.1/0.2 = 0.5.

iameter of Cyclone Cylinder (RPARM(1)) This input is required and is for Rating Mode only.

Inlet Height Ratio (RPARM(2)) This Rating/Design Mode entry is optional. Inlet Width Ratio (RPARM(3)) This Rating/Design Mode entry is optional.

iameter Ratio (RPARM(4)) This Rating/Design Mode

Cyclone Gas Outlet Diameter Ratio (RPARM(5)) This Rating/Design Mode ntry is optional.

Gas Outlet Tube Length Ratio (RPARM(6)) This Rating/Design Mode entry is optional. Height of Cylindrical Section Ratio (RPARM(7)) This Rating/Design Mode ntry is optional.

Ratio (RPARM(8)) This Rating/Design Mode entry is

s

cy for Design Mode (wt%) (RPARM(13)) This Design Mode entry is required.

inimum Cyclone Diameter (RPARM(14)) This Design Mode entry is optional. he default is 0.1 m.

b

D

Cyclone Dust Outlet Dntry is optional. e

e

e

otal Cyclone HeightToptional. Diameter of Vessel Housing (RPARM(9)) This Rating/Design Mode entry ioptional. Superficial Gas Velocity (RPARM(10)) This Rating/Design Mode entry is optional. Pressure Drop to Inlet (RPARM(11)) This Rating/Design Mode entry is optional. This value is the pressure drop between the feed stream and the inlet to the cyclone. The default is 0.0. Absolute pressure at cyclone inlet (RPARM(12)) This Rating/Design Mode entry is optional. For use if cyclone inlet pressure differs from feed stream pressure. The default is the lowest feed stream pressure. Goal Efficien

MT


Maximum Cyclone Diameter (RPARM(15)) This Design Mode entry is optional. he default is 0.5 m.

Maximum Pressure Drop (RPARM(16)) This Design Mode entry is optional. This value is pressure drop across cyclones in a unit The default is 2.488 kPa.

dy Diameter (RPARM(17)) This Design Mode entry 001.

he indicated cations in the ) array and can be accessed by a Controller, MVC or

) outputs are produced in both Rating and Design modes.

otal Solids In Overhead (RPARM(54)) This is the weight % of the total

let Height Dimension (RPARM(55))

let Width Dimension (RPARM(56))

yclone Gas Outlet Diameter Dimension (RPARM(58))

ARM(59))

Height of Cylindrical Section Dimension (RPARM(60)) Tot Dip lone be located above a fluidoutput ioverhea

T

the maximum

Tolerance for Cyclone Bois optional. The default is 0. Real Number Output from Cyclone

he output values calculated by the Cyclone model are stored in tTlo RPARM(Optimizer. All RPARM( Overall Efficiency (wt%) (RPARM(51)) In Design mode, this is an input value included in the output report for the cyclone unit. Diameter Of Cyclone Cylinder (RPARM(52)) In Rating mode, this is an input value included in the output report for the Cyclone model. Pressure Drop (RPARM(53)) This is adjusted for loading by the user. Toverhead stream. In In Cyclone Dust Outlet Diameter Dimension (RPARM(57)) C Gas Outlet Tube Length Dimension (RP

al Cyclone Height Dimension (RPARM(61))

leg diameter (RPARM(62)) This requires that the cycized bed, i.e., the cyclone must be located inside a vessel. This value is

n the cyclone output report only if applicable. PSD weight fraction in the d RPARM(64) This value is the particle size distribution weight fraction in


the over M(12) and IPA is is the ratio of weight in the specified size range divi the cycl ut report only if applicable.

head of the size and component specified. See entries for IPARRM(13) above. Th

ded by the weight of the component in the overhead. This value is output inone outp


Depressuri

ng Unit

General I Thethatdiffeunit ified. The y be either a vapor or a vapor-liquid mixture. Calculation options include procedures from API Standard 2000, API Recommended Practice 520, and other industry standards. Initial Relief Conditions The initial relief conditions can be based on either a specified initial time or a spe l pressure by selecting the appropriate radio button. The default selesim Not odel” is s Fin To set the finfina

om Relief by choosing the desired toggle text. If oth final Vessel Pressure and Elapsed Time are selected, the depressuring

hen the first criterion is satisfied.

nformation

Depressuring Unit simulates the time-pressure-temperature relationships occur when a vessel is depressured through a relief or control valve. Several rent valve models, vessel configurations and models for heat flow into the are available. An optional external makeup stream may also be specinitial phase of the vessel contents ma

cified initaction is to start the depressuring calculations at the beginning of the ulation (time zero.)

e: This option is only available if the heat input model type “Fire Relief Melected.

al Depressuring Conditions

al depressuring conditions, values may be entered for either or both l Vessel Pressure and Elapsed Time. The elapsed time can be measured Time Zero or from the Start of fr

bcalculations will stop w Time Step Size Calculation Options User-supplied values for the relative volume tolerance per time step, the maximum number of time steps, and the time step size can be entered on the Calculation Options window. This window is brought up by clicking Calculation Options… on the Depressuring Unit main data entry window.


The default value for the Volume Tolerance per Time Step is 0.0001. The default alue for the Maximum Number of Time Steps allowed in the depressuring

simulation is 0.

default v ue the sizing parameters rameters used in this

ulation m be p size basis is selected f

a. tob. vac. th

The default selecta user-supplied value for the constants can be entered in the pop-up float field.

the time p s For (2), the default val Specification of I Either the default the blowdown calcDepressuring Unit pt

Rigorous Bloworous Blo dow

Model, the default

n when rro

By default, the sim g on the Stop hyper

and low re

Valve Data Data can be entercharacteristics of t

v10

The al for the Time Step size is calculated using default values for . User-supplied values for the pa

calc ay entered via the appropriate hypertext string. The sterom a pop-up list, which includes

tal fluid quantity in increments of the amount* (a constant) por quantity in increments of the amount* (a constant), or e smaller of (1) or (2).

ion for time step size basis is (1). If either (1) or (2) is selected,

For ste ize basis of (1), the default value of the constant is 0.04.ue of the constant is 0.50.

sentropic Efficiency

isentropic efficiency or a user-supplied value may be used in ulations by selecting the appropriate radio button on the - Calculation Options window. For all heat flow models excedown or Semirigorous Blowdown, the dfor

Rigefault value is 0.0. If

n or Semirigorous Blowdown is selected for the Heat Flow isentropic efficiency is 1.0.

w

Actio

E rs are Detected

ulation will stop if pressure profile errors are detected. Clickintext on the Calculation Options window toggles the option to

Continuedetected.

al s the simulation to continue even if pressure profile errors a

ed on the Depressuring Valve Data window to define the flow he relief valve or control valve. This window is brought up by

clicking Valve Dat e ust b cted from the four choices by choosing the appropriate radio he a ilable valve models are Supersonic Flow, Subsonic Flow,

Constant Flow, and User Model. The default is Supersonic Flow. The equation for the selected model is displayed as an aid to entering the parameters in the

a… on the Depressuring Unit main data entry window. A ValvModel mbutton. T

e seleva


valve equatio Th layed for the equation are consistent with the default UOM for the problem and may not be changed. A Valve Constant For the Supersoni or the Subsonic Flow essure may be entered along with

uired the vaentry is the valve c ust be entered. The d critical flow factor ifactor may be ente

l Data The Depressuring depressuring unit. e Depressuring Unit

• Sphere • Horizonta

Vertic l CUnsp ifie

must be selected If Sphere is the selentered. If Horizontangent-to-tangengeometry, the diam

of ttional. For ss

must be entered. LShape. By default

osition a the or quilibrium ith

volume fraction ba The Vessel Weighgeometry. If one o

are reise the re

The volume correcCylinder, and Vertcorrect the vessel not supplied.

n. e units disp

(C) must be entered for all models except for the User Model. c Flow model, the valve constant is the only entry allowed. F model, an optional back pr

the req lve constant. For the Constant Flow model, the only allowable onstant. For the User model, the control valve coefficient m

efault back pressure value is 0.0, while the default value for thes 1.0 Different values for the back pressure and critical flow red.

Vesse

Vessel Data window is used to define the configuration of the This window is accessible via the Vessel Data button on thmain data entry window. One of the following,

l Cylinder ylinder •

• aec d Shape

by choosing the appropriate radio button.

ected vessel geometry, a value for the diameter must be tal Cylinder is the selected vessel geometry, the diameter and

t length must be entered. For the Vertical Cylinder vessel eter and tangent-to-tangent height must be entered. For

hese defined geometries, entering vessels of anop

y ve

a value for liquid height is els of the Unspecified Shape geometry, the vessel volume iquid Holdup is optional only if the geometry is Unspecified

, the holdup liquid is saturated liquid of the combined feed initial conditions. The remaining vessel volume contacomp

in et

wins vap

this liquid. The holdup may be on a mole, weight, or actual sis with the default being the mole fraction basis.

t and the Vessel Specific Heat may be input for any vessel f these two variables is entered, then both must be entered. quired only if “Blowdown” appears on the Heat InThese items

otherwput window,

optional. (See discussion on vessel Heat Input options below.) tion factor is an optional entry for the Sphere, Horizontal

ical Cylinder vessel geometries only. This entry is used to volume for pipes, fittings, and end plates and defaults to 1.00 if

y a


Heat Input Click Heat Input… on the Depressuring Unit main data entry window to open Heat Input window. A heat input model may be selected from the drop-down list box, which includes the following options:

the

• User-defined

• API RP 520 • Isothermal • Rigorous Blowdown • Semirigorous Blowdown • Fire Relief.

User-Defined is the default as this supplies no heat input to the vessel. The difference between the Rigorous and Semirigorous Blowdown models is the physical property calculations. The selected heat transfer equation is displayed, along with the equation’s units of measure. Depending on the Heat Flow Model selected, from one to five of the coefficients may be supplied. For the User-Defined or Semirigorous or Rigorous Blowdown models, values for these coefficients default to 0.0. For the Fire Relief Model only, the first two coefficients C1 and C2 are required. The Initial Wetted Area field is made unavailable when a value has been entered for Liquid Height on the Vessel Data window. Otherwise, a value for Initial Wetted Area must be entered for the API 2000, Scaled API 2000, RP 520, Scaled RP 520, and Fire Relief Models. The Area Scaling Factor is an optional entry for these same heat input models only when the Initial Wetted Area is input. It has a default value of 1.0. The Heat Input Scaling Factor may be input for any heating model except the Semirigorous and Rigorous Blowdown and Isothermal models. It has a default value of 1.0. For the heat transfer coefficient used in the Semirigorous or Rigorous Blowdown calculations, either a Calculated Using Scaling Factor coefficent, an Overall coefficient, or individual phase vapor or liquid heat transfer coefficient may be used by selecting the appropriate radio button. The default is to use the Calculated Using Scaling Factor coefficent, with a default value for the scaling factor of 1.0.

• API 2000 • API 2000 Method with Scaling • API RP 520 with Scaling


Makeup Stream One feed stream to the depressuring unit can be designated as a constant-rate makeup stream. Click Makeup… on the Depressuring Unit main data entry window to open the Makeup Stream window, where a makeup stream can be designated. Checking the box enables a drop-down list box which contains the names of all feed streams to the depressuring unit shown on the PFD. One

a makeup stream. The flow of this stream will always hen the depressuring begins. By default, no

te and final epressuring Unit. This window can be accessed through at/Unit Operations menu option or from the Depressuring

the toggle text

r

window, either the Default Time Step,a User-ssure Interval can be specified for the

results by selecting the appropriate radio button.

or prob m n one thermodynamic method has been specified, a drop-d e used for the

stream may be selected asegin at time = 0, regardless of wb

makeup stream is included. Print Results for Depressuring Unit

he Print Options window allows the user to control the intermediaTprinted results for the D

e Output/Report FormthUnit main data entry window.. The default for all stream printout is a molar basis; clicking onallows the user to select weight basis. By default, component compositions are printed at all steps. The user may opt to print all steps, or initial, final and relief conditions only by clicking on the hypertext. The user may suppress all composition printout by deselecting the ox. b

Intermediate printout is printed at each calculation step time by default. The usemay select a different interval by clicking on the default time step linked text, which will bring up the Intermediate Print Interval Options window. On the Intermediate Print Interval Optionsdefined Time Step,or aUser-defined Preprinting frequency of the intermediate

Thermodynamic System F le s where more tha

own list box allows the selection of a thermodynamic method set to bDepressuring Unit.


Dissolver

General Information

industry in both

cesses.

inlet pressure is taken to be the lowest pressure of all the feed streams.

oth an overhead and bottoms product must be specified. The default allocation may be modified in the Dissolver Products window. The bottoms contains the liquid product along with any remaining crystals. The overhead contains any vapor generated in the unit.

Calculation Method

e dissolver transforms crystals in solution from the solid to the liquid phase. O/II models the most common type of dissolver which is the stirred tank

ssolver. A feed heat exchanger may be included in the model if required.

Solid-liquid equilibrium method must be defined in terms of solubility, which is lculated from either the Van't Hoff equation or user-supplied solubility data.

select Design or Rating calculations in the Dissolver Calculation Mode indow. In Design mode, a specification is required and the volume is calculated r a given feed particle size distribution and operating conditions. In Rating ode, the vessel volume is defined and the exit particle size distribution is termined.

e mass transfer coefficient may be specified in the Dissolver Dissolution Rate indow. Alternatively, you may specify that the coefficient should be calculated m diffusivity data entered in the Thermodynamic Data.

Full details of the calculation method can be found in the PRO/II Reference Manual.

The Dissolver unit operation models the dissolution of solids into liquid solutions.This mass transfer operation is widely used in the chemicalorganic as well as inorganic pro Feeds and Products The dissolver unit can have any number of feed streams. The

B

ThPRdi A caYou mustwfomde Thwrof


Excel Unit

General Information The Excel unit operation can be used to include Microsoft Excel spreadsheet filesas general unit operations in the flowsheet. During calculation, PRO/II transfers feed stream information to the spreadsheet, in

the resulting product stream information bac

vokes a user-defined macro, then reads k into PRO/II.

and configure the Excel spreadsheet file which will be used for calculations.

ection

can be used for any other purpose.

d

d e output stream conditions

ased on the input feed streams and the unit operation data.

t has been customized, a user can add it to a PRO/II

croll to the bottom of the PFD palette, click the Excel button, and click an empty area of the flowsheet to add a new Excel unit operation.

Connect the required feed and product streams. Double-click on the Excel icon to display the tabbed dialog box (see next

section Excel Configuration Dialog Box). This tabbed dialog box is used to specify the name of the Excel file, the name of the worksheet used as

etailed Information D

Before using an Excel unit operation, a user must first create

An Excel file usually contains several worksheets of information. One of these worksheets will be used to exchange data between PRO/II and Excel. This data transfer worksheet has a specific format which is described below in the sData Transfer Sheet. All other sheets in the workbook are ignored by PRO/II and

When PRO/II is installed, an "empty" Excel file (ExcelTemplate.xls) is installewhich can be used as a starting point for developing custom spreadsheets. Note: ExcelTemplate.xls does not perform any calculations. A developer can copy and customize the spreadsheet by adding the requiremacros and/or spreadsheet formulas to calculate thb

fter the spreadsheeAflowsheet using the Excel unit operation:

After starting PRO/II, select File/New from the menu. The PFD Icon palette is displayed.

S


the data transfer area, and the name of the macro to invoke at calculation time.

After configuring the Excel unit operation, click OK to exit the tabbed dialog.

When the flowsheet is solved, PRO/II transfers feed stream information to the spreadsheet, invokes the user-defined macro, and then reads the resulting product stream information back into PRO/II.

When the default text report is generated, PRO/II will write the values of

Limitations

lls back into PRO/II.

the unit operation data arrays to the text report.

The Excel unit operation has the following limitations:

• The Excel macro cannot make any direct function caAll communication with PRO/II is done through the data transfer sheet.

• Use of the PRO/II COM Server functions to access data in the current flowsheet is not supported.

• The Excel spreadsheet is not included in the .prz file in the current version.

Excel Configuration Dialog Box When the user double-clicks on the Excel unit icon, the following tabbed dialog box is displayed

Figure9-1: Excel Unit Tabbed Dialog


The Data Entry Window for the Excel unit operation is used to specify the configuration and general unit operation information. The window is grouped into five tabs.

Spreadsheet Information: contains Excel configuration information.

ed

t name: Enter the name of the spreadsheet file. If no

path is specified, then the Excel file must reside in the same

el file

supply additional data to the Excel spreadsheet. A user can specify s and values for this data.

Double data: This tab contains a double-precision data array similar to the ric "User-added Unit Operation". This

ing calculations; therefore, the values can be used to supply additional data to the Excel spreadsheet. A user can

Display Excel during calculations: If checked, Excel will be display

when invoked by PRO/II. If unchecked, Excel will be executed in 'hidden' mode.

Save Excel file after calculations: If checked, the state of the Excel

spreadsheet will be saved after PRO/II calculations.

Spreadshee

directory as the PRO/II simulation file. Worksheet name: Specify the name of the worksheet in the Exc

which will be used as the transfer area. The default value is "Sheet1".

Macro name: Specify the name of the macro to be invoked by PRO/II during calculations. The default value is "Macro1".

Integer data: This tab contains an integer data array similar to the "Integer Data" grid in the generic "User-added Unit Operation". This data will be transferred to Excel during calculations; therefore, the values can be used to

description Parameter data: This tab contains a double-precision data array similar to the "Real Data" grid in the generic "User-added Unit Operation". This data isaccessible via PRO/II's SPEC/VARY/DEFINE mechanism, which allows Excel spreadsheets to interact with controllers, MVC units, Optimizers, and the Case Study feature. This data will be transferred to Excel during calculations; therefore, the values can be used to supply additional data to the Excel spreadsheet. A user can specify descriptions and values for this data.

"Supplemental Data" grid in the genedata will be transferred to Excel dur

specify descriptions and values for this data.


Thermodynamics: This tab contains a drop-down list box that can be used to select the Thermodynamic set for the unit operation. Notes: This tab contains two text boxes that can be used to specify the unit

t notes.

n and Cell identifiers ssume that the spreadsheet has been configured to support five feed streams

the spreadsheet is modified to increase or decrease l cell for the rows highlighted with an asterisk (*) will

olumn Cell

* Contents

description and the uni Data Transfer Sheet The worksheet used to transfer data between PRO/II and Excel has a specific format as described in the following table. The Columaand five product streams. If

is number, then the actuathchange accordingly. For example, if the spreadsheet is modified to increase the number of feed streams to 6, then the column corresponding to the first product stream will change from column H to column I. CorD2 At calculation time, PRO/II fills this cell with the number of

components in the simulation. F2 Maximum number of feed streams supported by the

spreadsheet. At calculation time, PRO/II reads this value to insure that the number of actual feed streams is less than or equal to the number of columns reserved in the spreadsheet. PRO/II does not change this value. This value must match the number of 'blue' columns used to store feed stream information. If a user customizes the spreadsheet to add one or more blue columns, then this number must be increased to match.

H2 Maximum number of product streams supported by the spreadsheet. At calculation time, PRO/II reads this value to insure that the number of actual product streams is less than or equal to the number of columns reserved in the spreadsheet. PRO/II does not change this value. This value must match the number of 'yellow' columns used to store product stream information. If a user customizes the spreadsheet to add one or more yellow columns, then this number must be increased to match.

J2 Number of rows (starting with row 5) reserved for bulk stream properties. At calculation time, PRO/II reads this number to determine in which row to begin writing stream compositions. PRO/II does not modify this value.

W4 * Number of additional parameters to be included in the text report. At report time, PRO/II reads this value to determine how many additional data items in columns V and W will be


Column r Cell

* Contents o

written to the output report. C5:G24 * At calculation time, PRO/II fills this range of cells with feed

stream information. The number of columns is defined by cell F2; the maximum number of rows is defined by J2.

C25:Gnn * At calculation time, PRO/II fills this range of cells with component rate information of the feed streams. The number of columns is defined by cell F2; the number of rows is defined by D2. The values are expressed in PRO/II internal units-of-measure.

H5:L24 * At calculation time, the spreadsheet must fill in this range of cells with product stream information. The number of columns is defined by cell H2; the maximum number of rows is defined by J2.

H25:Lnn * At calculation time, the spreadsheet must fill this range of cells with component rate information of the product streams. The number of columns is defined by cell H2; the number of rows is

RO/II defined by D2. The values should be expressed in Pinternal units-of-measure.

M, O * At calculation time, PRO/II will write values to columns M and O. Column M will contain the names of the unit operation

nit Operation Data es.

Integer (INT) attributes as defined in the UDefinition (.ini) file; column O will contain the current valuAfter the spreadsheet macro is complete, the updated valuesin column O will be returned back to PRO/II.

P, R ill write values to these columns. Column P will contain the names of the unit operation Parameter (PAR) attributes as defined in the Unit Operation Data Definition (.ini) file; column R will contain the current values. After the spreadsheet macro is complete, the updated values in column R will be returned back to PRO/II. The values

]

* At calculation time, PRO/II w

are expressed in the units-of-measure specified in the [UOMsection of the Data Definition file.

S, U * At calculation time, PRO/II will write values to these columnsColumn S will contain the names of the unit operation double-precision (DBL) attributes as defined in the Unit O

.

peration Data Definition (.ini) file; column U will contain the current

, the updated /II. The values

are expressed in the units-of-measure specified in the [UOM] section of the Data Definition file.

values. After the spreadsheet macro is completevalues in column U will be returned back to PRO

V * Contains the description of the attributes that will be included in the PRO/II default text report. PRO/II does not change these values. The number of descriptions and values included in the PRO/II report is specified by the number in cell W4.


Column * Contor Cell

ents

W * Contains the values calculated by the spreadsheet macros and/or formulas. PRO/II does not change these values. When generating the default text report, PRO/II will include the

s from column V and values from column W in the rt. The number of descriptions and values included in

the report is specified by the number in cell W4.

descriptiontext repo

X, Y * Column X contains the list of unit-of-measure classes. CoY contains the conversion factor between input anunits of measure. Normally this value is not required because PRO/II writes all values to the spreadsheet in the same units-of-measure regardless of the units-of-measure selected in the input file. For details on the unit-of-measure classes, refer the PRO/II 8.0 User-Added Subroutines Users' Guide

lumn d internal

to

Additional Customization

The Excel unit operation in PRO/II provides generic data attributes and GUI apability. It is possible to perform additional customization using the capabilities

s

cof the Modular User-Added Unit Operations. Specifically, the following items can be customized:

• Custom Data attributes names and full support for units-of-measure. • Custom tabbed dialog box. • Custom icon on the PFD palette.

To perform these modifications, refer to the PRO/II 8.0 User-Added SubroutineUsers' Guide.


Expander

General Information

eration may be used to model any isentropic expansion such as in a natural gas processing plant or a steam turbine, etc. An

diabatic expansion efficiency may be applied to the calculations. Rigorous calculations may be performed for both VLE and VLLE systems. Feeds and Products An expander operation may have multiple feed streams, in which case the inlet pressure is assumed to be the lowest feed stream pressure. An expander may have one or more product streams. The product phase condition for operations with one product stream is automatically set by PRO/II. For expanders with two or more product streams, the product phases must be specified in the Expander Product Phases window which is accessed by clicking

The Expander opan expander unita

P

roduct Phases… on the Expander main data entry window.

e product phases include: vapor, liquid, decanted water, heavy liquid, nd mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with

vapor and liquid products and is not allowed when four product streams are specified. Pressure and Work Specifications The outlet conditions for an expander may be selected with the radio buttons provided on the Expander main data entry window. A pressure or work specification is required for every expander. Options are as follows:

• Outlet pressure • Pressure ratio (absolute outlet pressure/absolute inlet pressure) • Pressure drop • Work

y also be defined for convergence of work

Allowabla

A relative tolerance in percent maspecifications. If none is given, a default value of 0.001 percent is used.


Adiabatic Efficiency

0 percent is used (perfect isentropic expansion).

Minimum Outlet Pressure

in the Expander main data entry window. The work will be reset as needed so this minimum pressure is not violated.

rature may be optionally supplied in the

Expander main data entry window to speed the calculations.

The thermodynamic system of methods to be used for expander calculations modynamic System drop-

down list box on the Expander main data entry window.

The isentropic work is adjusted by application of the adiabatic efficiency supplied in the Expander window. When not supplied, a default value of 10

For expanders with work specifications, a minimum outlet pressure may optionally be defined

Outlet Temperature Estimate

An estimate for the outlet tempe


may be selected by choosing a method from the Ther


Flash

eneral Information

temperature and pressure, pressure and nthalpy, etc. The phase equilibrium is determined and the product may be

treams corresponding to the phases. The duty required,

pressure is assumed to be the lowest feed stream pressure.

by PRO/II. For flash nits with two or more product streams, the product phases must be specified in

G

The Flash unit may be used to model any equilibrium calculation where two of the conditions are defined, e.g., eseparated into product sif any, to bring the feed to the final conditions is also reported. Both VLE and VLLE calculations are supported by this unit.

Feeds and Products A flash operation may have multiple feed streams, in which case the inlet

A flash may have one or more product streams. The product phase condition for flash operations with one product stream is automatically set uthe Flash Product Phases window which is accessed by clicking Product Phases… on the Flash main data entry window. Product phases allowable include: vapor, liquid, decanted water/second liquid, and mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with apor and liquid products and is not allowed when four product streams are

n corresponds to a pseudostream with the equilibrium liquid omposition and the optional vapor product from a Bubble Point calculation

First Specification

he temperature, pressure, or pressure drop from feed conditions is supplied by hoosing the appropriate drop-down list box on the Flash main data entry window nd supplying the value in the data entry field provided. Only one entry is

vspecified. Note that for Dew Point and Bubble Point calculations, only two product phases are allowed, vapor and liquid. The optional liquid product from a Dew Point calculatioccorresponds to the equilibrium vapor composition.

Tcaallowed.


Second Specification This specification is used in conjunction with the First Specification given above

define the equilibrium calculation desired. The Second Specification may be tion or a Product Specification as denoted by the radio

buttons on the Flash main data entry window. These two types of specification

sired second specification is chosen with the drop-down list box and the ata entry supplied in the field provided. Options are:

uty: This entry corresponds to an adiabatic (duty defined) flash. When the specification, the pressure is computed.

hen the pressure or pressure drop is supplied as the primary specification, the ),

t pressure is computed when the temperature is upplied as the primary specification. The dew point temperature is determined

pecification. The dew point temperature is determined when the ressure or pressure drop is provided as the primary specification. This option is

d by

ater Dew Point: The dew point pressure for the water portion of the stream is

to

is

toeither a Unit Specifica

are discussed separately below. Unit Specification The ded Pressure Drop or Pressure: These entries are only applicable when the temperature is chosen as the primary specification and correspond to an isothermal (constant temperature and pressure) flash. The Duty required to bring the feed to the specified conditions is calculated by PRO/II. Dtemperature is supplied as the primaryWtemperature is computed. The duty may be positive (heating), negative (coolingor zero (constant enthalpy calculation). Dew Point: The dew poinswhen the pressure or pressure drop is provided as the primary specification. The Duty required to bring the feed to the specified conditions is calculated by PRO/II. Hydrocarbon Dew Point: The dew point pressure for the hydrocarbon portion of the stream is computed when the temperature is supplied as the primary sponly applicable for thermodynamic systems which support a free water phase. The Duty required to bring the feed to the specified conditions is calculatePRO/II. Wcomputed when the temperature is supplied as the primary specification. The dew point temperature is determined when the pressure or pressure drop is provided as the primary specification. This option is only applicable for thermodynamic systems which support a free water phase. The Duty required bring the feed to the specified conditions is calculated by PRO/II.

Bubble Point: The bubble point pressure is computed when the temperature supplied as the primary specification. The bubble point temperature is


determined when the pressure or pressure drop is provided as the primary pecification. The Duty required to bring the feed to the specified conditions is

calculated by PRO/II. Isentropic: A constant entropy flash is calculated from feed conditions to final conditions. The product pressure is computed when temperature is given as the primary specification. The product temperature is given when the pressure or pressure drop is given as the primary specification. The Duty required to bring

e feed to the specified conditions is calculated by PRO/II.

ired

hen this radio button is selected, the pressure is computed when the mperature is provided as the first specification such that a calculated stream rameter meets a specified value. When the pressure or pressure drop is pplied as the first specification, the temperature is computed. The Duty quired to bring the feed to the final conditions is also calculated by PRO/II.

e stream parameter specification is entered by clicking on the hypertext strings d uses the general PRO/II specification format. This format is further described

the SPEC/VARY/DEFINE section of this chapter. The stream parameter ecification must correspond to one of the flash unit products and may be either absolute or relative value. An absolute or relative tolerance value may also be

supplied. Note that a default relative tolerance of 0.02 is used if none is given.

trainment

nt from one phase to another phase is requested in the Flash Drum

s

th Upper Dew Point: The Upper dew point pressure is available only when the temperature is chosen as the primary specification. This option is applicable for Vapor Liquid Equilibrium phases where a retrograde condensation region occurs. This option computes the upper dew point pressure if a temperature above the ritical temperature and below the cricondentherm is supplied. The Duty requc

to bring the feed to the specified conditions is calculated by PRO/II.

oduct Specification Pr Wtepasure Thaninspan

En

EntrainmeEnm

trainment window which is accessed by clicking Entrainment… on the Flash ain data entry window. The From and To phases are defined and the quantity ntrained is supplied as a fraction or percent of the donor phase or as an bsolute rate of material. The entrained material is assumed to have the same

composition as the donor phase. Since entrainment calculations are performed after the flash calculations, the resultant products may be different from the original flash specifications. Multiple entrainments are permitted.

ea


Temperature or Pressure Estimates Estimated temperatures or pressures may be supplied in the data entry boxes at the bottom of the Flash main data entry window. These estimates are optional, with a temp ature estimate relevant when the first specification is the pressure r pressure drop, and a pressure estimate relevant when the first specification is

ot apply to isothermal flash calculations.

main data entry window.

he thermodynamic system of methods to be used for flash calculations may be method from the Thermodynamic System drop-down list

box on the Flash main data entry window.

erothe temperature. They do n Pseudostream Flowrate For Dew and Bubble Point calculations, an optional liquid and vapor product maybe defined which corresponds to the equilibrium liquid or equilibrium vapor, respectively. The rate for this pseudostream may be supplied in the data entry eld provided on the Flash fi

Thermodynamic System Tselected by choosing a


Flash With Solids

General Information

t

section. phase stream from the flash drum section.

d water/second liquid from the solids separator section.

s stream from the flash drum section feeding the solids separator is inte l is not subject to specification by the user. The main data entry window for the Flash with Solids unit is identical to that of the i nit except that no specification of product phases by the user is required. The phases for the product streams are automatically specified by PRO/II and may be reviewed in the Flash Product Phases window accessible via

The Flash with Solids unit models a flash drum unit operation with a solid producstream. If a solids product stream is to be present, you must use the Flash with Solids unit rather than the conventional Flash unit operation. Feeds and Products A Flash with Solids unit may have multiple feed streams, in which case the inlet pressure is assumed to be that of the feed stream with the lowest pressure. A Flash with Solids unit typically has four product streams:

• A vapor phase overhead stream from the flash drum • A liquid• A decante• A solid phase bottom stream from the separator section. The default is

complete separation of the solid from the fluid stream and, hence, there is no required input data for this unit.

The bottom

rna to the Flash with Solids unit and

ord nary Flash u

the Product Phases… butto

n on the Flash main data entry window.

For further instructions on unit and product specifications, see the detailed discussions in the Flash section above (page 226, seq.).


Flowsheet Optimizer

General Information The Flowsheet Optimizer maximizes or minimizes an objective function by

nstraints on minimum and maximum alues on the flowsheet variables. The objective function may be an operational

um recovery or minimum loss, or an economic criterion, it or minimum cost. In order to optimize an economic

function, you must first include a Calculator in the flowsheet in order to define the profit or cost. Then use the Optimizer to minimize or maximize the Calculator result.

Objective Function Either you must choose either Maximize or Minimize as the objective function by selecting the appropriate radio button in the main Optimizer window. Enter the objective function by clicking the linked text string Parameter in the Objective

unction field to make the Parameter window available selecting the unit or

owsheet parameter or a mathematical expression that relates two flowsheet

he optimizer variables (VARYs) are selected by clicking the linked text string

ndow, designate the stream or unit parameter that will be varied, electing from the same choices given above for the Objective Function. For unit

/VARY/DEFINE section of this chapter gives more information on the ARY concept. The tables in that section list the flowsheet variables that may be sed for SPECs and VARYs for flowsheet optimizer units.

varying one or more flowsheet variables while meeting a number of specifications. Optionally, you can place covcriterion, such as maximuch as maximum profs

Fstream parameter to use as the Objective Function. This Parameter window is similar to the SPEC Parameter window, except that there is no entry allowed for the parameter value and tolerance. The Objective Function may be a single flparameters.

Variables TParameter in the Variables grid of the Optimizer main data entry window. In the Parameter wisor stream variables, you must also input minimum and maximum values. The SPECVu


Variable Step Sizes and Limits You may enter limits on the step size for each control variable. Click the linked

in Optimizer window to open the Variable tep Sizes window. You may enter a relative minimum step size and/or absolute

calculations. The alternative step size may be sized on either te basis by selecting the appropriate radio button.

text string default step sizes in the maSmaximum step size per iteration in this window. You may also enter a nondefault step size used to calculate the derivative in this window. The default relative step size depends on the Optimizer scaling option selected (see the section followingtitled Scaling of Optimization Variables). Alternatively, a user-supplied step sizecan be used in the

relative or absolua Specifications SPECifications may be entered for flowsheet parameters other than the control variables. Click Specifications… on the Optimizer main data entry window to bring up the standard Specifications window. Check the Use Specifications box to enable the grid which contains the standard specification linked text. Enter the

arameters for each SPECification by clicking the appropriate text strings in each

strings. See the PEC/VARY/DEFINE section of this chapter for details on the generalized SPEC

NStraint d for flowsheet parameters other than the control

pspecification. Click the linked text string Parameter, to open the Parameter window where you can select the unit or stream parameter to use as the SPEC. The SPEC may be a single flowsheet parameter or a mathematical expression that relates two flowsheet parameters. Next, enter the value and the default tolerance for the SPEC by clicking on the appropriate text Sform. Constraints

s may also be entereCOvariable able to a specified range. Click Constraints… on the i Constraints window from the SPE /V e Use Constraints box to enable the constraint rid. Enter the parameters for each CONStraint by clicking the appropriate text

the CONStraint. The se of this window is analogous to the Parameter window used in selecting the

imum Value, Maximum Value, and the default tolerance alues for the CONStraint are entered by clicking on the appropriate text strings.

s. Constraints limit a varima n Optimizer window to open the C ARY system. Check th

gstrings. Click the hypertext string Parameter to open the Parameter window where you can select the unit or stream parameter to use asuSPEC above. The Minv


Number of Calculation Cycles Several options regarding the operation of the Optimizer may be specified by clicking Options… on the Optimizer main data entry window.

ternatively, you may specify the number of cycles y selecting the appropriate radio button on the Options window.

on

percent.

alue for the overall error in any variable is 10-7. You may enter a ue for the overall error in the corresponding data entry field in the

hange in the box on the Options window.

uence that is affected by e control variable is

updated. Normally, this is determined automatically by the program. However, you must must s nit calculated whenever any of the optimization

s or constraint variables are thermodynamic parameters. Specify the

The PRO/II Optimizer currently supports the use of both Rigorous and Local Thermodynamic Models during the perturbation steps. Specify the

The default for the number of calculation cycles is set by PRO/II as 18 plus the current number of variables. Alb Scaling of Optimization Variables By default, Optimizer scales the optimization variables in the convergence algorithm. This scaling can be suppressed by deselecting the Use Scaling box the Options window. If scaling is deselected, the default value for the derivative step size that appearson the Variable Step Sizes window is increased from 2 percent to 5 Overall Error in any Variable The default vifferent vald

Options window. Minimum Relative Change in Objective Function The default value for the Minimum Relative Change in the Objective Function from one calculational cycle to the next is 0.005. You may enter a different value for the minimum relative c Selecting the Next Unit Calculated After Control Variable is Updated Normally, the first unit operation in the calculation seqthe control variable is the next unit calculated after th

pecify the next uvariablereturn unit by selecting the desired unit from the drop-down list box on the Options window. Type of Thermodynamic Method


thermodynamic model by selecting one of the following options in the Type of Thermodynamic Model drop-down list box: Rigorous

alculation models. This is the default selection.

ocal TP Model

d composition derivatives.

This option specifies that PRO/II will use rigorous thermodynamic c LThis option specifies that PRO/II will generate local K-value models for T and P derivatives. Local TPx Model This option specifies that PRO/II will generate local K-value models for T, P, anLiquid Local TPxy Model This option specifies that PRO/II will generate local K-value models for T, P, and Liquid and Vapor composition derivatives. Advanced Options Click Advanced Options.. to specify additional options for the Optimizer.

ou are unsure how these features may apply to your simulation, consult SIMSCI Technical Support or refer to the PRO/II Reference Manual.

option Specified Number of Trials in the drop-

The Optimizer Advanced Options are intended for experienced users of PRO/II. If y

Special Line Search Logic This option enables a line search mode method for the optimization calculations.

y default, this feature is Off. TheBdown list box enables this feature.

hen this feature is enabled, you may specify the maximum number of lineWsearch trials for any one optimizer cycle. The number must be a positive integer no greater than 20. Number of Independent Variables to Eliminate You may specify the number of independent variables to be eliminated during thesolution of the optimizer calculations.


Start Broyden Updating at Cycle You may specify the optimization cycle at which Broyden Updating will begin. By default, this option is Off. Specify a positive integer greater than 1 to enable this

ature.

wn list to produce an nalysis printout of the derivative step sizes for each optimizer cycle; in addition,

imit Optimization Step Sizes

). When enabled, this option limits the step izes taken by the optimizer to 30, 60, and 90 percent of the upper or lower

ion cycles 1, 2, and 3, respectively. This is intended as a afety feature to prevent the Optimizer from moving too far, particularly when the

s

utput File Once the flowsheet optimization has converged and the appropriate operating conditions have been determined, the shadow prices or Lagrange multipliers can be used to assess the sensitivity of the objective function to the specifications,

r bounds, a negative shadow price indicates that

dow price indicates that the lution By default, printout of these values is

ontains the IDs of the ariables, specifications, and constraints, along with their corresponding shadow

prices as part of the standard output report.

he All option produces a separate output report with the same file name as the input file (with an .shd extension) containing a detailed summary of the final Optimizer solution. This summary includes the values of the objective function, all variables, specifications, and constraints, along with the shadow prices for all

ctive bounds and constraints.

fe Derivative Analysis By default, this option is Off. Select On in the drop-doaa modified perturbation step size will be suggested, if appropriate. L By default, this option is Enabled (Yes sbounds during optimizatsderivatives are inaccurate. Selecting No in the drop-down list box disables thifeature. Separate Shadow Price O

constraints and bounds. For maximization problems, a positive shadow price indicates that the constraintis being pushed against its uppethe lower bound is still active, and a zero shaconstraint does not affect the sodisabled (the None option in the Separate Shadow Price Output File drop-down list box). The Brief option produces a separate output report with the same file name as the input file (with an .shd extension). This report cv

T

a


Complete technical details may be found under the topic Flowsheet Solution Algorithms in the PRO/II Reference Manual.

rint Results for Flowsheet Optimizer

P

The default is to suppress printing of a convergence report. Click Print Options… Optimizer window to open the Print Options window. Select the

esired printout level from a drop-down list that includes the print levels History, Brief, and All.

ist

hat l of printout is greater than or equal to the derivative printout option.

ox to generate a plot of the

ence diagnostics

on the main d

By default, no intermediate printout is produced. Print-out levels for intermediate printout of derivative and/or variable values can be selected from a drop-down lwhich includes the print levels None, Print after each cycle, or Print after the final cycle. The program limits the options for the variable printout selection such tthe leve

Select the Include Convergence Plots check bconverg .


Heat Ex

changer, LNG

General Informatio

He g late xcha f heat between any number t and cold streams. The exchanger is divided into cells representing the

cross-flow elements. Cells are designated as Hot, where the streams are cooled or as Cold where they are heated. The unit mu ain at least one hot cell and one cold cell.

ber initially defined o the LNG Heat Exch r Configuration at h unit placed on the PFD. Cells may be deleted in the main LNG Heat Exchanger window.

Feeds and

m ne e fe ams. If multiple feed streamshe mixed feed is flashed at the lowest feed stream pressure.

has from a cell may be separated into st containing one or more phase. The allowable product stream phases are vapor, liquid, decanted water and mixed (vapor+ . A mixed phas uct is not allowed wapor or a liquid product. The decanted water product is also used as the second

liquid produ ith us VLLE calcu s.

l has on uct st locate

n The LNGof hondividual

er simu s the e nge oat Exchan

ist cont

The numwindow thadded or

of cells is appears w

nis first

angeen the

Products

Each celldefined, t

ay have o or mor ed stre are

A multip e product reams

liquid) e prod ith a v

ct phase w rigoro lation

If a cel more than e prod ream, the phases must be al d to the streams in th P windo his w is acce ia the Cell e Product hases w. T indow ssed vData… button in the main LNG Heat Exchanger window, then via the Product Phases… b n en L at E ger Cell Data wind

anc ations

ny cell may er let temperature sp ation. However, at least one m nspe The uct stre rom all

nspecified cells leave the exchanger at the same temperature.

utton in the ow op NG He xchan ow. Perform

e Specific

A have eithcell must re

a duty or an outain u

ecificams fcified. prod

u


Cell Data

r r ea l def o zer ssure drop values he LNG Heat Exchanger Cell Data window. The thermodynamic

sed for the calcul change

ones Analysis

lysis may be requested in the LNG Heat Exchanger Zones Analysis

The pressuentered in t

e drop fo ch cel aults t o. Pre are

system uwindow.

ations for an individual cell may also be d in this

Z Zones Anawindow accessible via the Zones Analysis… button on the main data entry

w. This feature allo ernal temperatu ssove d pinch s to ied by dividing the exchanger into a number of zones. Warnings are

o r pinch points are found.

s Analysis calculations are normally performed when the exchanger is d. Howeve ger i

e e is a t tim

one Analysis will always be performed at calculation time if required by Controller specifications LNG exch er.

rint Options

windobe identif

ws int re cro rs an point

issued if cr The Zone

ssovers o

calculatesaved by p

r, if the exchanrforming th

s in a recyt outpu

cle, compe.

utation time may be analys

Z on the heat ang

P The Print Options window is opened via the Print Options… button on the main ata entry window. A number of different Y versus X plots may be generated for

temperature, duty and UA. The options are:

• Temperature vs. Duty (default) • UA vs. Duty (default) • ∆T vs. Temperature (default) • ∆T vs. Duty • UA vs. ∆T • Duty vs. Temperature.


he thermodynamic system of methods to be used for LNGHX calculations may be selected by choosing a method from the Thermodynamic System drop-down list box on the LNG Heat Exchanger main data entry window.

l cell window) overrides this

ermodynamic system for specific cells.

d

T

Note: The thermodynamic system used for the calculations for an individua(specified in the LNG Heat Exchanger Cell data th


Heat Exchanger, Rigorous

eneral Information

Rigorous Heat Exchanger simulates the operation of an existing heat

resistance is calculated.

Feeds and Products

ach side of the exchanger may have one or more feed streams. If multiple feed

m the exchanger may be separated into streams or more phase. The allowable product stream phases are vapor,

r and mixed (vapor+liquid). A mixed phase product is not used

ide has more than one product stream, the phases must be allocated to

G

The exchanger. The geometry of the unit has to be defined and the unit is rated to determine the duty, exit temperatures, and pressure drops. The exchanger duty, or one of the exit temperatures, may be defined. In this case, the fouling

Estreams are defined, the mixed feed is flashed at the lowest feed stream pressure.

multiphase product froAcontaining onequid, decanted wateli

allowed with a vapor or a liquid product. The decanted water product is alsoas the second liquid product phase with rigorous VLLE calculations. f either sIthe streams in the Product Phases window accessed via the Product Phasesbutton in the Rigorous Heat Exchanger–Feeds and Products Data window.

…

on type is selected from a drop-down list in the Rigorous Heat ndow. The available options are:

erred with the defined area and fouling factors. he default.

ned

Calculation Type The calculati

xchanger wiE Rating: Determine the heat transfT Fixed Duty: Determine the fouling factors and exit temperatures from the defiduty.


Tub uling factors, and shell exit outlet temperature.

hell Outlet Temperature: Determine the duty, fouling factors, and tube efined shell outlet temperature. If the selected g, a value must be supplied for the duty or exit

changers may be attached to any tray of a column for which a duty is defined, ther heating or cooling. To attach an exchanger to a column, double-click

e Outlet Temperature: Determine the duty, fo temperature from the defined tube

Sexit temperature from the dalculation type is not Ratinc

temperature as appropriate. Exchangers Attached to Columns ExeiAttach to Column… for the shell or tube side on the Rigorous Heat Exchanger–Feed and Products Data window and supply the appropriate information in the window provided. A column internal stream is considered as one side of the exchanger and a process stream is defined for the other side. Attached exchangers may be used to represent the condenser or reboiler for the column, a pumparound, or side heater/cooler. For side heaters and coolers, the column stream may be the vapor or liquid from the tray to which the exchanger is attached, the vapor from the tray below, or the liquid from the tray above. If the Calculation Type does not fix the exchanger duty or one of the outlet temperatures, the exchanger duty will be fixed by the column heater or cooler. It is generally best to allow the column operation to determine the duty required to meet the defined performance. If the duty is fixed by an exchanger specification, it is considered a “fixed” duty for the column calculations. Overall Configuration The overall configuration is defined in the Rigorous Heat Exchanger window by entering one or more of the configuration parameters:

• Number of Tubes/Shell • Area/Shell • Shell Inside Diameter

A value for at least one of these parameters must be supplied. If any of these parameters is missing, it will be calculated from the others.


Configuration Data The configuration details are defined in the Rigorous Heat Exchanger Configuration Data window accessible via Configuration… on the main data entry window. All data in this window have default values:

umber of Shells in Series: This is the number of identical shells connected in des are considered to be piped in series.

n

allowed, but are not

The exchanger orientation is selected from the drop-down list as

st as

EMA Type: The three characters for the TEMA type (front, shell and rear of the

eat Exchanger Tube

Nseries in the unit. Both shell and tube si

he default is 1 shell. T Number of Shells in Parallel: This is the number of identical shells connected iparallel in the unit. Both shell and tube sides are considered to be piped in parallel. The default is 1 shell. Number of Tube Passes/Shell: This can be any integer value between 1 and 6. The default is 2. Odd numbered values are1

recommended. Orientation:either Horizontal or Vertical. The default is Horizontal. Configuration: The direction of fluid flow is selected from the drop-down lieither Countercurrent or Cocurrent. The default is Countercurrent. Texchanger) are selected separately from drop-down lists. The default is AES. Tube Data Details of the exchanger tubes are entered in the Rigorous HData window which is accessed via Tubes… on the main data entry window. All

r

ults to 0.75 inches (19.05 m).

Wall Thickness BWG

tube data have default values. Length: The nominal tube length includes the thickness of both tube-sheets. FoU-tubes, it includes the thickness of the tubesheet and the last baffle. The lengthdefaults to 20 ft (6.1 m). Outside Diameter: The tube outside diameter defam Thickness: The tube thickness may be defined as:

Inside Diameter


Bare tubes default to an inside diameter of 0.58402 inches (14.834 mm). Finned n inside diameter of 0.49598 inches (12.573 mm).

Deg e– 45 Degrees.

may

be entered di

finned and bare surface areas. A value entered here, overrides the calculated

is is the number of fins per inch of tube length. (Default is 19). Thickness: The fin thickness defaults to a value in inches equal to 0.5/(Fins per

ch). Height Above Root: The fin height above the root defaults to a value equal to

ube Outside Diameter - Root Diameter)/2.

oot Diameter: The root diameter is the tube diameter at the base of the fins s to 0.625 inches.

Baffle Data

etails of the exchanger baffles are entered in the Rigorous Heat Exchanger

tubes default to a Pitch: The center-to-center distance between tubes defaults to 1.0 inch (25.4 mm). Pattern: The tube pattern is selected from the drop-down list. The options are Triangular–30 Degrees, Square–90 Degrees (default), Rotated Triangular–60

rees, and Rotated Squar Sheet Thickness: The tubesheet thickness is calculated if it is not supplied.

Fin Data

The default is not to have finned tubes. If fins are specified, the surface arearectly or calculated from the fin data.

Extended Surface Area: This is the total surface area of the tubes including the

area.

ins/Inch: ThF

In

(T

Rand it default

DBaffle Data window accessible via Baffles… on the main data entry window. All affle data have default values.

Baffle Type: The type is selected from the drop-down list. The options are No Baffles, Single (default), Single Baffles - No Tubes in Window and Double.

affle Geometry Data: The baffle cut is the height of the window divided by the

b

Bshell inside diameter and it defaults to 0.2. Alternatively, the Net Free Area Ratio may be entered instead. This is the area of the window divided by the cross-ectional area of the shell. s


Center Spacing: If a value is not supplied, the baffle center-to-center spacing is calculated by default to be 0.2*(Shell Inside Diameter). Any value entered will be

will be

let Spacing: This is the center-to-center spacing between the tubesheet and

defined, it defaults to 5 inches (133 mm) for bare tubes or 3 inches (88 mm) for finned tubes. Out S spacing between the tubesheet and the tl not supplied, it is calculated to meet the cente sp defined, it defaults to 5 inches (133 mm) for e Thickn s to 0.1875

ilm Coefficient Data are entered in the Rigorous Heat Exchanger Film

ignored if both Inlet Spacing and Outlet Spacing are defined and the value calculated to provide even spacing. Inthe inlet baffle. If the inlet spacing is not supplied, it is calculated to meet the center spacing or, if no center spacing is

let pacing: This is the center-to-center ou et baffle. If the outlet spacing is

r acing or, if no center spacing isbar tubes or 3 inches (88 mm) for finned tubes.

ess: If a value is not supplied, the baffle thickness defaultinches (4.763 mm). Number of Sealing Strips: This is the number of pairs of sealing strips per cross-flow pass. It defaults to zero. Film Coefficient Data FCoefficient Data window accessible via Film Coefficients… on the main data entry window. These data provide adjustment factors and override values for the heat transfer parameters.

efficient

Overall U-value Scale Factor: This is a multiplier which is applied to all calculated heat transfer coefficients. It can be used in order to match plant data more closely. It defaults to 1.0. Tubeside and Shellside Data The following items have separate entries for each side of the heat exchanger.

e

for

Overall U-value Estimate: This is the initial value for the heat transfer coused in the calculation. The default is 50 Btu/hr·ft2·°F (244.1 kCal/hr·m2 ·°C or1021.9 kJ/hr·m2 ·K).

Scale Factor: This is a multiplier which is applied to the film coefficient for thspecified side of the exchanger. It defaults to 1.0.

Coefficient: If a value is entered, it overrides the calculated film coefficientthe specified side.


Fouling Resistance: Thermal fouling resistance defaults to 0.002 ft2 ·hr·°F(0.00041 m2 ·hr·°C/kCal or 0.00010 m2 ·hr·K/kJ). If a duty or exit

/Btu temperature is

specified, the fouling will be calculated.

Fouling Thickness: The thickness of the fouling layer may be entered to model its effect on the pressure drop. The default value is zero. Material Data Tube and shell material property data are entered in the Rigorous Heat

Exchanger Material Data window accessible via Materials… on the main data entry window.

he default material is carbon steel. A different material may be selected from a drop-down list which shows the materials in the library.

Individual properties of the selected material may be overridden. Alternatively, the user may select User-added Material from the list and then supply the name and properties of the material. The list of materials in the library is tabulated below.

T

Heat Exchanger Materials of Construction Material Density Conductivity

Description Label lb/ft3 kkg/m3

/m.K

Btu/hr.ft.°F kCal/hr.m.°C W

Carbon Steel

CARB STL 490.8 7862 30.0 44.6 51.9

Carbon-moly Steel 0.1C, 0.5Mo

CARB MLY 493.2 7900 29.0 43.2 50.2

Chrome-moly Steel .0Cr,

CHRM MLY 490.1 7851 27.0 40.2 46.7

10.5Mo Low Chrome Steel 2.25Cr,

.0Mo

LOW CHRM

487.0 7801 25.0 37.2 43.3

1

Medium Chrome

teel 5.0Cr,

MED CHRM

480.7

S1.0Mo

7700 21.0 31.2 36.3

Straight Chrome Steel 12Cr

STR CHRM

487.0 7801 14.0 20.8 24.2

30StSt

4 304 S.S. 501.1 8027 9.3 13.8 16.1 ainless eel 18Cr,

8Ni 310 310 S.S. 501.1 8027 7.8 11.6 13.5


Stainless teel 25Cr,

i

S20N

31Stainless

6

Steel 17Cr, Ni

316 S.S. 501.1 8027 9.4 14.0 16.3

12 321 Stainless Steel 18Cr, 10Ni

321 S.S. 494.2 7916 9.2 13.7 15.9

Aluminum A1060H14 170.0 2723 128.3 190.9 222.1 1060 H14 Aluminum 1100 Annealed

A1100 AN 169.3 2712 128.3 190.9 222.1

Aluminum A3003H14 171.1 2741 111.0 165.2 192.1 3003 H14 Annealed Aluminum A3003H25 171.1 2741 111.0 3003 H25

165.2 193.1

Annealed Aluminum 6061 T4 Tempered

A6061 T4 169.3 2712 95.0 141.4 164.4

Aluminum 6061 T6 Tempered

A6061 T6 169.3 2712 95.0 141.4 164.4

Copper COPPER 556.4 8913 225.0 334.2 389.4 Arsenical Copper AS

COPPER 560.0 8970 187.0 278.3 323.6

Copper Nickel 90/10

CUNI9010 559.0 8954 26.0 38.7 45.0

Copper Nickel 80/20

CUNI8020 558.5 8946 22.0 32.7 38.1

Copper CUNI7030 585.0 9371 17.0 25.3 29.4 Nickel 70.30 Copper Nickel 60/40

CUNI6040 554.7 8885 12.9 19.2 22.3

Red Brass 85Cu, 15Zn

RED BRAS 546.0 8746 92.0 136.9 159.2

Admiralty ADMRALTY 531.0 8506 64.0 95.2 110.8


Brass 71Cr, 28Zn, 1Sn Commercial

rass 55Cu, COM BRAS 529.0 8474 67

B34Zn

.0 99.7 116.0

Muntz Metal 60Cu, 40Zn

MUNTZ 524.0 8394 71.0 105.7 122.9

Aluminum Bronze

AL BRONZ 510.0 81

93Cu, 5Al

69 48.0 71.4 83.1

Aluminum 86.3 100.4 AL BRASS 520.0 8330 58.0 Brass 78Cu, 2Al Nickel Annealed

NICKEL 556.4 8913 45.2 67.3 78.2

LNi

ow Carbon L CRB NI 554.7 8885 3ckel

5.0 52.1 60.6

Annealed Monel Nickel 70Ni, 30Cu

MONEL NI 551.2 8829 14.5 21.6 25.1

I76Ni, 16Cr, nconel 600 INCNL600 525.3 8414 8.7 12.9 15.0

8Fe Titanium Grade 2

TITANIUM 281.6 4511 9.5 14.1 16.4

Pressure Drop Data Pressure drop data are entered in the Rigorous Heat Exchanger Pressure Drop Data window accessible via Pressure Drop… on the main data entry window. These data provide adjustment factors and override calculated values for the ressure drops. All data may be defaulted.

A

P Scale Factor: This is a multiplier which is applied to the pressure drop for the specified side of the exchanger. It defaults to 1.0.

p By default the pressure drops are calculated for each side of the exchanger.scale factor may be applied to the calculated value for either side or the pressure drops may be overridden. D


P / Shell: If a value is entered, the pressure drop per shell overrides the

ll

Print Options Additional output reports are selected in the Rigorous Heat Exchanger Print

Dcalculated pressure drop for the specified side. DP / Unit: If a value is entered, the pressure drop for the exchanger unit overrides the calculated pressure drop for the specified side. Shellside Pressure Drop Method: The method may be selected from Be(default) for the Bell-Delaware method or Stream for the stream analysis technique.

Options window accessible via Print Options… on the main data entry window.

xtended: By default, a standard TEMA data sheet is produced for the exchanger. Checking the Extended check box produces an additional data sheet

ith information about stream properties, heat exchanger configuration and ydrodynamics.

Zones check box produces an additional table showing the

d zone bo ries used to calculate the duty-averaged log-mean-re differe ce.

lot: Chec Zones Plot eck box produces a plot showing the one boundaries used to c ulate the duty-averaged log-mean-

e difference.

ozzle Data

s can be overridden in the Rigorous Heat

E

wh

Zones: Checking the phase an undatemperatu n Zones P king the chphase and z

mperaturalc

te

N The default nozzle type and sizeEw

xchanger Nozzle Data window accessible via Nozzles… on the main data entry

Use Tube Side Nozzle or Use Shell Side Nozzle: If either check box is nchecked, the nozzle pressure drop will not be calculated for that side of the

exchanger.

side Diameter: The calculated diameters may be overridden. The Inlet and/or

indow. The default is to use conventional nozzles with calculated inside diameters. Nozzle data only affects the calculated pressure drop in the exchanger.

u

InOutlet diameter may be entered.


Use Annular Shell Side Nozzles: If this box is checked, the pressure drop will be calculated for annular rather than conventional nozzles. In this case, click Enter Data… to open zzle Data window to enter the nozzle details. The required data are:

nd o tlet annular passage lengths nd o tlet groove areas nd o tlet annular-shell wall clearances

ic

ynamic system of methods to be used for each side of the rigorous er may be selected by c sing a method from the Thermodynamic

drop-down list box on the Rig us Heat Exchanger main data entry

the Annular No

• Inlet a• Inlet a

uu

• Inlet a u Thermodynam System The thermod

hangheat exc

hooSystemwindow.

oro


Heat Exchanger, Simple

General Information The Simple Heat Exchanger may be used to heat or cool a single process stream, exchange heat between two process streams, or exchange heat between a process stream and a utility stream. Rigorous calculations may be performed for VLLE systems. It is also possible to attach an exchanger to any

ay of a distillation column and exchange heat between a process stream and a , either liquid or vapor.

or reference, streams and products are grouped according to the side of the ed

t ressure.

he product from each side of an exchanger may be phase separated as desired ,

ms only). The “water” product stream d liquid phase for systems in which

rigo s onsidered.

eed an s are accessed via the Heat Exchanger Process

trcolumn internal stream Feeds and Products Fexchanger as “hot” or “cold”, where the feed stream(s) on the hot side are cooland the feed stream(s) on the cold side are heated. Multiple process feed streams are permitted, with the lowest stream pressure used as the inlep Tinto multiple product streams, where products may be liquid, vapor, mixed phaseand decanted water (hydrocarbon syste

ay also be used to represent a seconmrou modeling of VLLE thermodynamics is c

F d product streamStreams window which is opened by clicking Process Stream… o

xchanger main data entry window. The product phase condition fon the Heat

r units with atically set by PRO/II. For simple heat exchangers

s from a given side, the product phases must be

Eone product stream is autom

ith two or more product streamwspecified in the Product Phases window accessible by clicking Product Phases… on the Heat Exchanger Process Streams window.

roduct phases allowable include: vapor, liPanva

quid, decanted water, heavy liquid, d mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with por and liquid products and is not allowed when four product streams are

specified.


Utility Streams

o simple heat exchangers with one process side, a hot or cold utility stream for the specified heat transfer is always

F rmay be defined. The required utility ratecHomputed. Utility streams may be specified by clicking Utility Stream… on the

t Exchanger Hot Side Utility window.

ndensed at its satu

onfiguration Data

onfiguration data are supplied in the Heat Exchanger Configuration Data

eat Exchanger main data entry window to access the appropriate hot or cold utility window. Cold utility streams are supplied in the Heat Exchanger Cold Side Utility window. Options are: Water: Temperature in and out must be supplied. Sensible heat transfer only. Air: Temperature in and out must be supplied. Sensible heat transfer only. Refrigerant: A designated component is vaporized at its saturation pressure or temperature. Latent heat transfer only.

ot utility streams are supplied in the HeaHOptions are: Steam: Steam is co ration temperature or pressure. Latent heat transfer only. Heating Medium: A designated component is condensed at its saturation temperature or pressure. Latent heat transfer only. C Cwindow accessed by clicking Configuration… on the main data entry window. These data only apply to exchangers with two sides and are optional for all exchangers for which a Performance Specification is provided (see below). Flow Direction: Countercurrent or cocurrent. Default is countercurrent. Tube and Shell Passes: When supplied, an N -2N configuration is always

ssumed, where the number of shell passes is twice the number of tube passes. he “FT” LMTD correction factor is computed, based on a correlation for N -2N xchangers. Default is two tube and one shell pass, i.e., true countercurrent flow.

actor for the exchanger. Note that this entry is nd Shell Passes.

aTe FT Factor: The LMTD correction f

utually exclusive with the Tube am


Performance Specifications Exchanger performance is specified in the Heat Exchanger Specifications window accessed via Specifications… on the main data entry window. Exchanger performance may be specified in a varity of ways:

ature out for hot or cold process fluid. Temperature pproach (Two-sided exchangers only)

• Minimum Internal Temperature Approach (MITA): Minimum internal

: The liquid fraction for the hot or cold side exit uid where 0.0 indicates bubble point and 1.0 indicates dew point conditions.

s of superheat (above the dew point) for the

w the bubble point) for

ry

to satisfy the U*Area and no other performance specifications are

ed to satisfy the U*Area and no other performance

nd

at ansfer otherwise determined by a performance specification if necessary. This

Outlet Temperature: TemperA

• HOCO: Hot out minus cold out. • HOCI: Hot out minus cold in. • HICO: Hot in minus cold out. • Minimum: Smaller of HOCI and HICO.

approach based on a zones analysis for the exchanger. Duty: Overall heat transfer duty for the exchanger. Outlet Stream Liquid Fractionfl

egrees of Superheat: The degreeDhot or cold side exit fluid.

egrees of Subcooling: The degrees of subcooling (beloDthe hot or cold side exit fluid. Overall Heat Transfer Coefficient (U): The area is calculated from this entwhen not supplied. When both U and Area are given, the heat transfer is omputedc

allowed for the exchanger. Exchanger Area: The overall heat transfer coefficient for the exchanger is calculated from this entry when not supplied. When both U and Area are given,

e heat transfer is computthspecifications are allowed for the exchanger. Lumped UA Specification: The product of overall heat transfer coefficient aexchanger area may be supplied directly. Individual U and Area Specification: Individual values for the overall heat transfer coefficient and exchanger area may be supplied directly.

aximum U *Area: A maximum U*Area may be supplied to limit the heMtr


specification is not allowed when either a Lumped UA specification or the xchanger overall U and Area have been supplied individually. e

Zones Analysis Zones analysis is requested by clicking Zones Analysis… on the main data entry window. The duty-weighted LMTD may be computed for exchangers in which phase changes occur by dividing the exchanger into at least five zones of equal duty. More zones may be requested as desired. Zones analysis is automaperformed for exchangers with MITA specifications. For other types of

tically

pecifications, the zones analysis may be performed during exchanger , as requested. Warning

essages are given for temperature crossovers.

y tray of a column for which a duty is defined,

scalculations or at the completion of all calculationsm Exchangers Attached to Columns Exchangers may be attached to aneither cooling or heating. To attach an exchanger to a column, click Attach to Column… on the main data entry window and supply the appropriate information

the window provided.

internal column stream is considered as one side of the exchanger; a process ream or utility stream defined for the exchanger is the other side. Note that for ility streams, the duty must be determined by the column calculations.

tached exchangers may be used to represent the condenser or reboiler for the lumn, a pumparound cooler, or a side heater or cooler. For side heaters and olers, the column stream may be: the vapor or liquid from the tray to which the changer is attached, the vapor from the tray below the tray to which the changer is attached, or the liquid from the tray above the tray to which the changer is attached.

is generally best to let the exchanger duty be determined in the column eration to meet a desired separation criterion. If the duty is defined by a rformance specification for the exchanger, it is considered a “fixed” duty for lumn calculations.

ermodynamic System

e thermodynamic system of methods to be used for each side of the simple anger may be selected by choosing a method from the Thermodynamic

System drop-down list box on the Heat Exchanger main data entry window.

in Anstut Atcocoexexex It oppeco Th Thheat exch


Heating/Cooling Curves

General Information

g curves for ,

urves may be generated by using equal temperature increments or equal duty crements. Additional points are included when phase boundaries are crossed.

eans es

desired temperature or duty ranges for the curves.

hermal properties, additional properties may be operties include physical, critical,

The Heating/Cooling Curve utility module develops heating or coolinany stream in the flowsheet. The tables are a composite of equilibrium flashesand present the data typically required for the design of heat transfer equipment. Cin For the Flash, Heat Exchanger, and Column unit operations, a convenient mis provided to retrieve the streams involved in heat transfer and generate curvbased on the actual duties for the units. For other flowsheet streams, you may define the In addition to the standard t

quested for the reports. These prrethermodynamic, transport, and petroleum properties. Heating/Cooling Curves for Flowsheet Streams A drop-down list box is used to retrieve flowsheet streams for which curves are desired in the Heating/Cooling Curves main data entry window. After selecting astream, click Enter Data to open the Heating/Cooling Curve for Flowsheet Stream window. This window is used to select the boundaries for the curves, type of curves, number of points for the curves, and the report options. A combination of two specifications is used to define the type and boundaries for

e curves. Curves may be at equal temperature increments, equal duty oint or bubble point curve for the fluid. Dew and

ned pressures or at defined temperatures. t

onditions. The number of points for the curves may be selected on this form by replacing the default number of 11. When phase boundaries are crossed, additional points are added to the report which represent the transition points.

thincrements, or may be the dew pubble points may be calculated at defib

When the temperature and pressure ranges are defined for a curve, the resultanpoints are always at equal temperature/pressure intervals. When a temperature, pressure, or duty increment is defined for a curve, the starting point is always aken to be the current stream ct


A check box may be used to select printout of liquid activity coefficients, vapor gacity coefficients, and Poynting correction factors for thermodynamic systems

ity coefficients. The equilibrium K-values for the components may also be selected for printout with a check box.

fubased on liquid activ

Heating/Cooling Curves for Unit Operations A drop-down list box is provided for selection of unit operations for which curvesare desired in the Heating/Cooling Curves main data entry window. Units for which curves may be requested include the Flash, Heat Exchanger, and Column. To select the options for the unit:

Click Enter Data adjacent to the unit name. The appropriate window for the unit operation appears for selection of curve

r may specify printout options for liquid activity s, and Poynting corrections for thermodynamic

systems based on liquid activity coefficients. The equilibrium K-values for the

heck boxes and radio buttons are used on the Heating/Cooling Curves for ash Drum window to select the options for the curves. The temperature and essure range is predefined as the inlet and outlet conditions for the Flash.

e curves may be defined as isothermal, i.e., at equal temperature increments, as adiabatic, i.e., at equal duty increments. The number of points for the rves may be selected on this form by replacing the default number of 11. When ase boundaries are crossed, additional points are added to the report which present the transition points.

Heating/Cooling Curves for Heat Exchangers

heck boxes and radio buttons are used on the Heating/Cooling Curves for Heat changers window to select the options for the curves. The temperature and

essure range is predefined as the inlet and outlet conditions for each side of e Heat Exchanger.

isothermal, i.e., at equal temperature increments, ments. The number of points for the

may be selected on this form by replacing the default number of 11. When hase boundaries are crossed, additional points are added to the report which

represent the transition points.

options. In each case, the usecoefficients, vapor fugacitie

components may also be selected for printout. Heating/Cooling Curves for Flash Units

CFlpr Thorcuphre

CExprth The curves may be defined as or as adiabatic, i.e., at equal duty increcpurves


Heating/Cooling Curves for Columns

oling

o umparound streams to simulate the effects of pumping.

rm by replacing e default number of 11. When phase boundaries are crossed, additional points

Column streams are selected in a drop-down list box on the Heating/CoCurves for Column Internal Streams window. Streams available include the condenser and reboiler feeds, and feeds to trays with duties such as side reboilers and pumparound coolers. The curves may be defined as isothermal, i.e., at equal temperature and pressure increments, or as adiabatic, i.e., at equal enthalpy and pressure increments. The temperature and duty ranges are predefined as the unit operating conditions. A pressure range may be added tp The number of points for the curves may be selected on this fothare added to the report which represent the transition points. Standard Reports Standard reports include the data in the table below: Total Feed Vapor Liquid

Temperature X Pressure X Molar Flow

X X

Enthalpy X X

X

Weight Flow

X X

Molar Entropy

X X X

Additional Stream Properties These properties are requested by clicking Report Additional Stream Properties

ected for the eating/Cooling Curve.

on the Heating/Cooling Curve main data entry window. These properties are reported in addition to the standard reports for all curves selH


Additional Stream Properties Reports Additional reports include the data tabulated below: Total Feed Vapor Liquid

Molecular Weight X X Actual Density X X Volumetric Flow X X Compressibility Factor

X

Specific Gravity X Flowing Entropy X X X Enthalpy (unit basis) X X X Latent Heat X X Heat Capacity X X Viscosity X X Thermal Conductivity

X X

Surface Tension X Critical Temperature X X Critical Pressure X X Critical Compressibility

X X

API Gravity X X Watson K Factor X X Molar Average

t X X

Boiling Poin Plots

and Plotting, for more information about generating raphical plots of Heating/Cooling Curve results.


on the Heating/Cooling Curves main ata entry window.

Refer to Chapter 11, Printingg

You may select the thermodynamic system of methods to be used for heating/cooling curves calculations by choosing a method from the Thermodynamic System drop-down list box d


Mixer

General Information The Mixer unit combines two or more streams into a single product stream. The outlet pressure may be specified if desired. The outlet temperature and phase condition are always determined with an adiabatic flash from the feed conditions. This unit supports both VLE and VLLE calculations.

he inlet pressure is assumed to be the lowest feed pressure. There is no limit on the number of feed streams to a mixer.

e

• Pressure drop from feed conditions, or • Outlet pressure

If neither entry is supplied, the default is a pressure drop of zero.

ynamic System

The thermodynamic system of methods to be used for mixer calculations may be selected by choosing a method from the Thermodynamic System drop-down list box on the Mixer main data entry window.

Feeds and Products T

Only one product stream is allowed for a mixer. PRO/II automatically sets thtemperature and phase condition for the product. If phase separation of the product is desired, a separate flash unit must be used for this purpose. Outlet Pressure Specification The pressure specification for the mixer product is selected with the appropriate radio button on the Mixer window:

Thermod


Multivariable Controller

General Information The Multivariable Controller (MVC) is an expanded form of the Controller andsimulates two or more feedback process controllers. The MVC is capable oadjusting an unlimited number of upstream variables to reach the same number of specified objectives. Each of the SPECifications may be a stream flowrate or property, a unit operating condition, or a Calculator result. The control variamay be stream and unit operation conditions, thermodynamic parameteCalculator results that are otherwise at fixed values in the flowsheet. For the Multivariable Controller, the number of variables must equal the numof specifications. The linked text above the Specifications grid in the Multivariable Controller main data entry window indicates whether the current num

f

bles rs, and

ber

ber of pecifications equals the number of variables. If they are unequal, the hypertext

will appear in red.

Establish the SPECifications by clicking the appropriate linked text in the

e

Variables

.

ay be used for SPECs and VARYs for multivariable controller nits.

sstring “does not equal” Specifications

Specification grid of the Multivariable Controller window. MVC SPECifications areestablished in the same manner as for the simple Controller SPECifications. Sethe SPEC/VARY/DEFINE section of this chapter for further details on the generalized SPEC form.

Establish the control variables (VARYs) by clicking the linked text string Parameter in the Variable grid of the Multivariable Controller window. MVC VARYs are established in exactly the same manner as simple Controller VARYsSee the SPEC/VARY/DEFINE section of this chapter for more information on theVARY concept. Tables are also given in that section listing the flowsheet variables that mu


Var l You a riable, if desired. Variable limits and teps sizes for MVC are established in exactly the same manner as simple

he Variables field in the ultivariable Controller window. After you have enabled the Scaled Variable

e to read user-defined limits.

iab e Limits and Step Sizes

m y input limits for the each control vasController limits and step sizes. In contrast to the simple Controller which has adefault percent change of 2.0% of the initial control variable for the second iteration, the MVC has a default percent change of 10.0%. Optional Variable Scaling Select the Use User-defined Variable Scaling check box on the Variable Limits window to enable a linear formula for scaling the variable. In order to access this window, click on the default limits linked text in tMformula, the default limits linked text will chang Defaults for the scaled variable data are displayed on the Options window whichcan be accessed via MVC Options on the Multivariable Controller window. The same initial value, step sizes and tolerances are applied to all scaled parametersin the MVC. You may enter your own values here to replace the default values 100, 10, and 10-5 respectively. Number of Calculation Cycles

r of calculation cycles is calculated by the program as 8 plus the current number of variables. Alternatively, you may specify the

number of cycles by selecting the appropriate radio button on the Options window. By default, the simulation will stop if any variable exceeds the maximum or

inimum limits. You may select the Continue Calculations if Any Variable Exceeds the Limits check box to continue calculations using the limiting value if the limit is exceeded. Selecting the Next Unit Calculated After Control Variable is Updated

next unit calculated after the control variable is updated. ormally, the calculation sequence is determined automatically by PRO/II.

nit by choosing a unit from the drop-down list box on the Options window.

You may access several options for the operation of the MVC through the MVC Options button on the Multivariable Controller window. The default for the numbe1

m

Normally, the first unit operation in the calculation sequence affected by the control variable is theNHowever, you must supply a calculation sequence youself whenever any of the control variables are thermodynamic parameters. You may specify the return u


Print Results for Multivariable Controller

The default is to suppress printing of a convergence report. The Print Optionswindow allows you to override the default. This window is accessed by clicking Print Options on the Multivariable Controller window or be selecting

utput/Report Format/Unit Operations from the menu. A convergence summary can be printed after the last cycle or after every cycle by selecting the appropriate radio button. Select the Include Convergence Diagnostics check box to generate a plot of the convergence diagnostics. Select the Include Convergence Diagnostics check box to generate a plot of the convergence diagnostics.

section of this chapter for a discussion of convergence the Multivariable Controller calculations.

O

Nonconvergence of Multivariable Controllers See the Controller techniques used in Controllers and Recycle Loops See the Controller section of this chapter for a discussion of recycle loops.


Phase Envelope

General Information

he Phase Envelope utility module generates phase envelopes T for

neration is performed after the completion of flowsheet

Sel i

the be

nvelope main data entry window. You may optionally supply a liquid mole fraction for any of the selected

sheet stream with no liquid fraction entry to generate the phase envelope, followed by one or more

. It is issible to duplicate the same stream with the same liquid mole fraction in

e

lot p

multicomponent streams using the Soave-Redlich-Kwong or Peng-Robinson equations of state. The module is not available for other thermodynamic systems. Phase envelope gecalculations and has no effect on flowsheet convergence. For systems with noncondensible gases such as hydrogen, helium, and nitrogen it may not be possible to converge bubble point calculations and results should be reviewed carefully.

ect on of Streams You may select feed and product streams from any of the unit Operationsinflowsheet for phase envelope generation. Up to five flowsheet streams may selected using drop-down list boxes in the Phase E

flowsheet streams to generate a curve at a constant liquid mole fraction. This option is useful for generating liquid fraction curves to be superimposed on the phase envelope. Normally, you would first select a flow

selections with specified liquid fraction entries to generate a family of curvesnot perma singl phase envelope.

P O tions Select a plot option for the phase envelope in the Phase Envelope Plot Options window which you can access by clicking Plot Options on the Phase Envelop

ain data entry window. e

.

m For each selected stream, a default descriptive label is provided in this windowThe default label will contain the stream name and an L/F value if specified. You may modify each label. Duplicate labels are not allowed. An example default stream label with a specified L/F is: “S100 - L/F= 0.9".


A drop-down list box contains plot options as follows: None - The default

Individual - generates a plot with only the stream selected.

Com be prompted to provide a comparison plot symbol to label the data points for the generated curve. The symbol may be an integer number in the range one through nine. If you do not provide a symbol is n son plot, the next available integer between one

nd nine is used

s

mic System

Individual

Comparison All streams with the Comparison option are plotted on the same graph. The Comparison option is useful for plotting a stream phase envelope withsuperimposed curves of constant liquid mole fraction. When you select the

parison option for a stream, you will

ot provided for the comparia Individual and Comparison - The Individual and Comparison option performboth the Individual and Comparison options for a stream. Thermodyna Select the thermodynamic system of methods to be used for Phase Envelope calculations by choosing a method from the Thermodynamic System drop-downlist box on the Phase Envelope main data entry window.


PIPEPHASE Unit Operation

General Information The PIPEPHASE Unit Operation (PPUOP) encapsulates a PIPEPHASE simulation enabling it to be solved in sequential modular form within a conventional PRO/II simulation. The PPUOP allows the user to link PRO/II simulation streams to PIPEPHASE simulations streams so that stream properties

om a PRO/II simulation isfr passed to the PIPEPHASE simulation, and back to n in

o other PRO/II unit

eed and Product Streams

ct

product streams are mapped to the Sinks in a PUOP. The PPUOP Source can be specified with one feed stream only where

/II or

se two options can be selected from the Component mapping drop- own list in the PRO/II PIPEPHASE window, which can be accessed by double- licking the PPUOP.

the components are mapped by Name, the PRO/II component data is mapped ith the PIPEPHASE component of the same name.

PRO/II upon solution of the PIPEPHASE simulation. As with any unit operatioPRO/II, the PPUOP can be accessed multiple times in calculation loops, and a PRO/II simulation can have multiple instances of PPUOPs in the flowsheet.

he PPUOP is represented as an icon and is similar tToperations. It can be initialized with a PIPEHASE simulation. Note: PRO/II currently supports PIPEPHASE v8.2 and later versions. F The PIPEPHASE Unit Operation (PPUOP) can have multiple feed and produstreams connected to it. The PRO/II feed streams are always mapped to the Sources in a PPUOP and thePas the Sink unit operation data can be mapped to multiple product streams. The stream properties that can be transferred through mapping are: Temperature, Pressure, Flowrate and Composition. Component mapping Component mapping is allowed only if the number of components in both PROand PIPEPHASE are equal. The components can be mapped by either NameIndex. Thedc Ifw


If the components are mapped by Index, then the first component in the PRO/II

itialization

The PPUOP can be initialized with a PIPEPHASE simulation (.inp for PIPEPHASE 8.2 and either a .inp or a .ppzip for PIPEPHASE 9.0) by clicking

component data list is mapped with the first component of the PIPEPHASE component data list, irrespective of the component names.

In

Initialize from PIPEPHASE simulation… in the PRO/II PIPEPHASE window. If the user reinitializes a PIPEPHASE simulation with another simulation, then all the information of the previous simulation will be removed. Note: If PIPEPHASE version 8.2 files are used for initialization, it is necessary that the GUI database files, (.pp0 and .pp1) be present. Otherwise, the user needs to generate the PIPEPHASE GUI database files by importing the corresponding keyword file. PIPEPHASE GUI The PIPEPHASE GUI can be launched from within the PRO/II flowsheet. The user can commit the changes made to the simulation in the GUI, and export the changes to the keyword input file. The user can launch the PIPEPHASE GUI by clicking the PIPEPHASE GUI..button in the PRO/II PIPEPHASE window. Note: If PIPEPHASE v8.2 GUI is launched, it is necessary that the PIPEPHASE GUI files (.pp0 and .pp1) of that simulation are present. If not present, a warning message is displayed. The user is then required to export the keyword file. However, for version 9.0, changes made in the PIPEPHASE GUI will be automatically exported to the keyword file while saving the simulation.

Export The user can export a copy of the PIPEPHASE simulation to an external location by clicking Export to external PIPEPHASE simulation….

PIPEPHASE Reports The PIPEPHASE Report displays only the results of the PIPEPHASE simulation and not the PRO/II PIPEPHASE integration flowsheet.

You can view the results of a solved PIPEPHASE simulation by clicking PIPEPHASE Report…button in the PRO/II PIPEPHASE window or right-click the PIPEPHASE icon and select View Results.


Stream link specifications

imulation and a PIPEPHASE simulation can be Link Specifications grid, in the PRO/II PIPEPHASE

to

ations

y double-clicking the PPUOP. Check the option Define data link ecifications to access the grid.

or more details on these concepts, refer to the SPEC/VARY/DEFINE section of

IP n. Themade to

A link between the PRO/II sstablished on the Stream e

window. This window can be accessed by double-clicking the PPUOP icon. PRO/II streams that have been attached as feeds, and products are displayed onthe left side of the grid. PIPEPHASE Source streams are available on the drop- down lists on the right side, adjacent to PRO/II feed streams, and PIPEPHASE Sink streams are available on the drop-down lists on the right side, adjacentthe PRO/II product streams.

Define Data link specifications The parameters of a PIPEPHASE unit operation can be specified as Spec/Vary/Define variables from within a PRO/II simulation to control either aPRO/II flowsheet or a PIPEPHASE network simulation. The Spec/Vary/Define variables can be specified in the Data Link specificgrid. This grid is available in the PRO/II PIPEPHASE window, which can be accessed bsp FChapter 9 in this manual. File Handling When you drag and drop a new PPUOP on the PFD, and initialize it with a PIPEPHASE simulation, a copy of the PIPEPHASE file along with its databasefiles is stored in the PRO/II Temp directory. This Temp folder is called the

anaged folder and it will be the working directory for that specific PPUOP. All MP EPHASE related files reside in this folder during the PRO/II simulation ru

files in the Managed folder are under the control of PRO/II and any changes these files by providing inputs through the PIPEPHASE GUI launched

by click d not When a ith all

e PIPEHASE files (.inp, .pp0, .pp1, .out and other intermediate files for version es

om the Managed folder. This zip file will be archived into the PRO/II .prz along ith the conventional PRO/II (.pr1, .pr2, .sfd..) files.

ing PIPEPHASE GUI… are saved to the files in the Managed folder anto the PIPEPHASE database files in the original location.

PRO/II session is saved, a new zip file “PRZfileanme_UnitID.zip” wth8.2 and. ppzip for version 9.0) is created by copying all the PIPEPHASE filfrw


Pipe

General Information

heandmodes: ied line t a speprovappli , in which duty is u dete pha Fee A pipe oressure is assumed to be the lowest feed stream pressure.

A pipe may have one or m ct phase condition for pipe operations with one product is automatically set by PRO/II. For pipe units

ith two or more product streams, the product phases must be specified in the

T Pipe unit is used to model single or multiphase pressure drops in pipes

/or fittings which connect unit operations. This unit may be used in two Rating Mode where the pressure drop is computed based on a specif

diameter, and Design Mode where the line diameter is calculated to meecified pressure drop and/ or velocity criteria. Numerous algorithms are ided for the pressure drop calculations to model a variety of piping cations. A rigorous heat balance may also be performed for the calculations

heat is transferred through the pipe to or from an ambient medium, or aniformly applied to the length of the pipe. The phase equilibrium is

rmined for the product and it may be separated into streams according to theses. Both VLE and VLLE calculations are supported by this unit.

ds and Products

peration may have multiple feed streams, in which case the inlet p

ore product streams. The produ

wProduct Phases window which is accessed by clicking Product Phases… on the Pipe main data entry window.

roduct phases allowable include: vapor, liquid, decanted water, heavy liquid, Pand mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with vapor and liquid products and is not allowed when four product streams are pecified. It is important to note that where two liquid phases ars e present in

id

e

multiphase calculations, all pressure drop methods consider only a single liquphase which has fluid properties that are an average of the properties for the twoliquid phases. Calculation Type

The Calculation Type may be selected with the radio buttons provided on thPipe main data entry window. Options are as follows:


• Fixed Line Diameter - Forward Calculation (default) • Fixed Line Diameter - Backward Calculation • Line Sizing - Forward Calculation

Backward calculations determine the pressure drop in a backward, or reverse irection, starting from th re

zing option may be e is determined to

ified design c

calculations re uid and por viscosities d, fo o phase flow, the liquid surface te herefore e the dyna syst or

e calculations must pro se prope ies.

orrective Action for Calculation Failures

he Continue text string on the Pipe main data entry window may be clicked to select th ive actio tain types of calculation failures. The default

ses t available solution sets a negative computed utlet pressure to a small value and allows the flowsheet calculations to continue.

alculation the line diamete hich st closely satisfies e desi selected and flowsheet calcul continue. A maximum of ree co ilures d for pipe units recyc loops.

he Sto ates all flowsheet calculatio s whenever the e unit fails o reach n, or a n utlet pr sure is encountered.

Pressur ethod

rop method in the Pipe Pressure Drop d window

d e pipe outlet conditions. The pipe inlet conditions adefined by the results of t ations. The line sised for design mode, in which case the diameter of the pip

he backward calculumeet a spec riterion. Note: Pipe quire

nsion. liq va

, th, anmic

r twem chosen fT

vide thermo

th

rt

C

Te correct n for cer

option of Continue u he best oroFth

or line sizing c failures, r w mogn criteria is nsecutive fa

ations inth

is allowe le

Tt

p option termin n pip a solutio egative o es

e Drop M

Select the pressure d Metho accessible via Pressure Drop Method… on the Pipe main data entry window. The

d is he drop-do list box in this window, and g me

eggs-B -Moody with Palmer Correction (BBP), s , Duk n-Flanigan (DEF), Mukherjee-Brill (MB), Gray

RAY), and Hagedorn-Brown (HB). Beggs-Brill-Moody is selected t correlat

An optio ated pre op may e supp d in this window reduce

he convergence toleran lt of one ercent and the default flow efficiency f 100 p y be replaced in this window. The flow efficiency is a linear

pressure drop methoncludes the followin

selected with tthods:

wni BOlimen

rill-Moody (BBM), Beggs-Brill (OLIMENS) ler-Eato

(G as the defaulion.

nal estim ssure dr b lie to

the computing time. To

ce defau percent ma


adjustment factor that is applied to the calculated pressure drop to better match

tor essure drop cal e pplied if desired. If no val is ent d, the Moody friction factor

he mo Colebroo hite e ation

may be us clude or lude pres e dro ontribution nder certain high velocity or high pressure drop nditions,

a high for the Begg -Brill-Moody equation. nder these co , dropping this term results in a more

reasonable answer.

Note: The Beggs-Brill-Mo uation does not c w.

s the Pipe Line/Fitting Data window which is

actual conditions. The Moody friction fac for the pr culations may b sudirectly in this window, ue ereis calculated using t dified k-W qu s. The check box ed to in exc the sur p cfrom acceleration. U cothis term becomes unre listically sTherefore, u nditions

ody eq over critical flo

Line/Fitting Data Line and fitting data are upplied n ireached by clicking Line/Fitting Data on the Pipe main data entry window. For

er calcula dio butt s on th windo are us to select or the pipe diameter. When the Inside Diameter rad button is

pipe inside d r is supp direc When the Nosired

on, the sen with a drop-down list box. When no schedule

chosen, schedule 40 pipe is assumed in most cases.

The line length is supplied directly in this window. The maximum allowable line length is 900,000 feet (274,000 meters). An elevation change over the line length may be entered in the Pipe Line/Fitting Data window. A plus value indicates an increase in elevation; a minus sign indicates a decrease in elevation. The absolute value of the elevation change must not exceed the line length. One fitting K-factor may be attached to a pipe unit and supplied in this window. The K-factor is defined as the total resistance coefficient, and is limited to a maximum value of 100.0. Note that the supplied K-factor may be used to represent multiple fittings, valves, and exit losses. When a pipe unit is being used to represent a fitting or fittings only, a negligible line length should be provided. Radio buttons are used to select the pipe roughness in this window. The Absolute roughness may be entered in length units or the Relative roughness may be supplied. The roughness applies to both the line and the fitting. A default absolute roughness of 0.0018 inches or equivalent (new steel pipe) is used when no roughness is supplied.

fixed line diamet tions, ra on is w edthe input mode f io selected, the iamete lied tly. minal Pipe Size radio button is selected, a drop-down list box is used to select the depipe nominal diameter from a table of common pipe sizes. For this opti

ipe schedule may also be chopis


The nu string at the bottom he pressure

rop calculations are bas g p s gerefore, it is important to use multip s for systems in h

ificantly over the line l th (s as multiphase systems). he number of calculation segments has ignific culated

pressure drop for such systems. It is also recomm lines be divided into segments of 10,000 feet (3040 meters) or less. Note that a default of

s used for a it unless otherwise specified.

calculations are performed, the line/fitting diameter and fitting K-factor cannot be supplied, and these data entry fields are not available. Line Siz

ine sizing data are supplied in the Pipe Line Sizing window which is accessed

mber of calculation segments is selected by clicking the textof this window. A maximum of 50 segments may be used. T

dth

ed on the averale segment

e fluid ropertie in a sew

ment; ich the fluid

properties vary sign enga s

uchant effect on the calTended that long

one segment i pipe un Note: When line sizing

ing Data Lby clicking Line Sizing Da he Pipe main data entry window. Primary sizing riterion options are:

•

Outlet Pressure

rop or the minimum outlet pressure are upplied directly in the data entry fields provided.

Maximum Average Fluid Velocity constraint may also be defined. This onstraint can not be violated, and the primary sizing criterion will be relaxed as eeded to not exceed the supplied maximum velocity.

he Line Inside Diameter Selection Method is chosen with radio buttons as llows:

• Use Explicitly-defined Inside Diameters • Use Nominal Pipe Sizes

default inside pipe diameter table with ten diameters is provided. The default

ta on tc

Maximum Pressure Drop • Minimum

alues for the maximum pV ressure d

s Acn

Tfo

Avalues may be replaced as desired. Use Clear All to clear the pipe diameter table. The Restore Defaults button restores the ten default diameters.

table of nominal pipe sizes and corresponding schedule numbers may be Asupplied in the Nominal Pipe Sizes window which is reached by clicking Enter Data… on the Pipe Line Sizing window. Up to ten pairs of data may be provided.

ominal pipe sizes are selected from a table of supplied values via drop-down st boxes. The corresponding schedule numbers are also selected via drop-down

dule numbers default to schedule 40 in most cases. The

Nlilist boxes. Pipe sche


Clear All button may be used to clear all selected nominal pipe sizes and correspon Heat Transfer Data

su the Pipe Heat Transfer dow accessible via

ding schedules.

Heat transfer data are pplied on winthe Heat Transfer iconoption is selected via radi

on main data entry window. The du calculation

• • eat Tra• l Opera

ulation upplied duty is applied evenly over the entire length of the line. A positive value is used for heating and a negative value signifies This opt a duty o ero is used as the heat transfer default option. This option e used for both forward and backward calculat

temperat st be prov for the Ambient Heat Transfer option. The ctor has units of en / (area)(time) ee). A default v °F is use he ambien re. The heat transfer is compute e pipe s t inlet and outlet temperatu es, U factor, pipe inside area, and the amb erature. This option may be used with

The Iso peration option performs all pressure drop calculations at the inlet temperature to the p This option is no lowed for backward calculations.

ste e pipe c ulatio cted with the the in data ry win w. The proble

n no o rmodynamic system is se

the Pipe tyo buttons:

Fixed Duty Ambient H nsfer Isotherma tion

For Fixed Duty calc s, the s

cooling. ion with f z may b

ions.

An overall U factor and ambient ure mu ided U fa ergy (degr

alue of 6 d for t t temperatud from th egmen r

ient temp not backward calculations.

thermal Oipe unit. t al


The thermodynamic sydrop-down list box onsystem is used whe

m for th alc ns may be sele Pipe ma

her theent do m Default

t lected.


Polymer Reactor

The Polymer Reactor mod s either a fre dical or stepwise polymerization process in an ideal Continuous Stirred Tank Reactor (CSTR) or

Reactor (PFR). The polymerization reactions are assumed to take e liquid phase and the system is assumed to be homogeneous. The

reactors may be run in the isothermal or nonisothermal modes and the operating be set.

cal model allows for up to 79 different eaction d in copolymer free radical kinetics. Not all are intended to

simultaneously, in fact, the fewer mechanisms specified for the polymer realistic and reliable the model.

hat the polymerization reactions occur in the liquid phase. If the ase situation, a warning message is given and the user

must then specify new operating conditions to keep the system in the one phase

R mass and energy balances are solved to identify a single stable operating point. The polymer which exists at this operating condition is then characterized in terms of the method of moments to provide number and weight

verage molecular weights.

ms of the method of oments to provide number and weight average molecular weights.

he user must supply the feed component temperature, pressure, and omposition along with an estimate of the temperature of the isothermal reactor r a temperature estimate for the nonisothermal reactor. Kinetic and ermodynamic data for the reaction between chemical species must also be

rovided.

General Information

el simulate e ra

Plug Flowplace in th

pressure may The Polymer Reactor mechanisms to be use

culation r

be used system, the more It is assumed treaction leads to a two ph

region. The CST

a The PFR mass and energy balances are solved to identify a sequence of stableoperating points along the axial dimension. The polymer which exists at each point along the axial profile is then characterized in term Tcothp


etailed Information

n regarding operating mode uirements, and y of th Polymer Reactor model, consult the PRO/II Add-On

D For detailed informatio s, data reqrange of applicabilitModules User’s Guide.

e


Procedure Data

General Information

o calculate the reaction rate based on a user’s own action rate calculation is required by the plug, CSTR,

nd the alternative User-Added Kinetic Subroutines (see PRO/II s User’s Guide) can be used to calculate the proper rate

ach Procedure’s name, description,

variables and parameters. The code section is where all calculations are tion resembles a subroutine written in a FORTRAN-like

nguage.

Pro u e Procedure Data data entry window, which is acc licking the

rocedure Data toolbar button

Procedures provide a way talculation method. The rec

reactive distillation and batch reactor units. PRO/II’s default method for reaction rate calculation is based on power law rate expressions. For any other rate, expression type (such as Langmuir-Hishelwood) or any reaction rate which deviates from the base rate (such as a reaction with a mass transfer limitation),

rocedures aPUser-Added Subroutinefor reactor simulations. Procedures are essentially in line routines written in a language based on FORTRAN 77. There are two sections to a Procedure: Setup and Code. Thesetup section allows for the definition of e

performed. This secla Procedure Setup

ced res are entered in thessed through the Input/Procedure Data… menu option or by c

. Each Procedure in this window has a nd an optional description. As soon as the name for a

Pmandatory name aProcedure has been entered, its Enter Data… button becomes available. The button opens the Kinetic Procedure Definition window where you may click Edit/View Declaration to access the Declarations of variables and parameters.

Any variable names entered in Defined Procedure Variables will be ation from the reactor unit to the Procedures it

DEFINEd in the reactor unit, and accessed in the

an the default of 15 reactions.

available to transfer informcalls. They can be same manner as any other variable in the Procedure code.

There is only one Parameter available to be specified, which is the maximum number of reactions allowed. This only needs be changed if the Procedure must handle more th

Once setup is complete, click Hide Declaration to close the Declarations.


Procedure Code Note: The Procedure Code section is required and must terminate with a RETURN statement. The actual FORTRAN procedure is entered directly in the Code field on the Kinetic Procedure Definition data entry window. You may check the procedure as you compose it by clicking Check Code. The following predefined

d from the calling reactor unit: varibles are

provide

Kinetic data: These are the kinetic parameters are provided via K… of the Reaction Data section, and/or Unit Reaction Definitions… of the

ssure), and ents and mixture at the

User data: These are the integer, real, and supplemental data provided

Reactor unit. Reactor data: These data include the reactor sizing parameters and

operating conditions. Property data: These data include the thermophysical property data of

the pure components (e.g., molecular weight or critical prethe property data of the individual componreaction conditions.

by the user via Enter Data… when the procedure narate calculations for a ctor unit.

me is specified for Rea

tures are discussed below.

nd (&) at the

1 to 99999 (shown as “nn” in this manual).

A dollar sign (“$”) causes all following data on the line to be interpreted as a omment rather than as code. Unlike in FORTRAN, a “C” in column 1 does not esignate a comment statement.

used to pass values etween the procedure and the unit operation that uses the procedure.

Procedure data: These are the defined procedure variables entered during the Procedure setup. Their values are DEFINEd in the same window as the User data.

The supported language fea Elements of the Language

ach statement contains a maximum of 80 characters. An ampersaEend of a line indicates continuation on the following line. Note that an asterisk(*) is not valid as a continuation marker, since it signifies multiplication. All lines of code except the CODE statement may be preceded by a unique

umeric label fromn

cd Predefined Variables

he following variable names are reserved. They are Tb


The s the procedure. They may not p atement.

fir t tables list variables that provide input values toap ear on the left side of an assignment st

Procedure Data Predefined REAL Scalar Variables

ame PFR CSTR Batch RxDist Variable N

R

EAL Scalar Variables - Supplied in standard problem dimensional units

Temperature RTEMP X X X X Pressure RPRES X X X X Total Molecular weight RMW X X X X

Vapor Phase

RVMW X

Liquid Phase

RLMW X

L1 Phase RL1MW X

L2 Phase RL2MW X Specific gravity (60/60) RSPG

R X X X X

Total Molar Rate

RMRATE X X X X

Vapor Phase

RVMRAT X

Liquid Phase

RLMRAT X

L1 Phase RL1MRA X

L2 Phase RL2MRA X Weight Rate

RWRATE X X X X

Standard Volumetric Rate

RSVRAT X X X

Actual Volumetric Rate RAVRAT X X X

Vapor Phase

RVVRAT X

Liquid Phase

RLVRAT X

L1 Phase

RL1VRA X

L2 Phase RL2VRA X Liquid Fraction RLFRAC X X X X

L1 Phase

RL1FRA X

L2 Phase RL2FRA X Vapor PhaseViscosity RVVISC X X X X


Liquid Phase Viscosity RLVISC X X X X REAL Scalar Variables - Supplied in standard problem dimensional units Vapor Ph X ase Conductivity RVCOND X X X Liquid Phase Conductivity RLCOND X X X X Vapor Phase Sp. heat RVCP X X X X Liquid Phase Sp. heat RLCP X X X X Surface tension RSURF X X X X Absolute Temperature RTABS X X X X Tube Diameter (fine length) TDIAM X

ube Length TLEN X T

X

Cumulative Length CUMLEN X Plug Flow Step Size (fine length)

DELX X lume (CSTR VOLUME X X X Total reactor vo

& BATCH) or volume step size of PLUGFLOW reactor Vapor Phase Volume RVVOLU X Liquid Phase Volume RLVOLU X L1 Phase Volume RL1VOL X L2 Phase Volume RL2VOL X Gas Constant RGAS X X X X 1 Volumetric flowrates for CSTR and PLUGFLOW are calculated using bulk compositions

suming the specified reactor phase, even if the phase is actually mixed. A warning is asprinted if the actual phase is mixed.


Procedure Data Predefined INTEGER Scalar Variables Variable Name

PFR CSTR Batch RxDist

To

tal # of components NOC X X X X

Total # of reactions

NOR X X X X

Re

action phase IRPHAS X X X

Basis for Rate Calculation 0 = molar 1 = partial pressure 2 = fugacity 3 = mole-gamma

ICPFA X X X

Step # ISTEP X Unit # for output file

IOUT X X X X

Unit # for

index file INDX X X X X

Maximum # of reactions

MAXNOR X X X X


Procedure Data Predefined REAL Variable Arrays

Variable Name


Dimension : NOC

Total Molar Composition XTOTAL X X X X Total Molar Concentration XCONC X X X

Vapor Phase XVCONC X Liquid Phase XLCONC X L1 Phase XL1CON X L2 Phase XL2CON X

Vapor Phase Fugacity XVFUG X X X X Liquid Phase Fugacity XLFUG X

L1 Phase XL1FUG X L2 Phase XL2FUG X

Liquid Phase Activity XLACT X L1 Phase XL1ACT X L2 Phase XL2ACT X

Vapor phase Mole Fractions XVAP X X X X Liquid phase Mole Fractions XLIQ X X X X

L1 Phase XLIQ1 X L2 Phase XLIQ2 X

Vapor phase Mass Fractions XVMFRA X Liquid phase Mass Fractions XLMFRA X

L1 Phase XL1MFR X L2 Phase XL2MFR X

Dimension: 70 Real numbers supplied on RDATA statement

RDATA X X X X

Dimension: 200 Real

SUPPLE statement

SUPPLE X X X X numbers supplied on

Dimension: NOR Activation Energy* Pre-exponential factor Temperature Exponent

ACTIVE PREEXP TEXPON

X X X

X X X

X X X

X X X

Dimension: (NOC,NOR) Stoichiometric factor Reaction order

STOICH ORDER

X X

X X

X X

X X

* There is an important distinction between the values of activation energy for in line procedures and calculations involving local reaction sets in distillation columns or reactors.

he values of activation energy supplied the reference reaction set (in RXDATA) or in the local reaction sets are assumed to be in thousands of energy units per mole units, whereas,

the case of procedures, the user-supplied value is used without the above assumption. TA or local rxnset is used

s. A procedure using the same variable, say ACTIV(1),

T

inE.g., for the SI system, a value of ACTIV=123 kJ/kmol in the RXDAas 123,000 kJ/kmol in calculation

ould calculate based on a value of 123 kJ/kmol.w


Procedure Data Predefined INTEGER Variable Arrays Variable Name


Dimensionpplied

: 10 Integer on IDATA

IDATA X X X X sustatement Dimension: NOR Base Component

IDBASE X X X X Basis for Rate Calculation

r each reaction (liquid

l pressure = fugacity

3 = mole-gamma 4 = mole fraction 5 = mass fraction

ILBASI X1 fophase) 0 = molar 1 = partia2

Basis for Rate Cfo

alculation r each reaction (vapor

phase) 0 = molar 1 = partial pressure

y = mole-gamma

IVBASI X1

2 = fugacit34 = mole fraction 5 = mass fraction

DP

imension: (NOC,NOR) IPHASE X hase of components in rxn

1 = Vapor = Liquid 2

1Available only for Boiling Pot CSTR

he following variables are the PROCEDURE blocTa

k results available to PRO/II fter control is returned to the PLUGFLOW, CSTR or Reactive Distillation unit

operation. RRATES must be defined for all reactions.


PROCEDURE Results Variable Name


Values of solution flag: Default value. PRO/II

X X X 0assumes the PROCEDURE

2 PROCEDURE failed, but continue calculations if in a e cle or control loop.

X

step has solved. 1 PROCEDURE solved.

r3

cy PROCEDURE failed, stop

all flowsheet calculations. Reaction rates for each

) L1

B moles/(vapvol*time) for

OPERATION PHASE=V1

RRATES(NOR)

X X X X reaction moles/ (liqvol*timefor OPERATION PHASE=,

Temperature derivatives for each reaction

DRDT(NOR)2 X Cea

omposition d vatives for ch reaction

DRDX(NOC, NOR)2 X eri

1 CSTR and PLUGFLOW should not be used when multiphase reactions are expected. Except for Reactive Distillation and the CSTR boiling pot model, PRO/II assumes the phase

100% liquid or vapor as defined on the OPERATION statement. is2 The use of this is optional. Procedure Data Programming Language

ssion of the Calculator module at the beginning of this chapter for a survey of the proper use of Declaration Statements , Assignment Statements ,

ortran Intrinsic Functions , PRO/II Intrinsic Functions, IF Statements , tements ).

See the discu

FCalculation Flow Control Statements , and Calculation Termination Sta


Pump

The d to compute the energy required to increase the pressure of a pro f energy is added to the feed enthalpy to determine the outlet temperature. Only one liquid phase is considered in the calc Feeds a

ssure. A single liquid

io utton on the Pump main data entry window as:

ressure re rise (∆P)

pumping efficiency in percent may be supplied in the data entry field provided on the P window. This value is used for the work and outlet tem ra lied, a default value of 100 percent is used.

hermodynamic System

used for pump calculations may be elected by choosing a method from the Thermodynamic System drop-down list

General Information

Pump may be usecess stream. This quantity o

ulations.

nd Products A pump operation may have multiple feed streams, in which case the inlet ressure is assumed to be the lowest feed stream prep

product stream is allowed from a pump.

utlet Conditions O The Pressure Specification for a pump is selected with the appropriate radb

• Outlet p• Pressu• Pressure ratio based on the lowest feed stream pressure.

Pump Efficiency A

ump main data entrype ture calculations. If not supp

T The thermodynamic system of methods to besbox on the Pump main data entry window.


Reaction Data General Information Use the Reaction Data Sets data entry wiheat of reaction, kinetic and equilibrium dafor each reaction. One or more reactions

s (coinimization, plug flow, CSTR, an

operations can have common access to th

er interface now suilibrium Reactor

Note: You may specify the base compone action and provide heat of

n and equilibrium and kinetic data i . For rsion reactors, these data are consi

unit operation level. See the Reactor sect

Reaction Data win

Click Reaction Data

ndow to supply reaction stoichiometry, ta, and to specify the base component

may be saved as separate reactiondata sets and used in all reactor typeenergy m

nversion, equilibrium, Gibbs free d boiling pot reactors). Multiple unit e same reaction data.

The PRO/II graphical usexpressions for each Eq

upports multiple equilibrium .

t of the renreactioconve

n the Reactor data entry windowdered to be local and are entered at the ion later in this chapter.

To access the

dow:

on the m Note: Any data entered in the Reaction Data window will be passed to the Unit Reaction Definitions window (a subwindow of the main Reactor window) and used as default values. Specifying Reaction Sets Provide a name and description for each n Data window. The name is required but th Note: You must define the component list try window before entering reaction data. Thicomponents for each reaction must be se eviously-defined omponent list .

o enter data for each newly-defined reaction data set, or to modify the

data for imported sets:

ain toolbar.

reaction data set in the main Reactioe description is optional.

in the Component Selection data ens order is important because

cted from a prlec

T

Click Enter Data… for that set.

This opens the Reaction Definitions window for that set. Here, you may enter the following information for the reaction data set:


• Kinetic rate calculation method • The name of all reactions in the set (required) • The reaction stoichiometry (required) • The heat of reaction and the base component (required) • Equilibrium data (optional) • Kinetic data (optional).

The k ed tic

med as one

the stoichiometry:

n the Reaction Components window.

ent (library components only), or based on the name (for library, non-library, or petro components).

o define the heat of reaction:

reaction in a specific action data set, in the Heat of Reaction Data window. This window appears

To select the kinetic rate calculation method:

inetic rate can be calculated from PRO/II’s reaction rate subroutine bason the power law rate expression, by an inline procedure or by the user’s kinesubroutine. The inline procedure must be first defined in the Procedure Data section and selected from the Procedure Name drop-down list box. When a user-added kinetic subroutine is used, it can be selected from the Subroutine Name

rop-down list box. The user’s added kinetic subroutine must be nadof the five USKIN1, USKIN2, USKIN3, USKIN4 and USKIN5 routines and linkedto PRO/II as described in the PRO/II UAS/PDTS Installation Guide. To define Define the reaction stoichiometry by clicking on the linked text Reactants =

roducts in the Definition column to opePHere, you may select the reactants and products for the reaction and supply thestoichiometric coefficient for each. You may define the reaction based on the hemical formula of the componc

T You may define the heat of reaction for any selectedrewhen you click H… located beside the selected reaction on the Reaction

efinitions window. In this window, you may choose one of two options:

e reaction components. This is the default.

User-specified: You supply the heat of reaction (in units of energy/ weight). If so optionally supply the reference temperature, nce reaction phase.

e: You must supply heat of reaction data for non-library components that do

ot have heat of formation data. You must also specify the base component for the reaction.

D Calculated from Heat of Formation: This option allows PRO/II to calculate the hea f sed on the heats of formation for tht o reaction ba

you do so, you may alcomponent, and refere

Notn


To supply equilibrium data for a specific reaction in a reaction data

et: s

Click E… located beside the selected reaction in the Reaction Definitionswindow. The R

eaction Equilibrium Data window appears.

Click the Define Equilibrium Data check box to enter equilibrium data.

s for the equilibrium equation t least one coefficient must be supplied).

underlined) text in the nits box. (If you do not change the temperature units, the global units are used

Equilibrium Constant Expression: The default reaction phase, reaction activity

Activity Exponent and Activity Phase to specify the exponent order and activity phase for each component in the

por ents

To supply kinetic data for a specific reaction in a reaction data set:

You may supply the following data in this window: Equilibrium Coefficients: Up to 8 (A-H) coefficient(a Units: Temperature, weight, volume and pressure units of measure for the equilibrium data may be supplied by clicking on the linked (uby default).

bases for both vapor and liquid phases, component reaction phases and exponent orders can be entered here. Click

reaction. The vapor activity basis is used for all components specified with vaphase activity phase while the liquid activity basis is used for all componspecified with liquid phase activity phase.

Click K… located beside the selected reaction in the Reaction Definitions window. The Reaction Kinetic Data window appears.

Click the Define Kinetic Data check box to enter kinetic data. You may supply the following data in this window: Pre-exponential Factor (A): The pre-exponential factor of the power law kinetic rate equation for the reaction. The default is 1.0. Activation Energy: The activation energy of the power law kinetic rate equation for the reaction in units of energy/weight. A default of zero is used if a value is not supplied. Temperature Exponent: The temperature exponent of the power law kinetic rate equation for the reaction. A default of zero is used if a value is not supplied. Reaction Order and Activity Basis: The default reaction phase, reaction activity bases for both vapor and liquid phases, component reaction phase and


kinetic orders that are used to define the kinetic rate expression can be entered here. Click Reaction Order and Activity Phase to specify the kinetic reaction order and activity phase for each component, which appeared in the rate expression. The vapor activity basis is used with all components specified with vapor activity phase while the liquid activity basis is used with all components specified with liquid activity phase.


Reactor General In

formation

The Reactor unit operation simulates the operation of many chemical reactors including conversion reactors, equilibrium reactors, Gibbs (Free Energy Minimization) reactors, Plug Flow Reactors (PFRs), Continuous Stirred Tank

er conversion or equilibrium reactors.

Feeds and Products

ctor may have one or more feed streams. A multiphase product from the reactor may be separated into streams containing one or more phase. The allowable product stream phases are vapor, liquid, decanted water and mixed (vapor+liquid). A mixed phase product is not allowed with a vapor or a liquid

roduct. The decanted water product is also used as the second liquid product

Reactors (CSTRs), and Boiling Pot Reactors. In addition to the above reactor types, PRO/II contains built-in Shift and Methanation reaction data sets for eith

Each rea

pphase with rigorous VLLE calculations. If this is more than one product stream, the phases must be allocated to thestreams in the Product Phases window. Access this window by clicking Product Phases… on the main Reactor data entry window for the particular reactor type.

tor type y choosing the appropriate reactor icon from the PFD palette. CSTR and boiling

on the main Reactor data entry window.

n the Gibbs reactor, you must select a reaction data own list box (option

e or a user-defined set may be specified. See the Reaction

Data section, earlier in this chapter, for more information on specifying reaction

Reactor Type For conversion, equilibrium, Gibbs, or plug flow reactors, select the reacbpot reactors share the CST/Boiling Pot Reactors icon. Select the desired reactor type from a drop-down list box

Reaction Set For all reactor types other thaset from the Reaction Set Name drop-d s include a built-in reaction set, e.g., Shift reaction, or a user-defined set) on the Reactor main data entry window. For the Gibbs reactor type, either no reaction data set may bselected (option None),

data sets.


Thermal Specifications

or most reactor types, the fixed operating temperature, the temperature rise he fixed reactor duty may be specified by using radio

uttons and entering values in the appropriate data fields. The available options are: Temperature Rise: This is the temperature increase across the reactor. This

ption is available for conversion and equilibrium reactors only where it is the

ou may specify the final reactor temperature for all reactor

actor

Facross the reactor, or tb

odefault. Combined Feed Temperature: The average temperature for all feed streams tothe reactor. This is available for plug flow and Gibbs reactors, and CSTRs only where it is the default.

Fixed Temperature: Ypes. ty

Fixed Duty: You may specify the reactor duty for all reactor types. A default value of 0 will be used if a value is not specified. The following additional reinformation may also be given via the main Reactor window: External Heat: You may specify information on the external heating or cooling source by selecting the External Heat option. This is for plug flow reactors only.Click Enter Data and enter data in the External Heating/Cooling window.

emperature Profile: YT ou may enter the reactor temperature profile in tabular percent or only.

form as a function of the actual reactor length, or as a function offractional distance along the reactor. This is for plug flow reactors Reactor Data Click Reactor Data… from the main Reactor data entry window to open the

r configuration informatio n. Reactor Data window where you can supply reacto

Conversion and Equilibrium Reactors


For these reactor types, you may choose an error handling option by clicking thStop calculations hypertext. The options are:

e

top Calculations: This stops calculations if an error occurs (e.g., for negative component flows). This is the default. S

Continue Calculations with no Reaction: Continue calculations with no reaction if an error occurs. Add Makeup of Limiting Reactant: Reduce conversion by adding a makeup of the limiting reactant if an error occurs. Reduce Conversion: Reduce conversion if an error occurs. Continuous Stirred Tank Reactor

You must provide the reactor volume for CSTRs in the Reactor Data window. Optionally, you may also provide estimates of the product flowrate. Plug Flow Reactor

Enter the following data for PFRs in the Reactor Data window:

ube Inside Diameter: The inside diameter of the PFR tubes. Data for this field

umber of Tubes: The total number of tubes in the PFR. Default is 1.

umber of equidistant locations along the actor length for the temperature profile. Default is 10.

Integration Options: You may select one of four integration options:

Reactor Length: The total length of the reactor. Data for this field is mandatory. Tis mandatory. N Number of Points for Profile: The nre


• Fixed step size Runge-Kutta method. The Runge-Kutta method with 20 steps is the default.

• Runge-Kutta method with user-specified step size. • Gear integration method with user-specified gear tolerance (default

tolerance = 0.1%). • LSODA (Livermore Solver of Ordinary Differential Algebraic equations)

method with user-specified tolerance (default tolerance = 0.1%).

in the Pressure window:

Select between the two options listed for Reactor Type

• Open Pipe: Select this option, when the packing is not found in PFR. • Packed Pipe: Select this option, when the PFR is packed with catalyst

particles. Select an appropriate option from the list to enter the pressure pecification

Inlet and Outlet Pressure

ed Pressure Drop

pen Pipe under Reactor Type, the first three options

ressure Profile: Selecting this option will enable the Enter Data button. Click Enter Data to open the Pressure Profile dialog box. Select the appropriate Location option from the drop-down list and start entering the data for Location and Pressure.

• Actual Tube Length • Percentage of Tube Length • Fraction of Tube Length

Enter the following data for PFRs

s

• • Pressure Profile • Pressure Drop Method • Packed B

you have selected OIf

mentioned above will be made available to the user. If you have selected Packed Pipe under Reactor Type, except Pressure Drop Method all other options will be made available to the user. Inlet and Outlet Pressure: Selecting this option will enable the Inlet and Outletsection. User is prompted to enter data listed under the following section.

• Inlet • Outlet

P


If you have selected Open Pipe in the Reactor Type section, Pressure Drop Method will be made available for selection. In case you have selected Packed Pipe in the Reactor Type section, Packed Bed Pressure Drop will be made available for selection. Pressure Drop Method: Selecting this option will enable the Enter Data button.

lick on it to open the Pressure Drop Method dialog box.

ressure Drop Correlation: Select the appropriate pressure drop method listed

C

Pin the drop list. Pressure Drop Correlation Significance Beggs-Brill-Moody This is the default PRO/II meth

is the recommended method for mood, and

st systems, especially single phase systems.

Olimens Used for gas condensate systems, which uses the Eaton correlation to calculate liquid holdup and Moody diagrams for friction factor.

Dukler-Eaton-Flanigan This hybrid correlation is for gas condensate systems that are mainly gas.

Gray e

Recommended for vertical gas condensate systems. It should not bused for horizontal lines.

Hagedo r rn-Brown This method is also recommended fovertical pipelines, and should not be used for horizontal pipes.

Mukherj or gas condensate systems. This method must be used with care due to its discontinuities. Use at least 2 pipe segments to avoid failures due to changing flow regimes.

ee-Brill Used f

Beggs-Brill-Moody-Palmer This method uses the same correlations as above and also includes the Palmer modification to account for liquid holdup, based on experimental data for uphill and

s. downhill line


Convergence Tolerance : Supplies a relative convergence tolerance value for the calculated pressure drop per reactor segment, between each successive

meter is used for linear adjustment of the calculated ressure drop to match actual conditions. For given flow conditions, decreasing

s an increase in the calculated pressure drop. The value may be reater than 100 percent. It is recommended that data for roughness or Moody

oody Friction Factor : PRO/II usually calculates the friction factor from reactor

ired.

oughness : A roughness value can be supplied either in Absolute or Relative absolute roughness of 0.0018 inch.

eleration Term : Check this option to include the acceleration pressure gradient. Under certain high velocity or high pressure conditions, the Beggs and Brill acceleration term becomes unrealistically large and dominates the equation.

ropping the term often results in a better answer in these cases.

Packed Bed Pressure Drop : Selecting this option will enable the Enter Data

iteration. By default, PRO/II uses a one percent tolerance. Flow Efficiency : This parapthis value causegfriction factor be provided for accurate calibration of results. Mroughness and Reynolds number using the modified Colebrook-White equations. You can supply a value for this field if des Runits. By default, PRO/II supplies an Acc

D

button. Click Enter Data to open the Packed Bed Pressure Drop Method dialog box. Pressure Drop Correlation : Select Ergun Equation to calculate the pressure drop across the packed bed. Diameter of Catalyst : Enter the diameter of the catalyst. Data for this field is mandatory. Void Fraction of the Packed Bed : Enter the Void fraction of the packed bed. Data for this field is mandatory. Under Shape Factor section, enter data for the shape of the catalyst. Select either of the two options depending on the catalyst. Sphericity : Enter the sphericity of the catalyst. Shape of the Catalyst : Selecting this option will make the following option available to the user. Select either of the two options.


• Spherical • Cylindrical : If you have selected Cylindrical, enter the Length.

Boiling Pot Reactor

You may supply the following reactor calculation options for the boiling pot reactor in the Reactor Data window: Tolerances: The absolute temperature and relative mole fraction and enthalpy tolerances for the reactor may be changed from their default values of 0.1º, 10-5, and 10-4 respectively. Note: If the Fixed Duty option is specified on the main Reactor data entry window, an estimate of the reactor temperature may optionally be provided in thReactor Data window. The minimum and maximum temperature defaults of 457.87 F and 4940.33 F may also

e

be overridden.

Maximum Liquid Volume: If a fixed volume is not supplied on the main Reactor window, you may supply a maximum liquid reactor volume in this window. A default of 3531.5 ft3 will be used if a value is not provided.

itial Volume Estimate: An initial volume estimate may optionally be supplied window.

-

Inin this Component product rate estimates may also be supplied by clicking Product Estimates… on the Reactor Data window. The number of Broyden trials before the Jacobian matrix is updated may be

derivative step size multiplier by clicking on the appropriate underlined linked text. The defaults are 3 trials and a step size specified along with the

multiplier of 0.01.


Gibbs Reactor

ser may provide a number of optional calculation window:

is

convergence tolerance. The default is nd 10-6 for adiabatic conditions.

addition, you may specify the physical property evaluation method by clicking

p: The physical property values are reevaluated at each

step of the search. This is the default.

ked text. The available options are:

upplied reacting component rates: This option uses the values given for the acting component estimated rates. Supply reacting components and estimated tes in the Reacting Components window, which is reached by clicking Reacting omponents and Estimates on the Reactor Data window.

he options to specify the parameters for the free energy minimization phase alculations are found in the Phase Split Parameters window. This opens by licking Phase Split Parameters on the Reactor Data window.

For the Gibbs reactor, the uoptions in the Reactor Data Maximum Iterations: The maximum number of iterations allowed. The default 50. Convergence Tolerance: The relative 10-4 for isothermal conditions a Fibonacci Tolerance: The convergence tolerance for the Fibonacci search calculations. The default is 0.01. Inon the underlined hypertext. The options are:

Evaluated at each ste

Used from previous iteration: The physical property values from the previous iteration are used. You may select the product rate estimate option by clicking on the underlined lin PRO/II default: The default generates an initial estimate of the product rates using the PRO/II method. Average of all feeds: This uses the average of all feed rates to generate an nitial product rate estimate. i

SreraC Tcc


Note: The Phase Split Parameters window is available only if the Reactor Phase is specified as Calculated on the Unit Reaction

efinitions window. See below for Unit Reaction Definitions.

pecfying Reactions: The number of chemical reactions (i.e., the number of st equal the number of chemical species minus the

ally, the number of effective atoms is the number f atomic species.

ple,

OperationD

SREACTION statements) munumber of effective atoms. UsuoThe number of effective atoms differs from the number of atomic species when two or more atoms always occur together in the same proportion. For examconsider the chlorination of ethylene: Keq

C 242242 ClHCClH +⇔+

here are 3 atomic species (C, H, Cl), but C and H always occur in a 1:2 ratio.

species, so only one chemical reaction is llowed.

his entry is the phase used for the initial reactor alculations. The user may select the vapor, liquid, vapor–liquid, liquid–liquid,or

default is vapor–liquid.

phase

tomic groups can be provided in the Atomic Groups window. This window can be reached by clicking the User-specified Atomic Groups button on the Reactor Data window. Unit Reaction Definitions The reaction phase, heat of reaction, equilibrium data, and kinetic data for the reactor may be entered in the Unit Reaction Definitions window. Bring up this

TTherefore, the number of effective atoms is 2 (Cl and CH2). These two effective atoms represent the three chemical a The options available on the Phase Split Parameters window are: Initial Phase Estimate: Tcvapor–liquid–liquid phase. The First Phase Evaluation at Iteration: Specify the first iteration where thewill be reevaluated. The phase should not be evaluated too early because the reaction results may still be far from the final solution. The default is 6. Phase Evaluation Frequency: Specify the number of iterations between phase valuations. The default is 4. e

Minimum Phase Tolerance: When the molar ratio of a phase to the total quantity of material is less than this value, the phase is considered as non-existent. The default is 10-6 . A

window by clicking Unit Reaction Definitions… on the main Reactor window.


Note: Any data previously entered in the Reaction Data Category window will be

es.

quilibrium Reactor

transferred to the Unit Reaction Definitions window and used as default valuYou can overwrite the data for a particular reactor in the Unit Reactions Definitions window for that reactor. E You may supply the operation phase of the reactor in the Unit Reaction Definitions window. By clicking Equilibrium Data… in this window, you gain

ccess to the fields where you may supply the following:

quilibrium Coefficients: Eight coefficients (A-H) of the equilibrium equation.

e

ptions are restricted to ºR or ºK for the temperature units.

reaction set by clicking the Define the Stoichiometry for the First eaction check box. The values of stoichiometric coefficients are to be

efined in the entire reaction set. The stoichiometric data displayed in the grid

t Reactor

ration phase, reaction activity basis and kinetic te calculation method in the CSTR Unit Reaction Definitions window.

.

eaction Activity Basis: For vapor phase, the options are Molar Concentration, artial Pressure or Fugacity. For liquid phase, the options are Molar oncentration, Fugacity or Activity. Currently, only homogeneous reaction rate xpressions based on either vapor or liquid phase reactions are allowed for the STR. For BPRs, heterogeneous reaction rate expressions are allowed.

inetic Rate Calculation Method: The options are Power Law, User Added Subroutine or Kinetic Procedure. If the default is used, the reation rates are

a E Units: The temperature, weight, volume and pressure units of measure for thequilibrium equation can be changed by clicking on the underlined linked text. O Conversion Reactor You may overwrite the stoichiometric coefficients for the first reaction in the selected Rdetermined from the calculation results of the selected Calculator unit. Frequently, this feature is applied to use a single reaction to represent the overall reaction behavior in the reactor and, therefore, there is only a single reaction dbox are merely used to echo the reaction equation previously defined in the Reaction Data section. Continuously Stirred Tank Reactor and Boiling Po You may supply the reactor opera Reactor Operation Phase: The options are vapor or liquid phase for the CSTR, but restricted to liquid phase for the BPR RPCeC K


computed by power law kinetics in the form of the general Arrhenius equation. Fbutton.

or any of these methods, kinetic data can be entered through the Kinetic Data…

Power Law: The default method.

ser-added Kinetic Subroutine: This option directs the CSTR module to use a S) written in FORTRAN to perform reaction rate

routine Name in the Unit Kinetic Data window. The

er left table for any

rray of integer variables and the upper right for an additional (Supplemental) These local data, kinetic reaction data specified in the

elected reaction set, and thermophysical property data of the reaction mixture s.

STR module to use a user-supplied line kinetic Procedure to perform reaction rate calculations. After selecting the

e selected rocedure.

Energy: The activation energy for the kinetic power law rate quation. The default is 0.

Temperature Exponent: The temperature exponent for the kinetic power law rate equation. The default is 0. Base Component: A base component must be supplied for the kinetic reaction rate report.

UUser-added Subroutine (UAalculations. Specify a Subc

identifiying arguments for the subroutine name “U1”, “U2” … “U5” correspond to user-added subroutines “USKIN1” … “USKIN5” respectively. After selecting the user-added kinetic subroutine, you can enter local values (i.e., specific just to this reactor) for variables to be used for the rate calculation. Use the upper left table

supply local values for an array of real variables, the lowtoaarray of real variables. swill be provided to the selected kinetic subroutine for reaction rate calculationRefer to the PRO/II User-added Sub-routine User’s Manual for instructions on creating and installing UASs. Kinetic Procedure: This option directs the Cinname of the Procedure (which must be first defined in the Procedure Data section), you can enter values for local variables similar to the procedure for theUser Added Kinetic Subroutine mentioned above. Additionally, you may provide the values for those procedure variables (PDATA) used by thP Plug Flow Reactor Data that may be specified for the Plug Flow Reactor are the same as those described above for the CSTR. Pre-exponential Factor: The pre-exponential factor for the kinetic power law rate equation. The default is 1. Activatione


Reaction Order and Activity Basis: As is done in the Reaction Data section on global basis, the default reaction phase, reaction activity bases for both vapor

ick Reaction Order and Activity Phase to specify the kinetic reaction rder and activity phase for each component which appears in the rate

por activity basis is used for all components specified with ctivity basis is used for all components

lculations wil be based on the selected

only.

aand liquid phases, component reaction phase and kinetic orders that are used to define the kinetic rate expression can be entered here as local data for this reactor. Cloexpression. The vaapor activity phase while the liquid av

specified with liquid activity phase. Gibbs Reactor You may specify the phase of the reactor operation in the Unit Reaction Definitions window. The reaction phase options are Calculated (default), Vapor, Liquid, Vapor–Liquid, Liquid–Liquid or Vapor–Liquid–Liquid. If Calculated is selected, PRO/II will determine the phase as part of the free energy minimization alculation. If a phase is selected, the cac

phase. Extent of Reaction To specify the extent of the reaction for a conversion, equilibrium and Gibbs reactors Click Extent of Reaction… on the main Reactor data entry window to open the ExtenReaction window.

onversion

t of

Reactor

determificients of the reaction will be taken as the absolute moles upply constants for the second order temperature-dependent

tent Reaction Set window,

C You may select the base component from which the conversion data were

ned. If the base component is not selected (select “none”), the stoichiometric coefeacted. You may sr

fractional conversion equation in this window. Default values for the constants are given in the table. Click on the underlined linked text to change the temperature units of measure for the conversion reaction. If the temperature unitsof measure are not specified locally, the problem temperature units are used. Equilibrium Reactor The base component for user-supplied reactions must be specified in the Exf Reaction window. You may access this window via the o

which contains a list of the reactions that have earlier been defined for the flowsheet. Upon choosing the desired equation, the Extent of Reaction window appears. (The base components of built-in reactions such as Shift and Methanation are predetermined and need not be supplied by the user.)


You may specify the approach to conversion either as a temperature or a

are given in e table. Click on the underlined linked text to change the temperature units of

ction. If the temperature units of measure are not re units are used.

Extent of Rea a component prod e specified for each individual

c proach or a base component product rate.

licking Catalysts on e Reactor Data window). Before the button becomes active, the following nditions must be met:

• You must specify the catalytic component with a reaction stoichiometry of ‘0.’ (Input/Reaction Data(Enter Data…)/ Reaction Definitions(Definition)/ Reaction Components). See the previous section on Reaction Data for more information on defining reaction data sets.

• You must specify the reaction order for the catalytic component as any number other than ‘0’ in the Reaction Order & Activity Phase window. This window may be accessed by clicking on the like-named button located on the Unit Reaction Definitions/Unit Kinetic Data window for the boiling pot reactor, or by the following path: Input/Reaction Data(Enter Data…)/Reaction Definitions/(K…)/Kinetic Reaction Data(Reaction Order & Activity Phase).

Pressure

fractional approach. As was the case with the Conversion reactor, you may supply constants for the second order temperature-dependent fractional conversion equation in this window. Default values for the constantsthmeasure for the conversion reapecified locally, the problem temperatus

Gibbs Reactor The extent of reaction can be provided on a global basis in the

ction window (as a component percent converted, or as uct rate). The extent of reaction can also b

rea

tion as a temperature ap

Amount of Catalyst For boiling pot reactors only, you can specify the amount of a nonvolatile catalyst componenton a weight or molar fraction, or total weight or mole basis in the Catalytic Components window (which may be reached by cthco

For conversion, equilibrium, Gibbs reactors and CSTRs, click Pressure on the main Reactor window to enter the following reactor pressure options in the Pressure data entry window: Pressure Drop: The pressure drop across the reactor. This defaults to 0 if not supplied. Outlet Pressure: The pressure at the reactor outlet.


For the plug flow reactor, either the inlet and outlet pressure or a pressure profile along the reactor length (actual length, or percent or fraction of tube length) may be entered on the Pressure window:

n ath for the heat of reaction calculation.

mic system of methods for the reactor calculations may be st

Inlet: Either the pressure drop below feed (the default is 0 psi), or the inlet pressure may be supplied. Outlet: Either the pressure drop below inlet (the default is 0 psi), or the outlet pressure may be supplied.

rint Options P For all reactor types, excepting the Gibbs reactor, the following print option is available through the Print Options window: Print Calculation Path for Enthalpy Balance: This option prints the calculatiop

Thermodynamic System The thermodynaselected by choosing a method from the Thermodynamic System drop-down libox on the main Reactor window.


Reactor, Batch

he roduction as a result of simvess

mova r phase products. The Batch Reactor may be run in a true batch or vessel prior to the the end of reaction

roc ghout the a teady- configuration automatically considers e presence of holding tanks for steady flow streams to provide the time-variant

e batch unit. Implicit holding tanks are also considered for the of the time-variant process to the nment. A representation of the product

ream comes from an overall process time average of the quantity

Batch Reactor supports only liquid-phase reactions. A reaction one or more vapor constituents. Whether the vapor constituent(s)

ase and again be available for reaction(s) will be uilibrium analysis done at the end of each time step.

stem

Thermodynamic Batch Reactor dialog box. Batch Reactor also

Det For deta tion about the use of the Batch Reactor unit operation, onsult the PRO/II Add-On Modules User’s Guide.

General Information T Batch Reactor unit operation models material p

ultaneous and/or sequential reactions in the liquid contents of a reactor el. Phase equilibrium analysis during the reaction allows for the tracking or

l of vaporesimulation mode, with the reactants charged to the reactnset of reactions, and product taken from the vessel at o

p ess, or in a semi-batch mode where reactants may be introduced throureaction process. Batch reactor calculations may also be integrated into

state process simulation. The unit sthreactants to thproduct streams to provide a couplingontinuous process simulation enviroc

steady flow staccumulated into a given product. Currently, the may producewill return to the liquid phdetermined by eq Thermodynamic Sy

he thermodynamic system for the unit is selected by using the TSystem drop-down list box in the allows the use of electrolyte thermodynamic methods.

ailed Information

iled informac


Solid Separator

The So ni material from a ms perates adiabatically at the lowest of the

ssures.

oduct Streams

parator unit can have up to ten (10) feed streams. The inlet thermal feed

r requ es both overhe ms.

Calculation Method The solid separator provides the option of specifying the fraction of the solid

that is removed in the bottoms stream. The default fraction of the solid compo d in the bottoms stream is 1.00. An adiabati tio ses and the outlet

ned feed.

or unit supports both VLE (two phase) and VLLE (three phase) calculat termine the individual phase compositions. See the online

echnical Information discussion entitled VLE Model and VLLE Model for more window for VLE and VLLE calculations,

the menu bar.

General Information

lid Separato t models th strea . The unit o

r u e separation of solid phasemixture of feedindividual feed stream pre Feed and Pr

he solid seTcondition is determined by an adiabatic flash calculation at the lowest stream p ure. ress

The solid separato

ir ad and bottoms product strea

components in the total feednents remove

c flash calcula n is used to determine the product phaal condition of the combitemperature based upon the therm

The solid separat

ions to deTdetails. To access the main data entry elect Tools/Binary VLE froms


Splitter

General Information This unit may be used to split a single feed or mixture of feeds into two or more

roducts of identical composition and phase condition. The outlet stream batic flash used to determine

ce of options is provided for splits in feed is available to meet the specified product rates.

sthe A sidenstrea e used

Specifications For a splitter with N product streams, N-1 product stream rates must be specified. Product rate specifications are supplied by clicking on the underlined

he unspecified rate.

cification format and are further described in EFINE section of this chapter. Only specifications that are rate

te total, stream or component(s) recove

ppressure may be specified, if desired, and an adiahe outlet temperature and phase. A choit

which insufficient Feeds and Products A plitter may have multiple feed streams. The lowest feed pressure is used for

pressure of the combined feed.

plitter must have two or more product streams. All product streams have tical compositions and phase conditions. Phase separation of product ms is not available in this unit, and, if desired, a Flash unit operation must

for this purpose. b Product Rate

hypertext strings in the Product Rate Specifications section of the Splitter main data entry window. All of the splitter product streams are listed and any one may e used for tb

Specifications use the general spethe SPEC/VARY/Ddependent are allowed, e.g., stream or component(s) ra

ry, stream enthalpy, etc.


Outlet Pressure Specification

re

The outlet pressure for the splitter products may be changed by applying a pressure drop to the lowest feed pressure. This value is supplied in the PressuSpecification window, which is accessed by clicking Pressure Specification…the Splitter main data entry window. When a pressure drop is supplied, the resulting outlet temperature and phase condition are determined by an adiabatic flash calculation from the composite feed inlet conditions.

on

te Feed Rate Options

Thesatisfy abuttons Sat

cific e products until the feed is exhausted.

Satproduct the tota o flow. The ord

Inadequa

re are two options for situations in which insufficient feed is available to ll product stream rate specifications. They may be selected by radio on the Splitter main data entry window:

isfy Each Specification in Order Until Feed is Exhausted: Each ation is satisfied in the order of thspe

The product stream that encounters insufficient feed is limited to the feed available and the remaining products are assigned zero rates. (This is the default option.)

isfy Each Specification and Normalize Flowrates if Needed: All specified rate specifications are satisfied and the resultant rates are normalized tol feed rate. The product with the unspecified rate is assigned a zer

er of the product streams in the list box may be changed, if desired, by clicking Change Stream Specification Order… on the Splitter main data entry window ication by clicking Reset Stream . You can reset a stream specifSpecification on the Splitter main data entry window.

ynamic System

he thermodynamic system of methods to be used for splitter calculations may be selected by choosing a method from the Thermodynamic System drop-down list b

Thermod T

ox on the Splitter main data entry window.


Stream ator

Calcul

General Information

r uni r of feed streams and splits them duct streams with defined compositions and thermal condition. It may

lso be used to create a pseudoproduct stream based on the blended feeds or y defining

Product

The stream ca or may have any number of feed st s. Scale factors or negative) may be applied to all feeds in the Sca indow in

ate a mixed feed with the desire sition. If scale factors other us he u ill no erial b ce. Multiple feed ams are

the l st fee eam sure.

spl , bot he over and bottoms pro are required. In e a stream, a pseud product must be defined. The feeds may be

rodu ated in the sa tream calculator u it. If there is the unit, only a pseudo ct may be specified.

p ct fro the str calcu may b into streams ng one or more phase. Th wabl duct stream phases are vapor, ecanted water and mixed (vapor+liquid). A mixed phase product is not with a vapor or a liquid produ d water product is also used

as the second liquid product phase with rigo VLLE ations.

attached, the which is

he Stream Calculato t blends any numbeT

into two proab the amount of each component in the stream. Feeds and

s

lculat ream(positive ling wFeedorder to crethan 1.0 are

d compoed, t nit w t mat alan stre

flashed at

owe d str pres

For stream itting h t head ductorder to creat osplit and a pseudop ct cre me s nno feed to produ

aseA multiphcontaini

rodu m eam e allo

latore pro

e separated

liquid, dallowed ct. The decante

rous calcul If any product, overheads or bottoms, has more than one stream phases must be allocated to the streams in the Product Phases window, accessed by clicking Product Phases in the overhead or bottoms product windows.


Mode of Operation

he mode of operation is specified by the number of feeds and pro s attached the unit so it i important to co correc en

plitting

order to define the component splits, specifica must be entered in the Product Specific e ch of each component goes into

ead or the bottoms product. Specifications may be on single components or on ranges of contiguous components. Several specifications may be required and pecify the amount of compon e overheadand oth e amount in the bottoms pr t. E omp ent must appear one, and only o ation. e co ent rates, re very or co itio

a product may be specified.

The thermal condition of the products may optionally be defined in the Overhead roduct Conditi Bott Pro Conditions windoressure defaults to the lowest feed pres specification is upplied for either product, the product t ratures are set equal at a value alculated from the enthalpy bala e, us e d enter on the Stream alculator window. If one tempe ure is supplied, the other temperature is alculated to me balance. th eratu s are given, duty alculated.

emperature specifications may be a temperature value, the temperature rise bove the feed, dew or bubble point or a pro o dew or bubble point.

tream Creatio

order to defin o ct, sp atio ust entered in the duct Specifi window to much of each compouct. Specifications may be on single components or on ranges of

ontiguous components and sev pecifications may be required. A st opecification must be defined. Any s not appear in a

will be set to zero in the pseudoproduct. If the unit has feeds, omponent rates, recovery or composition in the product may be specified,

Otherwise, the c tes be defined

no feed to the unit, pseudoproduct thermal condition must be defined in e Pseudoproduct Conditions window. If there is a feed, the temperature and

ressure specifi ptio he su fault to lowest fessure and the temperature is ulat py balan

uty is supplied, it will be used only for the stream splitting enthalpy balance. Duty is not used for the pseudoproduct enthalpy balance.

T ducttly before to s nnect the streams tering the

unit data. Stream S In tions

ations window to defin how mueither the overh

some may s ents in th ers th oduc ach c on in

ne, specific Th mpon co mpos n in

ons window and the w. P oms ductPs

sure. If no temperature empe

c nc ing th uty edratC

c et the enthalpy If bo temp re is c Ta n ap ach t S n In e the pseudopr

cations du ecific

define hons m

w be

nent is Pseudopron the prodics

eral scomp

t lea ne onent which doe

specification c

omponent ra must .

If there isthp cations are o nal. T pres re de s ed pred

calc ed to satisfy the enthal ce. If a


emperature specifications may be a temperature value, the temperature rise bove the feed, dew or bu ble point or a pro o dew or bubble point. If ere is no feed ature sp atio nnot be used.

Negative Comp tes

is possible th it suc that tive component rates alculated in a p T appropriate n if this happens is selected

from:

• reset any negative rates to zero (this is the default) • reset th ir ab lute lue • the unit should fail.

hermodynam

he thermodyna m hods r the stream Calc r me selected by c tho from The ynam m drop-dowst box on the S lator ain d entr dow.

Ta b

, the tempern ap ach t

th rise ecific n ca

onent Ra It to specify e

roduct stream.un h nega are

c he actio

e rates to the so va

T ic System T mic system of et to be used fo ulato ay b hoosing a me d the n rmod ic Systeli m ata y wintream Calcu


SPEC/VARY/DE

eneral Info

RO/II has an e system of cross-referencing for flowsheet parameters. sheet para ude op ating nditio r unit operations, calculas from unit operations, and stream flows, compositions, and properties. For

xample, the su et pressure for a Pump, the calculated temperature for dew point Flas e simul d D8 inety perc istilled

temperature for roduct stream re al shee ameters

ost unit opera m y be either DEFI Ed o Cified ny other flowsh meter in the problem. S unit tions m AR flowsheet param rdina rema nsta the inp luehe table below e ethod for cro ferearameters:

PEC: A unit op am erformance s fication (calculated resultust meet a de lue, either on an solute s or relative basi .

VARY: A unit operation or stream heet parameter is varied from the supplied value.

EFINE: A unit operation param r is d ined by cross-reference to another er.

RO/II uses a c n for at fo he SPECifica VAR d DEFatures. Each f cuss pa tely below. Tab re also entith cross-refer bilities of the wshe rame for strea nde unit operatio

PECifications

y definition, a tion must alwa be a ated flowsheet r ult. Tllowing unit op se the nera d SPerformance of sh, Splitter, Column/Side Column, and Controller.

SPEC has the following g

arameter = value within the default tole nce

choice for the ter and a numer value must be liedlicking on the u hypertext strings to ga cess e pertin atntry fields. Optionally, the tolerance bas may ang the d lt tbsolute or rela defa tolera e val 0.02 replaced by direct

entry.

FINE G rmation P xtensive

meters inclFlowresult

er co ns fo ted

e pplied outl, and tha h ate 6 n -five ent d

a Column p a l flow t par . M tion parameters a r SPE relative to

ay VN

ome a eet para opera Y . a eter that would o

summarizes trily in co nt at ut va

T h m s ss-re ncing flowsheet p S eration or stre p peci ) m sired va ab basi s

flows

D ete efflowsheet paramet

P ommo meature is dis

r t tion, Y, an INE fe ed se ra les a pres ed w ence availa flo et pa ters ms a th ns. S B SPECifica ys calcul es he fo erations u ge lize EC format to define the p the unit: Fla A eneral form: P ra A Parame ic entry for the supp by c nderlined in ac to th ent d a e is be ch ed from efau o a tive and the ult nc ue of


Click on the Parameter hypertext to access the Parameter window. Choose the Stream or Unit from the drop-down list box. Select the unit or stream name in the drop-down list box. Finally, on he Para ter hypertext and sele re

parame e wind that displa Note only those unit or stream that valid r use s a SPEC are available.

the SPEC is not related to another flowsheet p eter

click tter from th

me ct the desi d ow is yed. that

parameters are fo a If aram :

Click OK to return to the unit specificatio Click on hypertext, and enter the desire c value for

SPEC. To create a mathematical expression for the SPEC:

Select the = sign linked text and select an option from the pop-up window. Choices are as follows:

o Operator Primary parameter only (the default) + Operator

rimary parameter plus reference parameter

Operator rimary parame arameter IFFERENCE)

rator ry parameter divided by reference parameter (RATIO)

Operator rimary parame referen para ter (TIMES)

ct the Reference Parameter and click on the Parameter text string, and sele ed reference parame ch is displaye

ote: Only thos r st am parameters whi e valid for a specification re available.

n. the value d numeri the

N

P(SUM) - P ter minus reference p(D / Ope

rimaP xP ter tim s e ce me

Select the desird.

ter from the list whi

N e unit o re ch ara

Click O turn to the it spe on window click o value linked text string to enter the desired numer lue for t PE

K to re un cificati ; then n theic va he S C.


The following examples illustrate e use f SPE

xample 1: Re ssu of stream S 6.0

nit or stream parameter = a value withi relat lerance of 0.02 | |

| [6.0] pecification

Unit/Stream Stream Name {Parameter Windo [Strea [S103

arameter [Vapor Pre

xample 2: Du xchanger X103/ Duty of exchanger X104 = 1. 0.001

r stream parameter = a value within a relative tolera e of 0.02

| | | | .0] [absolute

Specification Unit/Stream Unit Nam {Parameter W ow}

[Heat Exch r] [X103] arameter

[Duty]eference: [/ P

nce Parameter Unit/Stream Unit Name {Parameter Window}

[Heat Exchanger] [X104] arameter

[Duty]

[ ]denotes user input.

ARYs

or each SPEC u be on RY or degree of freedom.he VARY for th it is im licitly fined, not d d expli y ser. For Flash ith specifications, the degree of freedom is the mperature wh p essure o press drop is given and the pres wh n e temperature d. Other unit O ratio ich h ve VARYs are the

n and the Controller. A VARY is always a flowsheet arameter that has a rsus calculated value in the flowsheet.

th o Cs:

E id Vapor Pre re 103 = U n a ive to

Sw}

m] ] P

ssure] E ty of e 0 +

Unit o nc | [1 ] [0.001]

e indange

P

R arameter =] Refere

P

Note: V F in a flowsheet, there m

e Flash unst e VA

the T p de i.e., efine citly bu units w

en thete r is supplie

r ure sure eth pe ns wh a Column/Side Colump fixed ve


For Columns/Side Columns a VARY ma e a fe tream , produ awte, or a heat duty. For example, the lean oil feed rate to a column may be

efined as a VA order to meet a sp ificati the propane recovery foe column. Ord lean o feed rate wou ve a or con ra

in the flowsheet

ontrollers have VARYs that are associated with other unit operations. For xample, the su re fo Com or may be a VAR r aontroller. Note heet parameter w have a fixed or onstant value in the flowsheet. On the other hand, the ca ted temperaturr a dew point unit could not be u d as a VARY, s this is a sh

arameter that i ed by flow eet ca tions

VARY has the

Vary Parameter

ter a parameter:

Click on ertext string t cess e ow From this window, select the type of vary, i.e., stream or unit t in t

drop-down list box. Next, se it or s am name in t e adjace op-dow list box. Finally, e Para ter hypertext string an sired

parameter to be varied f the list.

ote: Only thos r stream parameters whi re valid for use as VARYre available.

he following example illustrates the use of VAR

xample 3: The ture for isothermal flash unit is varied by aontroller.

ary unit or stre ter | |

n Unit/Str t Name {Variable Wi } [Flash] [D101] Parame[Temperature]

ote: [ ]denotes user in

y b ed s rate ct dr rad RY in ec on on r th inarily, the il ld ha fixed stant te

. Ce pplied outlet pressu r a Y fo press

that this flows ould ordinarily Cc lcula e fo se ince flow eet Flash p s determin the sh lcula . A following general form:

To en

the underlined hyp o ac the Variabl wind . ype, he

lect the un tre h nt dr n click on th me d select the de

rom N e unit o ch a a a T Ys: EC

tempera D101

V am parame

Specificatioeam Uni

ndow

ter

put.N


DEFINE

he DEFINE is used to dynamically define the value for a flowsheet parametely has a fixed versus calculated value in the flowsheet. Thus, the

alue for a unit operating be set to a value that is based on a alculated flows eter. r exa le, th FINE y be us et

the temperature al Flash to the temperature that is calculated fompressor ou plus 1 re . This ept ly enha the

flowsheeting ca RO/II, and, in ct, ne ever operat n inpuarameter may

o define a flow et

Select the parameter in the appropriate window for the unit operation.

T r that ordinariv condition may

heet param Fo mp e DE ma ed to sc for an isotherm or a tlet stream 0 deg es conc great ncesCpability of P fa arly y unit io t

p be DEFINEd in PRO/II. T sheet param er:

At this point, the Define button on the toolbar is activated if the parameter may be lick fine to access the Definition window.

From thi , selec e che e EFINE ns. Click on meter t t strin nd s the desired parameter fr

the wind is disp yed.

ote: Only thos ream parameters whi e valid for use as a DEFIre available.

DEFINEd. C Des window t th ck box to enabl the D optio the Para ex g a elect om ow which la

N e unit or st ch ar NE a

If the D not rela eet eter cli k OK treturn to the unit window. If the DEFINE lated other f wsheeparame lish the p te ma atica tionship. Mathem ession for a FINE crea a mancomple ous to that described e on 309 fo PE .

Select t ar eter e in t me m er as uselect th am er.

EFINE is ted to another flowsh param c o is re to an lo t

ter, estab appro ria them l relaatical expr s are ted in ner DE

tely analog abov page r a S Che reference p

param typ he sa ann sed to

e primary et Click th n the child windows to return to the unit operation

window

or a constant:

Select C the onstant/Stream/Unit drop-down list box in the Parame

Enter a nstant in the suppli ta enhe following example illustrates the use of a DEFINE:

xample 4: DE tempe ure for Flash drum D103 to be the temperature of S104 minus 15 gree

elect the temp n t Flas econ ecification]

e OK button i .

F

onstant from Cter window. numerical co ed da try field.

T E FINE the rat

stream de s. [S erature field o he h S d Sp[Click Define from the Toolbar] [Select the check box to set up the Define]


| Primary Parameter: Unit/Stream/Constant Unit Name {Definition Window} [Stream] [S104]

eference: [= Parameter - Parameter]

l in structure to the SPEC.

Parameter [Temperature]

RReference Parameter: Unit/Stream/Constant Value [Constant] [15.0] Note that the DEFINE is nearly identica

Stream Parameters Available for Cross-referencing SPECS DEFINE1 VARY2

Parameter Flash Splitter Column Controller All Units Controller

Temperature Yes - Yes Yes Yes Yes Pressure Yes - Yes Yes Yes Yes Enthalpy Yes - Yes Yes Yes - Mole Weight Yes - Yes Yes Yes - Total Flow Yes Yes Yes Yes Yes Yes CFl

omponent Yes Yes Yes Yes Yes - ow

Composition Yes - Yes Yes Yes - Phase Fraction Yes - Yes Yes - Density/Volume Yes - Yes Yes Yes - Distillation

urve Yes - Yes Yes Yes -

CVapor Pressure Yes - Yes Yes Yes - Transport Property

Yes - Yes Yes Yes -

Refining roperty

Yes - Yes Yes Yes - PSpecial User Yes - Yes Yes Yes - Property 1 Note that not

In general, any applicable stream property may be used to define a unit operating condition. all stream properties are applicable to all unit operating conditions.

2 With the exception of the Column, only the Controller may vary stream parameters. The Column may vary the total flow of a feed strean.


Unit Parameters Available for Cross-referencing

Within Operation

External Controllers

Unit Parame

ter SPEC VARY DEFINE Reference1 SPEC VARY

Calculator Result - Yes Yes Yes Yes Yes Parameter - Yes Yes Stream Calculator

Temperature - Yes Yes - Yes Yes - Yes Yes - Yes Yes Pressure - Yes Yes - Yes Yes

Delta T - Yes Yes - Yes Yes Temp. Below

Bubble Pt. - Yes Yes - Yes Yes

Temp. Above Dew Pt.

- Yes Yes - Yes Yes

Delta P - Yes Yes - Yes Yes Feed Cofactor - Yes Yes - Yes Yes Duty - Yes Yes Yes Yes Yes Frac. Overhead - Yes Yes - Yes Yes Frac. Bottoms - Yes Yes - Yes Yes Frac. Product - Yes Yes - Yes Yes Overheat Rate - Yes Yes - Yes Yes Bottoms Rate - Yes Yes - Yes Yes Product Rate - Yes Yes - Yes Yes Comp.

Overhead - Yes Yes - Yes Yes

Comp. Bottoms - Yes Yes - Yes Yes Comp. Product - Yes Yes - Yes Yes

Controller Yes Yes Yes Yes Yes Specification

MVC

Specification Yes Yes Yes Yes Yes

Optimizer Specification Yes Yes Yes Yes Yes

Constraint Yes Yes Yes Yes Yes


Column

Reflux Yes Yes Yes Ye s Yes Yes Reflux Ratio Yes Yes Yes Yes Yes Yes s Yes Yes Yes Yes Duty Yes Ye Feed Rate - Yes Yes Yes Yes Draw Rate - Yes Yes Yes Yes Specification - - Yes Yes Yes Percent of Flood - - Yes Yes Yes Yes Max % of Flood - - Yes Yes Yes Yes Downcomer B/U - - Yes Yes Yes Yes Max D.C. B/U - - Yes Yes Yes Yes CS Approach

- - Yes Yes Yes

Flood Approach - - Yes Yes Yes Tray Diameter - - Yes Yes Yes Yes

Max Tray Diam. - - Yes Yes Yes Yes Condenser Pres - - Yes Yes Yes Top Tray Pres - - Yes Yes Yes Tray Delta P - - Yes Yes Yes

Column Delta P - - Yes Yes Yes Tray Temp - - Yes Yes Yes Yes Feed Tray No - - Yes Yes Yes Yes Draw Tray No - - Yes Yes Yes Yes Duty Tray No - - Yes Yes Yes Yes Tray Effy Factor - - Yes Yes Yes Yes P/A Rate - - Yes Yes Yes P/A Return T - - Yes Yes Yes Product Moles - - Yes Yes Yes Thermosiphon Reboiler Circulation Rate - - Yes Yes Yes Yes Vapor Fraction - - Yes Yes Yes Yes Liquid Fraction - - Yes Yes Yes Yes Outlet Temp - - Yes Yes Yes Yes Delta T - - Yes Yes Yes Yes LLEX Specification - - Yes Yes Top Tray Pres - - Yes Yes Feed Rate - Yes Yes Yes Draw Rate - Yes Yes Yes Duty - Yes Yes Yes Pump Temperature - - Yes Yes


Outlet Pres - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Pres. ratio - - Yes Yes Yes Yes Work - - Yes Yes Head - - Yes Yes Efficiency - - Yes Yes Pipe

Diameter - - Yes Yes Yes Yes

Max velocity - - Yes Yes Yes Yes Average velocity - - Yes Yes Yes Delta P - - Yes Yes Yes Duty - - Yes Yes Yes Yes Rel Roughness - - Yes Yes Yes Abs Roughness - - Yes Yes Yes Friction Factor - - Yes Yes Yes Flow Efficiency - - Yes Yes Yes Length - - Yes Yes Yes Heat Transfer

Coeff. - - Yes Yes Yes

Ambient Temp - - Yes Delta P Max - - Yes K-Factor - - Yes Yes Simple Exchanger Duty - - Yes Yes Yes Yes Cold Delta P - - Yes Yes Yes Yes Cold T Out - - Yes Yes Yes Yes Cold Liq Fr - - Yes Yes Yes Cold Subcool - - Yes Yes Yes Cold Sup’heat - - Yes Yes Yes Hot Delta P - - Yes Yes Yes Yes Hot T Out - - Yes Yes Yes Hot Liq Fr - - Yes Yes Hot Subcool - - Yes Yes Hot Sup’heat - - Yes Yes LMTD - - Yes Yes Zoned LMTD - - Yes Yes Overall U - - Yes Yes Yes Yes Area - - Yes Yes Yes Yes U * Area - - Yes Yes Yes Yes actor Yes Yes Yes Ft F - - Yes s Yes Yes Approach - - Yes Ye Yes MITA ( ch - - Yes Pin )


Yes Yes Yes Min. Approach - - Yes Rigorous Heat Exchanger Duty - - Yes Yes Yes Yes Overall U - - Yes Yes Yes Estimated U - -

Area - - Yes Yes Yes Yes U*Area - - Yes Yes Yes

LMTD - - Yes Yes Shell T Out - - Yes Yes Yes Yes Tube T Out - - Yes Yes Yes Yes Tube Foul Factor - - Yes Yes Yes Yes

Shell Foul Factor - - Yes Yes Yes Yes Required Foul

Factor - - Yes Yes Yes

LNG Heat Exchanger Duty - - Yes Yes

T Out Yes Yes Yes - - Yes le Str m

Duty Yes Yes Yes Sing ea - - Yes

Yes Yes Delta P - - Yes Yes Yes U*Area - -

LMTD - - Yes Yes MITA - - Yes Yes Splitter Temperature - - Yes Yes Yes Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Specification - - Yes Valve Temperature - - Yes Yes Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes C

ompressor

Outlet Temp - - Yes Yes Yes Yes Outlet Pres - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Compr. Ratio - - Yes Yes Yes Yes Actual Work - - Yes Yes Yes Yes Head - - Yes Yes Yes Yes Adiab. Effy - - Yes Yes Yes Yes


Poly Effy - - Yes Yes Yes Yes Max. Press - - Yes Yes Cooler DP - - Yes Yes

Cooler Temp - - Yes Yes Temp Estimate - - Yes Yes RPM - - Yes Yes Yes Curve RPM - - Yes Yes Yes Expander Outlet Temp - - Yes Yes Outlet Pres - - Yes Yes Yes Yes - - Yes Yes Yes Yes Pressure Drop Expans. Ratio - - Yes Yes Yes Yes Yes Yes Yes Actual Work - - Yes Head - - Yes Yes Yes - - Yes Yes Yes Yes Adiab. Effy - - Yes Yes Min. Pressure Flas

- h

Temperature - - Yes Yes Yes Yes Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes

Duty - - Yes Yes Yes Yes Specification - - Yes Entrainment - - Yes Yes Pseudo Prod. - - Yes Mixer Temperature - - Yes Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes

Specification - - Yes Pump re - - Yes Yes Yes Temperatu

es - - Yes Yes Yes Yes Outlet Pr

- - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Press Ratio - - Yes Yes Work - - Yes Yes Head - - Yes Yes Efficiency Equi i

libr um Reactor

Temperature - - Yes Yes Yes Yes


Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Duty - - Yes Yes Yes Yes Conversion - - Yes Yes Yes Yes Stoic. Coeff. - - Yes Conv

ersion Reactor

s Yes Yes Yes Temperature - - Ye Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Yes Yes Duty - - Yes Yes Yes Yes Conversion - - Yes Yes Yes Yes Gibbs T ure - emperat - Yes Yes Yes Yes Pre - ssure - Yes Yes Yes Yes D - - elta P Yes Yes Yes Yes Dut - - y Yes Yes Yes Yes PFR Te ure - mperat - Yes Yes Yes Yes Pressure - - Yes Yes Yes Yes Delta P - - Yes Yes Inlet Pres. - - Yes Yes Delta P In - - Yes Yes Duty - - Yes Yes Yes Yes Tube Diameter - - Yes Yes Length - - Yes Yes No. of Tubes - - Yes Yes U - - Yes Yes Max Veloc. - - Yes Yes Yes Temp In - - Yes Yes Yes

Temp Out - - Yes Yes Pre-exp. Factor - - Yes Yes

Activation E - - Yes Yes Yes Conversion - - Yes Yes Yes CSTR/Boiling Pot Temperature - - Yes Yes Yes Yes Pressure - - Yes Yes Yes Yes

Delta P - - Yes Yes Yes Yes Duty - - Yes Yes Yes Yes Conversion - - Yes Yes

Pre-exp factor - - Yes Yes Yes Activation E - - Yes Yes Yes Volume - - Yes Yes Yes


Min. Temp. - - Yes Yes Max. Temp. - - Yes Yes Max. Veloc. - - Yes Yes Depressuring Final Pres. - - Yes Yes Yes Yes Relief Pres. - - Yes Yes Yes Final Time - - Yes Yes Yes Yes Relief Time - - Yes Yes Yes Relief Duration - - Yes Yes Yes Yes Valve Constant - - Yes Yes Yes Valve Back P. - - Yes Yes Valve Coeff. - - Yes Yes Yes Critical Flow - - Yes Yes

Factor Yes

Init. Wetted A - - Yes Yes Yes HT Area - - Yes Yes Yes HT Coeff - - Yes Yes Yes HTC Fac - - Yes Yes Yes Vapor HTC - - Yes Yes Yes Liquid HTC - - Yes Yes Yes Coeff C1 - - Yes Yes Yes Coeff C2 - - Yes Yes Yes Coeff C3 - - Yes Yes Yes Coeff C4 - - Yes Yes Yes Coeff C5 - - Yes Yes Yes Final Temp - - Yes Yes Yes Final Duty - - Yes Yes Yes Final Vent Rate - - Yes Yes Yes Vess. Vol. - - Yes Yes Liquid Holdup - - Yes Yes Vess. Diam. - - Yes Yes Vol. Corr. Fac. - - Yes Yes Ht. of Holdup - - Yes Yes Vess Weight - - Yes Yes Vess. CP - - Yes Yes Tan-tan Vess.

Length - - Yes Yes

Tan-tan Vess. Height

- - Yes Yes

Time Step - - Yes Yes Isen Eff. - - Yes Yes Yes Heat Scal. Fac. - - Yes Yes Yes Area Scal. Fac. - - Yes Yes Yes 1 Available for any SPEC or DEFINE.


User-added Unit Operations

General Information The PRO/II User-added Unit Operation capability enables users to add their own

of unit operation or to perform alculations on flowsheet parameters. The subroutine must first be linked into the

The User-added Unit Operation has access to the PRO/II physical property data

vailable. See ’s Guide for

info a ation subroutines. The devadd uired for c

ot If in the User-added Unit Operation, you

on the PFD, the User-added must select the name of the

User-added Unit Operation may be executed during the flowsheet e only. The User-added Unit Operation

lculated. This affects

FORTRAN subroutines to simulate any typecPRO/II program and it is then accessed via the graphical user interface in thesame way as any other unit operation.

and may call the PRO/II flash and property calculation subroutines. Other information, such as input and output dimensional units, is also a

e PRO/II Data Transfer System and User-Added Subroutine Userthrm tion on writing and interfacing User-added Unit Oper

eloper of the User-added Unit Operation can also customize the User-ed Unit Operation Data window to request only data which may be reqthe alculations.

N e: transport properties are requiredmust select a suitable method in the Thermodynamic Data. Selecting the Subroutine When a User-added Unit Operation is laid down

nit Operation window opens in which the userUrequired subroutine. Calculation or Output Execution Aconvergence calculations or at output tim

ata window will show when the selected subroutine is caDwhether feeds and/or products are allowed. The default is to perform the calculations for the user-added unit as part of the normal flowsheet convergence calculations.


Calcula e normal ional calculations may be performed at utput time and an output report may be produced.

utput time: If the User-added Unit Operation requires only converged tput time

ation may have up to ten feed streams. The ubroutine can retrieve each feed separately. They are not mixed or flashed. If

st do this in the subroutine. User-added Unit ted during the flowsheet convergence must

nce may have up to ten product streams. These may be any

re than one feed or product, they will be sho laid down on the PFD. The user may need

reorder the streams so that they are presented in the correct order to the User-ays

cond.

tion time: The User-added Unit Operation is calculated as part of thflowsheet convergence. Addit

o Oflowsheet data for calculations and reports, it can be executed at ouather than during the flowsheet convergence. r

Feeds and Products The User-added Unit Opersthey are to be mixed, the user mu

perations which are to be execuOhave at least one feed stream. Those which are only executed at output timeneed not have any feeds. User-added Unit Operations which are to be executed during the flowsheet onvergec

combination of phases. User-added Unit Operations which are only executed at output time cannot have any product streams.

tream Reordering S

ded Unit Operation has moIf the User-adwn in the order in which they were

toadded Unit Operation. For example, the User-added Unit Operation may alwfeed vapor to the first product stream and liquid to the se Reordering is done in the User-added Subroutine - Stream Reordering window accessible by clicking Reorder Streams on the User-added Unit Operation Datawindow. Entering Data Data are supplied to the User-added Unit Operation in four tables:

• Real Data • Supplemental Data • Integer Data • Heat Balance Data

her a “Customized Data Entry Window” or the standard “Developers Data Entry Window.” These two choices are explained below.

Data can be supplied to a User-added Unit Operation using eit


Data may also be entered into the variables in the Real Data table using tPRO/II Define feature. The variables in the Real Data table are also available to other unit operations by means of SPECs, VARYs and DEFINEs. The other tables “Customized” Data Entry Window

he

dard PRO/II User-added Unit Operations use the default names USER41 - USER60 (displayed as US1-US20). If you create a customized

ation subroutine, the name that is selected for it will replace one of the default names in the list of available

d ted in the directory specified

y the “UserConfigDir= entry in the PVISION.INI file. These two files are called UASLIST.INI and USERXX.INI and are described below. File UASLIST.INI

ntains the user-specified names for specific user-added calculation ubroutines that will be displayed in place of the default names US1 - US20,

sponding to the subroutines USER41 - USER60. Each line in the file has o entries; the entry number in the list of user-added subroutine names, and the

actual text that is to be displayed for example of a typical U

1. 2. ating Value

These entries in the UASLIST.INI file will result in the following list of available user-added calculational subroutines being displayed when a User-added Unit Operation is laid down on the PFD:

A user has the option of defining a “Customized Data Entry Window” to be used for all user-added unit operations that utilize a specific user-added calculation subroutine. The stan

data entry window for a user-added calcul

subroutine names that is displayed when a user-added unit is laid down on the PFD. Creating a “Customized” Q Data Entry Window To create a customized data entry window to be used for a specific user-addecalculation subroutine, two ASCII files must be creab

This file coscorretw

the user-added subroutine. AnASLIST.INI file is shown below:

PIPE DP Routine Stream He


File USERXX.INI This file contains the variable names and array locations for all of the Real,

pplemental, Integer, and Heat Balance Data values that the specific user-ded calculation subroutine requires or that can be input by the user. For a er-added subroutine with a customized data entry window, a user will only be le to enter values for the data items specified in this file. The “XX” in the name

the USERXX.INI file corresponds to the respective user-added subroutine referenced, i.e. the user-added subroutine USER41 with a user-specified name of “PIPE DP Routine” above would need a “USER41.INI” file to describe the

quired data for the calculations. An example of a typical USERXX.INI file is own below:

ample USER41.INI file:

iPPrint ControllN Required RPARM 1 iPDiameter (in)lm Required

PARM 2 iPLength (ft)lg Required

SUPPLE 1 “No. Of Segments” Required ...

ry on each line indicates to which data array the variable belongs. The second entry is the array number where the data value entered by the User

ill be stored for access by the User-added calculational subroutine.

e third entry is the label to be displayed for the variable in the customized data try window. This entry must be enclosed in double quotes (“”).

e fourth entry on each line indicates whether or not data entry for the item is ptional or is Required. The default is Optional, and this entry is not required.

e entries in the USER41.INI file shown above will result in the following required data values and variable names being shown in the custom window displayed for data entry, for any User-added Unit Operation where the user-

lected “PIPE DP Routine” as the user-added subroutine when the unit was laid wn on the PFD as shown below.

tomized UAS Data Entry Window The order in which the variable labels appear on the customized User-added Unit Operation Data window is the same as the order in which they appear in the USERXX.INI file.

the number of variables that can be entered for each array are shown below. These limits are:

Suadusabof

resh Ex IPARM 1

R...

The first ent

w Then ThO Th

sedo Cus

The limits on


• Real Data - up to 500 elements • Supplemental Data - up to 10,000 elements • Integer Data - up to 250 elements • Heat Balance Data - up to 10 elements

Each table shows the name(s) of the variable(s) for which values must be entries

displayed using a customized data entry window are required. No checks on validity or completeness of the data are carried out until the User-added Unit Operation is executed.

er’s Data Entry Window

. It is ized

Data Entry Windo

at Balance Data - up to 10 elements

which elements of each array are used by the User-added r the array element number along with the value. Values

d

RO I bout the data requirements of a User-added Unit Ope ti rictions are imposed in the data entry.

e: Unless the user defines a custom Data Entry Window for a specified User-dded Unit Operation, the data entry for that unit will be via the developers data

entered. They will scroll if they contain more than four rows. All data

The Standard Develop

A special window is available for developers of User-added Unit Operationsthe default window displayed for a User-added Unit Operation if a “Custom

w” has not been defined for the specific unit. The developer’s data entry window has no variables names and any number of variables may be entered up to the limits of each array. These limits are:

• Real Data - up to 500 elements • Supplemental Data - up to 10,000 elements • Integer Data - up to 250 elements • He

The user must know

nit Operation and enteUmay be entered for any or all of the elements in the arrays. The elements defineneed not be contiguous and may be entered in any order. P /I knows nothing a

ra on and so no rest Notaentry window.


Electrolyte Module

ipe changer, LNG heat exchanger ctor, Equilibrium reactor

• Column (Electrolytic Algorithm, see below)

hermodynamic Models

ight built-in electrolyte models in PRO/II simulate aqueous systems in a wide nge of industrial applications. The models apply to fixed component lists with a

redefined set of thermodynamic methods for K-values, enthalpies and densities. is not possible to define individual methods for K-value, enthalpy or density hen using electrolyte thermodynamic models.

ote: Electrolyte models may not be used to calculate the following properties: ) Nonaqueous electrolyte systems; (2) Free water decant; ) Water dew points; (4) Hydrocarbon dew points, (5) Entropy and heat capacity.

he following electrolyte models are available in this release:

• Amine Systems • Acid Systems • Mixed Salt Systems • Sour Water Systems • Caustic Systems • Benfield Systems • Scrubber Systems • LLE and Hydrate Systems

General Information The optional Electrolyte Module of PRO/II allows you to handle systems containing electrolytes. See the PRO/II Add-On Modules User’s Guide for more information. The following unit operations can be used with this electrolyte version:

• Flash • Pump • Valve, Mixer, Splitter • P• Simple heat ex• Conversion rea• Stream calculator • Heating/Cooling curve • Calculator • Controller, Optimizer

T ErapItw N(1(3 T


To select an electrolyte model:

• Click Themodynamic Data on the toolbar to open theThermodynamics Data main data entry window.

• Select the Electrolyte option in the Category list box. • Choose an appropriate electrolyte model.

The suggested range of applic

ability for the electrolyte models is summarized below:

ressure: 0-200 atm ole %

Ionic solute 0-30 ionic strength

e PRO/II and the Electrolyte Utility Package (EUP). If you wish to do this, rt office for more information.

Notmethod different

nthalpy re sed, PRO/II automatically takes care of the difference but it may appear to be

confusing. To avoid this, select the electrolyte enthalpy method for all nonelectrolyte thermodynamic systems in a mixed application. All systems will then use the electrolyte model basis. Electrolytic Column Algorithm (ELDIST) This column algorithm was designed to solve nonideal aqueous electrolytic distillation columns involving ionic species. It uses a Newton-Raphson method to solve the mass balance, vapor/liquid equilibrium and specification equations simultaneously. The K-values and enthalpies are supplied by the electrolyte thermodynamic model. The Electrolytic Column Algorithm is selected from the Column Algorithm drop-down list box on the Column main data entry window. Note: Electrolytic thermodynamic models only support VLE and so total phase draws are not permitted.

Temperature: 32-390 F (0-200 C) PDissolved gases: 0-30 m

s: Amine Systems Pressure: 0-30 atm LLE Systems Organic solutes: 0-10 weight % You may add your own models, specifically suited to your application, by using thcontact your nearest SIMSCI suppo

e: Take care when using nonelectrolyte and electrolyte thermodynamic s in the same application. The PRO/II electrolytic models use a basis from that used for other thermodynamic systems. When both ae

u


Advantages and disadvantages of the Electrolytic Column Algorithm are given below: Advantages (1) Rigorously models ionic equilibrium systems. (2) Solves highly nonideal distillation columns. Disadvantages (1) Side columns are not supported. (2) Pumparounds and tray hydraulics are not available. (3) Certain Column Specifications and Variables are not permitted.


Simsci Add-on Modules

Add-on modules can be obtained in th /II to extend the functionality of the program. These m les include units for modeling polymer systems, separating solid component s with different component and refinery insp tics hydrotreating and reformer reactor mo SIMSCI POLYMER CSTR Unit Oper

ins features for handling ty prediction method, polymer moment a d, and polymer flash). The SIMSCI Polymer CSTR Add-on M deling a polymerization reactor operating unde

• Single monomer producing a • Single phase reaction (effects of heat and mass transfer on the mass

are not considered)• Ideal CSTR (steady-state, we• Free radical polymerization ki• Bulk or solution polymerizatio

This reactor unit has been added to PRO/II as part of the SIMSCI Add-on Models

m SIMSCI as the SIMSCI Polymer CSTR

Required Data for the Polymer Reactor Unit This version of PRO/II does not allow you to enter the necessary Component, Stream, or Thermodynamic Data via required the data entry windows. However, you can enter the necessary Polymer CSTR data using the Polymer CSTR data

ow for the SIMSCI Add-on Model.

To enter data for the Polymer CSTR:

data for the Polymer ent

is version of PROodus from feed streams, blending streamection properties, as well as Profimadels.

ation

PRO/II conta polymers (e.g., van Krevelen properttributes, ALM thermodynamic metho

odel offers you the capability of mor the following conditions:

linear homopolymer.

transport . ll-mixed, constant volume reactor). netics. n.

(Polymer CSTR) and is available fromodule.

entry wind

Once you have entered your simulation data, including theCSTR, but excluding any polymer-specific thermodynamic, stream, or compondata, you will need to do the following:


.

• Add the necessary polymer-specific data to the keyword file. lation

problem in Run-Only mode. For add ide.

SIMSCI COMPONENT PROPERTY REPORTER Unit Operation

rints out the Component Properties and Refinery Inspection Properties r all the thermodynamic methods in the current flowsheet. This unit is selected

a entry window. o data input is required.

IM

he Blend unit allows you to blend two or more streams to give one product tream with different component and refinery inspection properties. This unit is

CI Add-on Units main data entry indow.

nction correctly, but this is not necessary. The unit thermodynamic method ust be different from any of the feed stream thermodynamic methods.

he following data must be provided:

• Product stream temperature.

The product stream pressu lied, but if it is not given, the ressure will be set to the lowe ressure.

The unit thermodynamic method component properties will be recalculated from the blend of the feed streams propert art of that thermodynamic method data storage. Only petroleum and assay generated

onent properties will be recalcul mponent properties do not change in the flowsh et. The unit first recalculates the normal

point, molecular weight and sp components. These recalculated prop hen used to recharacterize all the other petroleum fraction propertie s the critical temperature.

• Export the simulation data to a PRO/II keyword file

• Import the modified keyword file into PRO/II and run the simu

itional information, refer to the PRO/II Add-On Modules User’s Gu

This unit pfofrom a drop-down list box on the SIMSCI Add-on Units main datN

S

SCI BLEND Unit Operation

Tsselected from a drop-down list box on the SIMSw The feed streams should have different thermodynamic methods for this unit to fum T

re may also be supp

st feed stream pp

ies and will then be stored as p

comp ated; it is assumed that Library coe

boiling ecific gravity for all the petroleumerties are t

s such a


Using the Blend Unit with Refinery Inspection Properties Any refinery inspection properties specified in the input will also be blended from the feed streams properties using the property. It is necessary that every the method must have the same refinery inspection properties specified and that these properties must use the ame property method and blending basis in order for the unit to work. A check is

done at input time to check that all the methods in the problem have the same finery properties, methods and bases specified. You can request this check to

s

ration

The are required to spe ble point or vapor

ac ditions will be calculated s are entered

field and are as follows:

feed stream temperature 2 Specify the product stream at the feed stream enthalpy

ion temperature le temperature

Notmethod is different from the thermodynamic method of any of thfor the RESET unit, the BLEND unit and any Profimatics reactor models.

specified blending method for that rmodynamic

s

rebe done, at calculation time, on the methods used in the current unit using the IPARM entry. Note: Requesting this check at calculation time should be used with care and inot recommended. SIMSCI RESET Unit Ope The RESET unit allows you to reset the product stream enthalpy datum using the thermodynamic method specified within the unit. This unit is selected from a drop-down list box on the SIMSCI Add-on Units main data entry window. Only one feed and one product stream are allowed for the unit. Note: If you try to import a keyword file that specifies more than one feed or product stream, PRO/II will produce an input error.

feed stream pressure is always kept constant and youcify whether the temperature, enthalpy, dew point, bub

frb

tion is kept constant. The new product stream conased on the option specified. The available calculation option

through the first value in the Integer Data for Unit Value Entered Calculation Option

1 Specify the product stream at the

3 Specify the product stream at the feed stream vapor fract4 Specify the product stream at the dew5 Specify the product stream at the bubb

e: In this version, a warning message will alert you if the thermodynamic of the unit operation

e feed streams. This warning message applies to all unit operations except


SIMSCI Profimatics Reactor Unit Operations

and Reformer Reactor unit perations and can be selected from a drop-down list box on the SIMSCI Add-on

These units model Profimatics Hydrotreater oUnits main data entry window.


Valve

Gen The urs

o te, etc. The temperature

va let re

or is automatically set by PRO/II. For

eral Information

Valve is used to model the Joule-Thompson effect that occacrfo

ss a pressure restriction such as a valve, orifice plar the exit fluid is computed by assuming that the operation is adiabatic.

Rigorous calculations may be performed for both VLE and VLLE systems. Feeds and Products A lve operation may have multiple feed streams, in which case the in

ssure is assumed to be the lowest feed stream pressure. p A valve may have one or more product streams. The product phase condition falve operations with one product streamv

valve units with two or more product streams, the product phases must be specified in the Valve Product Phases window which is accessed by clicking Product Phases… on the Valve main data entry window.

roduct phases allowable include: vapor, liquid, decanted watePa

r, heavy liquid, nd mixed phase (vapor plus liquid). Mixed phase is mutually exclusive with

vapor and liquid products and is not allowed when four product streams are specified. Outlet Conditions The outlet condition for a valve is selected with the appropriate radio button on the Valve main data entry window as:

• Pressure drop • Outlet pressure

Thermodynamic System The thermodynamic system of methods to be used for valve calculations may be selected by choosing a method from the Thermodynamic System drop-down list box on the Valve main data entry window.


Wiped Film Evaporator

General Information The Wiped Film Evaporator unit operation (WFE) provides the capability to model the separation of solvents and/or monomers from a polymer melt. A Wiped Film Evaporator should be used when the removal of volatiles from a viscous polymer melt is diffusion limited. The blades inside the wiped film evaporator continually mix and spread a thin film of the melt on the wall of the evaporator. As the melt moves down the evaporator, the volatiles diffuse out of it and into the vapor space of the evaporator. The volatiles are pulled out of the evaporator under vacuum. Detailed Information For detailed information regarding operating modes, data requirements, and range of applicability of the Wiped Film Evaporator model, consult the PRO/II Add-On Modules User’s Guide.


Chapter 10 Running and Viewing a F

se breakpoints, and view calculation history and results.

interaction with the simulation (running the simulation by stepping nce or simulation results. You access ate button on the Run palette. If all

lowsheet This chapter describes how to run a simulation, interactively change the alculation sequence, uc

sing the Run Palette U

The PRO/II Run palette shown in Figure 10-1 provides options for data erification, v

through the units) and viewing convergehese features by choosing the approprit

req when you choose Run, PRO/II will disp complete.

o

sappears on the PRO/II main window.

uired input data have not been providedlay a warning message telling you which data are in

T display/hide the Run palette:

Select/deselect the View/Palettes/Run option from the menu bar. The Run palette appears/di

Chapter 10 RUNNING AND VIEWING A FLOWSHEET 341

Figure 10-1: Run Palette

he palette displays push buttons that execute or access a feature: T

Operation Description

Status Displays the global messages for the current simulation.

Check Data Checks the input data to determine whether there are any data inconsistencies.

Run Executes the simulation, either from the beginning or from a breakpoint. irCheck Datalc is automatically performed, if necessary.

Step Steps through the execution of the simulation by stopping at each unit operation in the calculation sequence.

Stop Interrupts or stops the simulation while it is executing. The program completes its current calculation before stopping.


Set Breakpoints Selects the units you want to assign as kpoints. The program then utes the simulation, stopping at

these breakpoints.

breaexec

Goto Starts the execution from any specified

in the flowsheet.

unit. You can select the unit by clicking the ihGoto cursorlg on the desired unit

Mes

engine is executing the simulation, in which case, the history will be updated

sages Displays the calculation history as it is being produced. This window can be displayed when the PRO/II calculation

as the calculation proceeds.

View Results Displays the detailed output results of

without executing it again by opening the appropriate .OUT file.

the highlighted unit operation or stream in the flowsheet of the previously run simulation. You can review the results of multiple units or streams, if desired. If the simulation has been run previously, you can view its results

Show Breakpoints

Shows wbreakpo

hich units are assigned as ints by displaying their icons in

a different color. Clicking the button a second time disables the breakpoint display.

Checking the Simulation Status Use Status to display the Flowsheet Status window. This window allows you view the global status messages for the current simulation. This button is highlighted as a selectable operation only if Check Data has been previously invoked either directly from the palette or indirectly from execution of the Run

to

operation. The following colors around the Status button indicate the Check Data results:

red border indicates that errors weA re found. A yellow border indicates that warnings were generated. A black border indicates that no errors were found when Check Data was last performed.


In all cases, the status can be viewed by selecting Status. To see the current global status messages for your simulation:

Choose Status from the Run palette. The Flowsheet Status window appears. The results appear in a scrollable window. Check Data

Figure 10-2: Flowsheet Status

If er

rors were detected, you must correct your simulation data.

lation.

Unders

s the simulation progresses, you will observe that the individual units will

Choose Close to exit the Flowsheet Status window. Correct your simulation errors.

f no errors were detected, run the simuI

tanding the Unit Color Coding Cues

Achange color. Refer to the following for the default color codes.


Unit Color Coding Color Significance

Yellow Unit operation at initial condition.

Red Unit operation has not been solved.

Green Unit operation in process of being

calculated.

Blue Unit operation has been solved.

Dark Blu s been calculated. This color is displayed only when you use the Run button, and a unit operation was previously calculated.

e Unit operation ha

Purple Breakpoint set directly before or after a unit operation

Using the No Colors Feature If you do not wish to see the unit icon colors update as the flowsheet solves, you can get a performance benefit by deselecting the View/Show Run Colors option on the menu bar. This option operates exactly like the Run button on the Run palette, but unit icon colors are updated only when the simulation finishes or stops at a breakpoint. Running the Simulation When you begin executing the simulation, the flowsheet convergence can be viewed in a Messages window by clicking Messages on the Run palette. You can close this window by clicking again on Messages or by double-clicking on the Message window’s control-menu box. Use Run to begin executing the simulation. The program starts from:

The unit at which the calculations were stopped; The unit you selected using the Goto option.

The first unit, if this is the first run;


The Run option automatically runs Check Data. To begin executing the simulation:

Choose Run from the Run palette. When stepping through or stopping simulation execution, you may choose to examine the status of the simulation.

Select Status from the Run palette. You may continue stepping through the simulation on a unit-by-unit basis

by selecting Step . Alternatively, you may choose to run the simulation without stepping by

selecting Run . If the run encounters problems, warnings will appear in the Flowsheet Status window. You have the option to close the window and correct the warnings or continue the run by clicking Run Simulation. Stepping Through Simulation Execution Use Step to execute the calculations for the current unit (stopping at the next unit in the calculation sequence). In this manner, you can step through the execution of the simulation by stopping at each unit operation in the calculation sequence. To step

through the execution of the simulation:

Choose Step from the floating Run palette. f the MessagesI window is open, you can observe that execution ceases after

completion of the current unit.

topping Simulation ExecutionS Use Stop to interrupt or stop the simulation while it is executing. The program completes its current calculation before stopping. To stop or interrupt simulation execution:

Choose Stop from the Run palette. The unit after the calculation stops becomes the current unit, as indicated by its color.


Using Goto Use Goto to start execution from a selected unit. This can be invoked at program

itiation or after execution pauses while stepping or stopping. in To start the execution from a specified unit:

Select a unit on the PFD. Choose Goto from the Run palette.

The selected unit becomes the current unit. When execution completes ounit, its Goto status is remove

n this d.

et breakpoints using a cursor:

sing Breakpoints U

You can set a breakpoint on any unit. Breakpoints can be before the unit operation, after it, or both. You can set breakpoints using the cursor or by utilizing the Breakpoints window. In addition, you can set breakpoints before and after a loop using the Breakpoints window.

o sT

Choose Set Breakpoints from the Run palette to turn on the Breakpoint mode. This automatically brings up the Breakpoints window.

Select the unit for which you want to set a breakpoint. Choose Close to exit the Breakpoints window.

RO/II updates the values in the Breakpoints window to show that there is no

and nits without a

reakpoint are considered “Off.” Breakpoints are for use during the current

PRO/II turns units selected as breakpoints purple and updates the values in the Breakpoints window. To delete a breakpoint in Breakpoint mode:

Select the unit. PRO/II will no longer show this unit as purple. Plonger a breakpoint attached to this unit. The Breakpoints window lists all unit operations in the calculation sequence identifies the breakpoint type for each unit: (before, after, both). Ubsession. PRO/II does not save breakpoint information.


To set breakpoints using the Breakpoints window:

Choose Set Breakpoints from the Run palette. The Breakpoints window

ote: Click Show Breakpoints to highlight those units or loops where

appears. Nbreakpoints have been previously set.

Figure 10-3: Breakpoints Window

Set the desired breakpoint type by clicking on the check boxes. You can

set before, after, or both. Select a unit from the list.

The breakpoint for the unit is set based on the breakpoint placement you select. To close the Breakpoints window:

Choose Close.

ow does not turn off Breakpoint mode.

To

Note: Closing the Breakpoints wind

turn off Breakpoint mode:

Choose Set Breakpoints on the Run palette a second time.


View

ing Calculation History

Use Messages to view the calculation history that has been produced so far. This lly ends, or

hen the simulation reaches a breakpoint.

o view the calculation history for the simulation thus far:

can be used while the simulation is executing, after the simulation finaw

T

Choose Messages from the Run palette. The Messages window appears. This is a multiline data window that is continuously updated. Viewing Results Use View Results to display results for the selected stream or unit in the default

Select the desired stream or unit.

text editor. To view results for a stream or unit:

Choose View Results from the Run palette, or

Click View Results on the toolbar. Alternatively, you can view process unit and stream results via the Unit List and

windows: Stream List (Go To)

Click unit or stream to open the Unit List or Stream List window

. Highlight the desired unit or stream.

Click View Results .

he PRO/II report generator creates a single ASCII file.

Theselected

T

default text editor will be used to display the standard PRO/II output for the stream or unit.


Viewing Results in Stream Property Tables

he stream property tables provide a convenient means to display selected results for a group of streams on the PFD. Four predefined report formats are supplied. These formats may be modified as desired and/or additional formats may be defined by the user. In addition to the stream properties selected for display, the titles and number of decimal places to display for each stream property may be chosen by the user. A quick check of the material balance for the problem may be accomplished by displaying the source and sink streams for the problem.

T


electing Streams for Property Tables

S

Stream property tables are set up from the PFD palette by adding a stream roperties icon to the PFD.

Double-click the stream properties icon on the PFD to display the Stream

d for available stream selection by selecting the appropriate radio button:

Include All Streams: This is the default. All the streams in the flowsheet are displayed in the Available Streams list box. Include Flowsheet Source/Sink Streams: Only those streams entering the flowsheet as feeds and leaving the flowsheet as products are displayed in the Available Streams list box, producing a material balance check for the flowsheet.

p

Property Table window. Choose the metho

The streams in the Displayed Streams list box may be sorted using the Up, Down, Top and Bottom buttons. Customizing the Stream Property Tables The appearance of a stream property table may be customized with options provided on the Stream Property Table window. The property list (format) to use for the display may be selected in the Property List to be Used list box. Note that

PRO/II, the user may also prepare fining Stream Property Lists below for

formation. Con component

roup for printout. For example, a C6 plus component group might be used to NC6 and heavier. Any number of component groups

in addition to the property lists supplied byspecial property lists for selection. See Dein

tiguous strings of components may be grouped into a single ggroup all components from may be set up. To specify a component group, click Define Component Groups…

dow.

ups.

on the Stream Property Table window to access the Group Components winThis window may be used to define and name component groups, as well as to edit existing component gro


The appearance of the steam property table itself may be altered by the user in

s)

am Property Lists from the enu bar. PRO/II provides four default lists that may be edited if desired:

Material Balance Lisased c

ole

lar flowrate, Vapor and rate, Vapor and liquid

ol r and liquid CP, Vapor nd rmal

tension.

the Stream Property Table window. Options include multiple rows per table, displaying the row grid lines, and setting the widths for the borders, lines, and property cell characters. Defining Stream Property Lists (Format Stream property lists are defined and edited via the Define Property List window. This window is accessed by choosing Options/Strem

hort Property List: Temperature, Pressure, Molar flowrate, Phase. S

t: Temperature, Pressure, Molar flowrate, Phase, Molar- omposition. b

tream Summary: Phase, Molar flowrate, Standard liquid flowrate, S

Temperature, Pressure, Molecular weight, Enthalpy, Specific enthalpy, Maction liquid, Reduced temperature, Reduced pressure, Acentric factor, UOP fr

K-value, Standard liquid density, Vapor and liquid moiquid mass flowrate, Vapor and liquid volumetric flowlm ecular weight, Vapor and liquid specific enthalpy, Vapo

liquid density, Vapor and liquid viscosity, Vapor and liquid theaconductivity, Liquid surface Comp. Molar Rates: Molar component and total flowrates, Temperature, Pressure, Enthalpy, Molecular weight, Mole fraction vapor and liquid. To edit an existing property list:

Use the drop-down list box to select the property list name. To create a new property list:

Click New to access the New List window and enter a name for the new list in this window. This window also allows you to select an existing lfrom a drop-down list box to be copied to create the new list.

ist

drop-down list box on the Define Property List window and click the button to transfer the property to the Property Description Format list box.

The property that was selected is expanded in this window, with the addition of a description and a format which may be edited in the data entry fields provided.

To add a property to a property list:

Select the property in the Select Properties


The description for the property may be changed from the default value and the ntout may also be changed if desired.

selected in the Property d as desired.

nthalpy, etc., property

n a

main data entry window by selecting

number of decimal places for pri When editing an existing property list, properties may be Description Format list box and edited, deleted, or rearrange

addition to such properties as temperature, pressure, eInitems such as “double line,” “line,” and “text” may be incorporated in a propertylist to add blank lines and special headings. Running a Case Study Case Study is an executive level feature that allows you to perform studies obase case solution by altering parameters selectively and rerunning the simulation.

Access the Case StudyInput/Casestudy Data… from the menu bar.

Figure 10-4: Case Study Main Data Entry Window

Enable the window by checking the Define Case Study box.


In this window, you can specify the changes you want to make to your input Parameters and to define the Results you want to examine. You may define as many parameters and results as you want. Parameters: The table of parameters initially has one row. You may insert or remove as many rows as you wish. Parameter Identifier: The parameter identifier defines the way you want the output data to be presented after the Case Study has been executed. A default identifier (here “PARAM1”) is supplied. To change the parameter identifier, click on the data field and enter a new name. Parameter: You must identify a parameter to change. Click Parameter to open the Parameter window. Select the parameter that you want to change. When you close this window, the parameter you have specified appears in place of the original text. Start Value: Click Base Case Value to open the Parameter Start Value window where you define the starting value for the parameter. The starting value defaults to the value of the parameter in the base case. When you close this window, the starting value will be displayed. Start Cycle: The start cycle is the cycle after which the incremental changes are implemented. Cycles before the start cycle use the value in the base case. If necessary, enter a new start cycle number. By default, the starting cycle is one (1). End Cycle: Cycles after the end cycle use the value in the end cycle. If necessary, enter a new end cycle number. The end cycle defaults to the value of the start cycle. Step Value: Next, define the value of the incremental step change per cycle. The new step value will be displayed. Results: The table of results initially has one row. You may insert or remove as many rows as you wish. You may define a Result as one flowsheet parameter or as a function of two flowsheet parameters or as a function of one flowsheet parameter and a constant. See SPEC/ VARY/DEFINE in Chapter 9 for details on

s and composing specifications.

esult Identifier: The result identifier will be used when you define how you d after the Case Study has been executed. A

efault identifier is supplied. To change the result identifier, click on it and enter a new identifier.

using and changing mathematical operator Rwant the output data to be presented


Firswindow element of the function you are defining. SecParame you select the parameter (or constant) that you want s the second element of the function you are defining.

Execute: list to execute the base case only

. If you do not want to execute all the cycles f the case study, select Base Case and Specified Cycles and specify a

beg

wing Case Study Results

t Parameter: Click on the first (or only) parameter to open the Parameter where you select the parameter that you want as a Result or as the first

ond (Reference) Parameter: Click on second parameter to open the ter window where

a

Execution Options: Select from the or the base case and the case studyo

inning and ending cycle. Vie

Select Output/Case Study/Plots… or Output/Case Study/Table… from the menu bar to specify the format of your Case Study results. After entering a required name and optional title for the plot or table, click Data… to open a window where you may specify the parameters and results you wish to have plotted or tabulated, enter labels for the axes of the plot or rows and columns of the table, etc. Running Files in Batch Mode You can execute one or more PRO/II ASCII keyword input files or flowsheet simulation files in Batch Mode from within PRO/II. The keyword input file may be one that was created using a text editor or word processor, or one that was previously created using the Keyword File Export capability. You can also execute flowsheet simulations that were created using PRO/II from the GUI, or were created by importing a PRO/II keyword input file. The batch execution of keyword input files or simulation files generates the standard PRO/II ASCII output file for each of the selected files. While executing simulation problems in batch mode, you can continue to work with other Windows applications. You can terminate the currently executing problem or the batch execution mode completely by pushing the Terminate Current Problem or Terminate Batch Run buttons, respectively. To select a PRO/II keyword input file, simulation file (or group of files), or a previously stored execution list file:

Close the currently open simulation. Choose File/Run Batch from the menu bar. PRO/II displays the Run

Batch - Input and/or Simulation Files Selection window.


Figure 10-5: Run Batch - Input and/or Simulation Files Selection

Initially, there are no keyword input (*.INP) or simulation files (*.PR1) disp yed in

thods of adding keyword input or imulation files to the file sequence list:

lathe File Sequence window. There are two mes

Select the files explicitly using the Add Files… button, or Load a previously saved list of files using the Load List… button.

To select the desired keyword input or simulation files:

Click Add Files…. PRO/II displays a list of available existing keyword input files. The default file

pe is keyword files (*.INP). You can change the file type to simulation files (*.P

tyR1, *.PRZ) using the Files of type drop-down list-box.


Figure 10-6: Run Batch - File Select

Type or select the name of the file that you want to execute. You can

select multiple files within a given directory. Only the keyword inptory will be added to the list of .

ut files highlighted in the currently selected direcfiles to execute when you exit this window

Click OK to validate your selection and return to the Run Batch - Input

o load an existing list of keyword input and/or simulation files:

and/or Simulation Files Selection window.

T

Click Load List….

RO/II displays a list of available existing execution list files. The default file type the complete path and name of

rder previously specified by he below:

C:\SIMSCI\PROII_W\USER\CASE1.INP C:\SIMSCI\PROII_W\USER\CASE2.INP

xe es (beginning with a semicolon ;), and

n e

Pis Run Batch List (*.LST). These files contain eyword input and simulation files in the execution ok

t user. An example of the typical contents of an execution list file is given

C:\SIMSCI\PROII_W\USER\CASE3.INP E cution list files may include comment lin

include list file directives given by #include followed by the .LST file name. xample is given below: A


;This is a comment C:\SIMSCI\PROII_W\USER\CASE1.INP C:\SIMSCI\PROII_W\USER\CASE2.INP ; The following list file to be loaded ; contains flash problems #include flash.LST Note: The #include directives may be nested, e.g., in the example above, flash.LST itself could contain the directives #include dewpt.LST and #include bubpt.LST.

Figure 10-7: Run Batch - Load File List

Type or select the name of the execution list file that you want to load.

a given directory. Only the list files ed directory will be used to create the

list of keyword input and simulation files to be executed.

You can select multiple list files withinhighlighted in the currently select

Click OK to validate the selection and exit. When you return to the Run Batch - Input and/or Simulation Files Selection

indow, the contents of the previously selected execution list file(s) will have anded and are now displayed in the File Sequence list box. Selected

files will be added to the bottom of the list of previously selected files displayed in

wbeen exp

the File Sequence list box.


Revising the File Execution Sequence Order

er in which the selected files are to be executed using the

ou can revise the ordYRemove , Move Up , Move Down , Move Top and Move Bottom buttons. Creating an Execution File List

You can n Execution File List that can be retrieved and executed at a later date.

store a list of keyword input or simulation files as a

Click Select from Lists….

PRO/II displays the Run Batch - Save File List As window containing the execution file list options.

Figure 10-8: Run Batch - Save File List As

Enter a name for the Execution List File. Click OK to store the list as a *.LST file in ASCII format.

xecuti

return to the Run Batch - Input and/or Simulation Files Selection

E ng the Batch List

hen youWwindow, you can begin the execution of the specified file list. To start the batch mode execution of the list:

Click OK.


The specified list will be executed in the order shown in the File Sequence box. Wh t the batc een completed. Ter tch List

e execution of the selected keyword files:

en the execution is complete, a message will be displayed to notify you thah mode execution has b

minating Execution of a Ba

You have the choice of terminating the currently executing simulation problem, or terminating the batch mode execution completely.

o terminate batch modT

Click Terminate Current Problem to terminate the currently executing problem.

The problem execution will stop after the current unit calculations are complete. Note: You can terminate an executing problem only during calculation. To terminate batch mode execution completely:

Click Terminate Batch Run to end the execution. Viewing Output Results Results of Batch Execution of Keyword Input (*.INP) Files: By default, the program deletes the simulation files that remain after batch mode execution of specified keyword input files (*.INP). The standard PRO/II ASCII output report will be located in the corresponding .OUT file(s). Results of Batch Execution of Simulation (*.PR1, *.PRZ) Files: By default, the program will not delete the simulation files that remain after the batch mode execution of specified simulation files (*.PR1, *.PRZ), or the ASCII format standard output report located in the corresponding .OUT file. You can open the resulting simulation file(s) with the File/Open command, and then proceed to generate reports or modify the simulation flowsheet as desired in PRO/II. Whatever type of file (keyword input or simulation) was executed in batch mode, you can always view and edit the corresponding standard ASCII output files with any ASCII-capable text editor or word processor.


Chapter 11 Printing and Plotting

his iew and print reports, and generate

ef

RO/II pdimensional units. You can change the output format of a report for any solved simulation without re-executing the simulation.

o define the output format:

Choose Output/Report Format from the menu bar. The Report Format menu appears with options for Units of Measure, Miscellaneous Data, Stream Properties, and Unit Operations.

Ta

chapter describes how to generate, vnd print plots. Printer setup is also described.

D ining Output Format

rovides a variety of report options for streams, unit operations and P

T

Figure 11-1: Report Format Menu

Setting Miscellaneous Data Report Options You can set the report dimensions, identify the data you want to include and set the product stream scaling using the Miscellaneous Data option.

Chapter 11 PRINTING AND PLOTTING 361

To set miscellaneous data options:

Choose the Option/Report Format/Miscellaneous Data from the menu bar. The Miscellaneous Report Options window appears.

Figure 11-2: Miscellaneous Report Options


Setting Product Stream Scaling To change the scale stream flowrate:

Choose Product Stream Scaling… from the Miscellaneous Report Options window. The Report Options - Product Stream Scaling window appears.

Select the Scale Stream Flowrate checkbox. Specify the stream to be scaled, the components to be scaled, and the

scaled flowrate.

Figure 11-3: Scale Stream Flowrate

Click OK twice to commit the changes and return to the PFD.


Setting Stream Properties Report Options To set the stream properties report options:

Choose the Output/Report Format/Stream Properties menu item. The roperty Report Options window appears (Figure 11-4).

Select the desired flowrate, fractions, or percent values for the Standard

PFD.

Stream P

Component Flowrate/Composition Report. Click OK to commit the entries and return to the

Figure 11-4: Stream Property Report Options

Setting Units of Measure Report Options In addition to the global, problem and unit level default units of measure you set for input data, you can also set Problem Units of Measure for output reports. You can change the output values for all the fields by applying a different units of measure set or you can make individual value adjustments. To set units of measure for output reports:

Choose the Units of Measure menu item from the Report Format menu. The Default Units of Measure for Problem Output Report window appears.


Figure 11-5: Default Units of Measure for Problem Output Report

Click Initialize from UOM Library… to extract default values from another

set or replace the default values as necessary. Optionally, click Standard Vapor Conditions… to change the vapor

condition settings for this problem. The Problem Standard Vapor Condition window appears.

Figure 11-6: Problem Standard Vapor Conditions

Specify the desired standard vapor conditions.


Click OK in the child win Setting Unit Operations Report Options You can set specific print options for each type of unit opera To set the unit operations rep

dows to return to the PFD.

tion.

ort options:

Choose the Output/Report Format/Unit Operations menu item. The Unit Operation Output Report Options window appears.

Figure 11-7: Unit Operations Output Report Options

Select the desired unit operation.

Choose Print Options… . The Column Print Options window appears.


Figure 11-8: Column Print Options

Select the items you want to include in a Column Report.

Optionally, click Plot Colu sults… to set options for a plot. The Column Plot Options window appears

mn Re.


Figure 11-9: Column Plot Options

Close to commit the entries and

Generating a Report You rmat option to define the form

o gen simulation:

Click OK in the child windows, then

return to the PFD.

can generate a report to a file. Use the Define Foat of the report.

T

erate a report from an executed

Click Generate Reports on the toolbar, or choose Output/Generate

As PRO/II generates the report, a window appears, displaying the status of the report as it runs. Once the report has been generated, the default editor window appears displaying the contents of the report. PRO/II appends an .OUT extension to the current simulation name and saves the file in the USER directory.

Reports from the menu bar.


Viewing a Report To view a previously generated report of the current simulation:

Choose Output/View Report from the menu bar. To view a previously generated report for any simulation:

Choose File/Open from the menu bar. Select Report Files in the List Files of Type list box and choose the

desired file. Printing a Report To print the report:

Print from your text editor while viewing the report, or Choose File/Print from the menu bar.

-down list box in the Print window.

Assay stream analysis Output Results

(temperature, flowrates, composition, and

Zones analysis for simple and rigorous heat exchangers Phase envelopes Heating/Cooling curves

Plots can be displayed using PRO/II’s Plot Viewer or Microsoft Excel. The section Setting Up the Plot Driver later in this chapter describes how to select and configure the plot driver.

Select Report in the Print drop Click OK .

Plotting PRO/II generates and displays a variety of plots for input data and tabulated results. The following plots can be generated:

Input Data

Distillation column profilesseparation factor)


Generating a Plot To generate an assay stream analysis plot, select View Curve... on the Stream Assay Definition window. Three curves will be generated:

The actual user input distillation data The regressed TBP curve The component cuts generated.

To generate one of the output results that PRO/II supports:

Choose Output/Generate Plot from the menu bar. PRO/II displays the Generate Plot window as shown in Figure 11-10.

Figure 11-10: Generate Plot Window

By default, the Units for Selecflowsheet for which plots are

tion list box displays all the unit Operations in your available. If you check the Selected Units option,

nly available will

hen you select a unit operation in the Units for Selection list box, the Available Plots list box displays all plots available for that unit. You may select a plot then

o those units you previously selected on the PFD for which plots arebe shown.

W

click Plot… to display the plot. If the plot requires additional options to be chosen, the Plot… button will change to an Options… button. Currently, additional data is

red only for Distillation Column Plots. requi


Plot To

ting a Column

obtain a plot of vapor and liquid compositions:

Choose Vapor and Liquid Compositions, then choose Options… to open the Column Vapor and Liquid Composition Plot window.

Figure 11-11: Column Vapor and Liquid Composition Plot

Enter the additional data required. Click Plot….

Up the Plot Driver Setting

internal Plot Viewer or Microsoft Excel (through ers

The PRO/II Plot Viewer i nts plots.

s a complete set of formatting features. With Excel, you can change plot colors, axis titles, and other attributes to create a presentation-quality graph. To select and configure the plot driver:

Choose Options/Plot Setup on the menu bar to open the Plot Setup window.

RO/II can display plots using itsP

v ion 7).

s a built-in utility that also pri Microsoft Excel provide


Figure 11-12: Plot Setup Window

RO/II’s installation procedure will set up the options in this window. Select the desired plot driver using the list box. If you need to configure the currently selected plot driver, press Setup to display the Setup Plot Driver window. You cannot configure the PRO/II Plot Viewer (option “SIMSCI”).

P

Figure 11-13: Setup Plot Driver Window


The Driver File: The complete path and filename of the dynamic link library (DLL) for

e plot driver.

river.

Comma cation. Options: Additional driver-specific options.

he Plot Viewer

PRO/II’s Plot Viewer utility land ttributes are not supported. If ouhoose the Excel plot driver.

o save a plot:

ou can send a plot from the Plot window to your plotter.

o s

Plot window menu.

o export a plot to an ASCII file:

ow menu. limited) and click OK .

o copy the plot image to the clipboard:

Plot window menu.

configuration options are:

th

river Function: The function name to invoke the dD

nd Line: The full command line to invoke the plotting appli

T

ets you view a plot, print it, copy it to the clipboard, export its data to a file. Modifications of plot a

yc

want access to comprehensive editing and formatting features for your plot,

T

Choose File/Save As from the Plot window menu. Enter the desired plot file name and click OK .

Y T end a plot to the plotter:

Choose File/Print from the T

Choose File/Export from the Plot wind Select the file type (tab- or comma-de

T

Choose Edit/Copy from the


Setting Up the Printer To

se File/Print Setup from the menu bar.

Select paper orientation and size and click OK .

g a Flowsheet Layout

To print a flowsheet diagram:

the menu bar. es and click OK .

set up the printer:

Choo Select a printer.

rintinP

Choose File/Print from Select the range of pag


Chapter 12

zation of PFD appearance. You can control unit and stream appearance, modify the stream property tables, and set the font style used on your PFD. Changing Unit Style

n, name, or label starting number for any unit peration. These changes affect all unit operations that you subsequently place

on t Cha

o change the style of a unit globally:

Customizing the PFD Workplace

his chapter surveys the customiT

You can specify a different icoo

he PFD.

nging the Unit Icon Globally T

Choose Options/Drawing Defaults/Unit Display… from the menu bar. The Unit Style window appears.

Chapter 12 CUSTOMIZING THE PFD WORKPLACE 375

Figure 12-1: Unit Style Window for Classes of Units

Select the type of unit operation you want to change. Enter your changes for the label format and starting number.

The text portion to the left of the “%” sign is the label displayed with the unit number. The label may not contain spaces or underscores. The integers following “d” are appended to the automatically applied sequential unit numbers. You may also choose the starting number for the particular unit. For example, if the Auto Label Format for the Flash unit operation were “FLASHUNIT%d05,” subsequent Flashes placed on the PFD would be labeled “FLASHUNIT105,” “FLASHUNIT205,” “FLASHUNIT305,” and so forth. You can also modify the type face and type size used in the stream label as discussed below under the topic Changing the Default Font.


Icon for a Single Unit

ifferent display icon for any unit opns can be re ferent

icons. This choice is particularly useful when di of the same unit eled.

No n available can be assigned to a routine.

tyle of a single unit:

the icon of the unit you w nit menu ars.

Changing the Unit You can specify a d eration currently shown in

presented by several difyour flowsheet. Some unit operatiofferent variants

operation are being mod

te: Any ico User-Added Sub To

change the s

Right-click on ish to modify. The uappe

Figure 12-2: Unit Menu

Select Display... from this menu (or sel isplay Style… from the

menu bar) to open the Unit Style windo ected unit type as own in Figure 12-3.

ect Edit/Dw for the sel

sh


Figure 12-3: Display Style Window

Select an alternative icon from the palette at the top of the window. Choose OK to confirm the change.

ou can also change the type face, type size and color of the unit label by Y

choosing Select… to access a standard font editing window. Changing the Label for a Particular Unit PRO/II automatically labels each unit you place it on the PFD. You can change the label for each unit without altering the numbering sequence. To change a unit label:

Double-click on the unit on the PFD. Type over the existing “Unit” label in the data entry window. Commit the change by pressing OK.

Changing Stream Style You can modify stream appearance by changing:

The height and width of the arrows



The fill of the arrows The segments on which the arrows appear The label format The starting number The stream label location The stream label border The label type (name or list of properties) The contents of the property list (material balance, gas report,

comparative molars rates, etc.). To change the style of a stream:

Choose Options/Drawing Defaults/Stream Display… from the menu bar to open the Stream Style window.

Figure 12-4: Stream Style Window

By default, stream labels have rectangular borders and appear on the stream line. (Optionally, you may select (1) diamond-shaped or circular label borders, or, alternatively, no label border at all, and (2) the position of the label relative to the stream.) Process stream arrows are not filled and appear only on the horizontal segments of an orthogonal process stream. You can change the appearance of the arrows and where the arrows appear on the process stream.


Figure 12-5: Default Stream Style

Figure 12-6: Modified Stream Style


Changing the Label for a Particular Stream PRO/II automatically labels each stream as it is placed on the PFD. You can change the number or label for just one stream without altering the ongoing numbering sequence. To change a stream label:

Double-click on the stream to open the Stream Data window. Alternatively, right-click on the stream and choose Data Entry….

Figure 12-7: Stream Data Entry Window

Enter the new stream name in the Stream entry field.

Displaying Stream Properties on Stream Labels PRO/II allows you to display various stream properties on labels attached to the streams on the PFD. Display options include:


Selecting a global default property list for all stream labels in the flowsheet

Choosing from a group of predefined property lists Creating a custom stream label property list Positioning stream property labels anywhere on or beside the streams on

the PFD Choosing the type of border for any label Choosing a different font for any label

To Select a Global Default Steam Property:

Choose Options/Drawing Defaults/Stream Display… from the menu bar to open the Stream Style window.

From the Stream Label Type drop-down list, choose the Properties option.

Choose one of the predefined property lists and click OK to commit your choice.

The property list that you have selected will appear on all streams subsequently drawn on the PFD. Creating a Customized Stream Property List PRO/II allows you to create customized property lists for use in Stream Property Tables. You can use the same property list in more than one simulation. The default Stream Property Table is outlined by a single-lined rectangular box. You may arrange the properties in any desired order, and you may separate entries by single or double horizontal lines to improve the legibility of the list. To select a property list:

Choose Options/Stream Property Lists from the menu bar to display the Define Property List window (Figure 12-8).


Figure 12-8: Define Property List Window

Select a list from the Property List box (Figure 12-9).

Figure 12-9: A Typical Property List

You can add or delete properties, modify the property description and

change the numerical format. To create a property list:

Choose New… from the Define Property List window. The New List window appears.


Figure 12-10: New List Window

Enter a name for the new list, or Select the list from which you want to copy an existing property list. Choose OK to commit the entries.

To add one or more properties to a list:

Select the desired properties. (The usual Windows click, shift-click and control-click selection options are supported.)

Choose Add-> . The selected properties will be added to the bottom of the property list. To change the order of the properties in a list:

Select the properties you want to move. Use the Up, Down, Top, Bottom buttons to move the selected properties.

To change the description or the format of a property:

Select the property you want to change. Enter the new description and format in the entry fields under the

property list. Commit the changes using the Replace button.

To delete a property from a list:

Select the properties you want to delete. Choose Remove.


To clear (delete) all properties from a list:

Choose Clear. To demarcate sections of a list:

Insert single or double horizontal lines where desired. Positioning Stream Property Labels on the PFD You may place stream labels on, above, below or beside the streams on the PFD. The labels may appear with or without stems connecting them to the streams. To position stream labels:

Choose Options/Drawing Defaults/Stream Display… from the menu bar. Select the desired position from the Stream Label Location drop-down

list. Click OK to commit your selection.

Alternatively, you may drag a stream label to any of these positions from the PFD itself. While in the Stream Styles window, you may also choose a text font and a border style for the labels from the corresponding drop-down lists. Toggle stream property list: Select the table of properties to be included during the toggle action. User can select a particular stream property table as the toggle stream property list. When the user clicks the toggle button on the toolbar the stream label toggles between the stream label type and the toggle stream label list. The default option for the toggle stream list is "Property Label List"


Figure 12-11: Toggle Stream Property List

User configured property lists will also be included in the drop-down list of toggle stream property list and the same can be used to toggle between the existing stream label and the toggle list. Tooltip property list: User can configure the tooltip feature using this list box. By default the “Property Label List” acts as the tooltip option. This list box will help the user to configure the property lists so that they can be used as tooltip displays. User should select a particular property list from the tooltip property list box The selected property list will be displayed as tooltip display, when the user hovers the mouse pointer on the stream. User can also set this option to OFF so that stream name will appear as tooltip display. Modifying Drawing Preferences Drawing preferences include settings for snap and move tolerances, zoom and pan increments, the PFD palette icon, icon fill, unit snapping, and delete confirmation. To modify drawing preferences:


Choose Options/Drawing Defaults/General… from the menu bar.

The General Drawing Defaults window appears with current settings. The settings can be changed as desired. Specifying a Default Editor You can specify a default editor (such as Brief, Edit or Notepad) for use with PRO/II to display output reports and keyword input files. Using the editor, you can save any displayed text to a file or printer. The default editor is the Programmer’s File Editor (pfe.exe). To specify a default editor:

Choose Options/Editor from the menu bar to open the Set Text Editor window.

Enter the full path name to the editor executable program file.

Figure 12-12: Set Text Editor

Changing the Default Font The Default Font option enables you to set the default font, font style and size used in PRO/II’s main and data entry windows. This option is useful if the default font size for your system is too large for PRO/II’s data entry windows. Note that you cannot change the fonts for the title, menu, and status bar text. Also, changing the font size will not change the size of PRO/II’s windows. To specify the default font:


Choose Options/Font from the menu bar to display the Font specification window.

Choose the desired font, font style, and size.

Figure 12-13: Font Window

INDEX 389

Index Aligning Text, 77 Boiling Pot Reactor, 299 Border Handles, 13 Bounding Box

Changing the size, 83 Moving, 83

Calculator calculator, 150

cancel Unit placement, 59

Cancel Delete, 59

Changing Window Size, 13 Column, Side, 197 Components, 26 Continuous Stirred Tank Reactor, 295 Control Menu, 13 Conversion and Equilibrium Reactors,

294 Data Entry Window Buttons, 19 Depressuring Unit, 219 Dissolver, 224 edit text, 77 Entering Text, 66 Excel Unit, 225 Expander, 231 Fill from Structures, 88 Fixed Properties, 105 Flash, 233 Flash With Solids, 237 Floating Palettes. See Flowsheet Optimizer, 238 Gibbs Reactor, 300 Go To Buttons, 20 Heat Exchanger, Lng, 244 Heat Exchanger, Rigorous, 246 Heat Exchanger, Simple, 256 Heating/Cooling Curves, 260 Help Button, 22 Henry’s Law, 116 Importing a PRO/II keyword input file, 37 Linked text, 97 Menus, 14 Minimize/Maximize Buttons, 13 Mixer, 264 Multiple View and PFD Palette Buttons,

18

Multivariable Controller, 265 Objects

Deselecting, 74 Flipping, 76 Moving, 76 Rearranging, 75 Resizing, 74 Rotating, 76 Selecting all, 73 Selecting group, 73

Pan Left, Right, Up or Down, 83

Panning, 81 Phase Envelope, 268 Pipe, 273 Pump, 288 Reactor

Polymer Reactor, 278 Reactor, Batch, 307 Report options, 361 Run/Results Buttons, 20 Save

Current Simulation, 32 Save as dialog box, 33 Simulation to another name, 32

Screen Color Coding, 14 Scroll Bar

Horizontal, 12 Vertical, 12

Scrolling increments, 79 PFD, 79

Select all objects, 73 Group of objects, 73 Multiple objects, 71

Set Breakpoints, 347

Setting Up the Printer, 374 Simsci Add-On Modules, 335 Simulation

Closing, 34 Copy, 35 Deleting, 34 Opening, 31 Opening a existing simulation, 32 Save current simulation, 33


Savings tp another file name, 33 Simulation defaults

Problem Description, 48 Units of measure, 48

Simulation Defaults, 47 Snapping, 58 Solid Separator, 308 Splitter, 309 Starting PRO/II, 9 Stream Calculator, 311 Stream Information, 27 Stream Property, 44 Temperature-Dependent Properties,

106 Thermodynamic Methods, 26 Toolbar, 18 Transport Properties, 120 turn off, 348 Unit data entry window, 27 unit icon, 58 unit label, 378 unit opeartion

Cyclone, 212 unit operation, 148

Column, Batch, 171 compressor, 200 Controller, 205 Crystallizer, 208 Distillation, 172

Unit Operations, 27 Units of Measure Library, 51 User defined special properties

Thermodynamic Data, 142 User-Added Unit Operations, 167, 327 User-defined Special Properties,

139, 140 Valve, 339 Vertical Scroll Bar, 12 View Buttons, 21 Viewing Results, 349 VLE Tools Buttons, 20 Water Decant Options, 121 Window Position, 13 Wiped Film Evaporator, 340 Zoom Area, 21 Zoom Increment, 80 Zooming, 79

Guia de Usuario de Proii

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