Aspen Plus Exercises
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Transcript of Aspen Plus Exercises
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I t d ti t A PlIntroduction to Aspen PlusShort Courses on Computer Applications for ChE Students
Speaker: JianKai Cheng (程建凱)p g (程建凱)[email protected]
PSE LaboratoryDepartment of Chemical EngineeringDepartment of Chemical Engineering
Nation Taiwan University
What is Aspen PlusWhat is Aspen PlusWhat is Aspen PlusWhat is Aspen Plus
• Aspen Plus is a market‐leading process modeling tool for conceptual design, optimization, and performance monitoring for the chemical, polymer, specialty chemical, metals and minerals, and coal power industries.
2Ref: http://www.aspentech.com/products/aspen-plus.cfm
What Aspen Plus providesWhat Aspen Plus providesWhat Aspen Plus providesWhat Aspen Plus provides
• Physical Property Models– World’s largest database of pure component and phase equilibrium
data for conventional chemicals electrolytes solids and polymersdata for conventional chemicals, electrolytes, solids, and polymers– Regularly updated with data from U. S. National Institute of Standards
and Technology (NIST)
• Comprehensive Library of Unit Operation Models– Addresses a wide range of solid, liquid, and gas processing equipment
d d l d l f f d– Extends steady‐state simulation to dynamic simulation for safety and controllability studies, sizing relief valves, and optimizing transition, startup, and shutdown policies
– Enables you build your own libraries using Aspen Custom Modeler or programming languages (User‐defined models)
Ref: Aspen Plus® Product Brochure3
More DetailedMore DetailedMore DetailedMore Detailed
• Properties analysis– Properties of pure component and mixtures (Enthalpy, density, viscosity, heat capacity,…etc)
– Phase equilibrium (VLE, VLLE, azeotrope calculation…etc)– Parameters estimation for properties models (UNIFAC method for binary parameters, Joback method for boiling points etc)points…etc)
– Data regression from experimental deta
P i l ti• Process simulation– pump, compressor, valve, tank, heat exchanger, CSTR, PFR, di till ti l t ti l b b filtdistillation column, extraction column, absorber, filter, crystallizer…etc 4
What course Aspen Plus What course Aspen Plus can be employed forcan be employed for
• MASS AND ENERGY BALANCES• PHYSICAL CHEMISTRY• CHEMICAL ENGINEERING THERMODYNAMICS • CHEMICAL REACTION ENGINEERING• CHEMICAL REACTION ENGINEERING• UNIT OPERATIONS• PROCESS DESIGN• PROCESS CONTROL
5
Lesson ObjectivesLesson ObjectivesLesson ObjectivesLesson Objectives
• Familiar with the interface of Aspen Plus• Learn how to use properties analysis• Learn how to setup a basic process simulation
6
Problem Formulation 1: Calculation Problem Formulation 1: Calculation the mixing properties of two stream the mixing properties of two stream
1 2 3 4Mole Flow kmol/hr
WATER 10 0 ? ?BUOH 0 9 ? ?BUAC 0 6 ? ?
Total Flow kmol/hr 10 15 ? ?C 0 80 ? ?
Mass Balance
E B lTemperature C 50 80 ? ?Pressure bar 1 1 1 10
Enthalpy kcal/mol ? ? ? ?E t l/ l K ? ? ? ?
Energy BalanceEnthalpyEntropy…
Entropy cal/mol-K ? ? ? ?Density kmol/cum ? ? ? ?
7
Problem Formulation 2: Problem Formulation 2: Flash SeparationFlash Separation
120T
115
T-x T-y
Saturated Feed
T=105 CP=1atm
105
110
T (o C
)
P=1atmF=100 kmol/hrzwater=0.5 0.0 0.2 0.4 0.6 0.8 1.0
100
105
waterzHAc=0.5
What are flowrates and compositions of the two outlets?
xWater and yWater
What are flowrates and compositions of the two outlets?
Problem Formulation 3: Dehydration of Problem Formulation 3: Dehydration of Acetic Acid by Distillation Column Acetic Acid by Distillation Column
(Optional)(Optional)
1 0
( p )( p )
0.8
1.0
Reflux
0.4
0.6
y Wat
er
ratio ?
0 0
0.2Duty ?
0.0 0.2 0.4 0.6 0.8 1.00.0
xWater
OutlineOutlineOutlineOutline
• Startup in Aspen Plus (Basic Input) (45 min)– User Interface– Basic Input: Setup, Components, Properties.
• Properties Analysis (1 hour)– Pure Component– Mixtures (phase equilibrium)
• Running Simulation (1 hour)– Blocks (Unit Operations)– Streams (flow streams)– Results
10
Introduction to Aspen Plus – Part 1Startup in Aspen Plus
11
Start with Aspen PlusStart with Aspen PlusStart with Aspen PlusStart with Aspen Plus
A Pl U I t fAspen Plus User Interface
12
Aspen Plus StartupAspen Plus StartupAspen Plus StartupAspen Plus Startup
13
Interface of Aspen PlusInterface of Aspen PlusInterface of Aspen PlusInterface of Aspen Plus
Process Flowsheet WindowsProcess Flowsheet Windows
Model Library (View| Model Library )Model Library (View| Model Library )y ( | y )
Stream
y ( | y )
Status message14
More InformationMore InformationMore InformationMore Information
Help for Commands for Controlling Simulations 15
Data BrowserData BrowserData BrowserData Browser
• The Data Browser is a sheet and form viewer with a hierarchical tree view of the available simulation input, results, and objects that have been defined
16
Status IndicatorsStatus IndicatorsStatus IndicatorsStatus Indicators
17
Basic InputBasic InputBasic InputBasic Input
• The minimum required inputs to run a simulation are:– Setup– Components Property Analysis
– Properties– Streams
Process Simulation– Blocks
Process Simulation
18
SetupSetup –– SpecificationSpecificationSetup Setup –– SpecificationSpecificationRun TypeRun Type
Input mode
19
SetupSetup –– Run TypeRun TypeSetup Setup –– Run TypeRun TypeRun Type Description Use to
A t d l d t A l d t h d t t tAssay Data Analysis A standalone assay data analysis/pseudocomponents generation run
Analyze assay data when you do not want to perform a flowsheet simulation in the same run.
D t R iA standalone data regression run. Can contain
t t t ti ti d t l i
Fit physical property model parameters required by Aspen Plus to measured pure component, VLE LLE d th i t d t A PlData Regression property constant estimation and property analysis
calculations.VLE, LLE and other mixture data. Aspen Plus cannot perform data regression in a Flowsheet run. Prepare a property package for use with Aspen C M d l i h hi d i l
Properties Plus A Properties Plus setup runCustom Modeler, with third party commercial engineering programs, or with your company's in house programs. You must be licensed to use Properties Plus.P f l i b i bl
Property AnalysisA standalone property analysis run. Can contain property constant estimation and assay data analysis calculations.
Perform property analysis by generating tables of physical property values when you do not want to perform a flowsheet simulation in the same runE i h d
Property Estimation A standalone property constant estimation runEstimate property parameters when you do not want to perform a flowsheet simulation in the same run.
A Flowsheet run (including sensitivity studies and
Flowsheet
( g yoptimization). also include the following calculations: Property estimation, Assay data analysis and Property analysis
Perform process simulations
20
ComponentsComponents –– SpecificationSpecificationComponents Components –– SpecificationSpecification
I t tInput componentswith Component name or Formula
21
Input componentsInput componentsInput componentsInput components
Remark: If available, are
22
SpecificationSpecificationSpecificationSpecification
To do this Click this buttonFind components in the databanks FindDefine a custom component that is not in a databank
User Defined
Generate electrolyte components and reactions from components you entered
Elec Wizard
Reorder the components you have specified
Reorder
Review databank data for components you have specified (Retrieved physical property parameters from databanks )
Review
property parameters from databanks.)
23
Find ComponentsFind ComponentsFind ComponentsFind Components
Click “Find”
24
Find Components (cont’d)Find Components (cont’d)Find Components (cont d)Find Components (cont d)Input Component name or Formula or CAS numberp p
25
NIST ChemistryNIST Chemistry WebBookWebBookNIST Chemistry NIST Chemistry WebBookWebBook
26
PropertiesPropertiesPropertiesProperties
Process type(narrow the number ofProcess type(narrow the number ofmethods available)
Base method: IDEAL NRTL UNIQAC UNIFACBase method: IDEAL, NRTL, UNIQAC, UNIFAC…
27
Property Method SelectionProperty Method Selection –– AssistantAssistantProperty Method Selection Property Method Selection –– AssistantAssistant
Interactive help in choosing a property method
28
Assistant WizardAssistant WizardAssistant WizardAssistant Wizard
Specify Component typeChemical Systems
Is the system at high pressure?(NO)
Two liquid phases
29
30Reference: http://www.et.byu.edu/groups/uolab/files/aspentech/
Thermodynamic ModelThermodynamic Model –– NRTLNRTLThermodynamic Model Thermodynamic Model –– NRTLNRTL
Vapor EOS
NRTL Liquid gammaLiquid enthalpyLiquid volumeLiquid volume
31
Modify Property ModelModify Property ModelModify Property ModelModify Property Model
Check “Modify Property Model”y p y
Specify New Method Namep y
32
NRTLNRTL –– Binary ParametersBinary ParametersNRTL NRTL –– Binary ParametersBinary Parameters
Cli k “NRTL” d th b ilt i bi tClick “NRTL” and then built-in binary parameters appear automatically if available.
33
Access Properties Models and Access Properties Models and ParametersParameters
Review Databank Data
34
Review Databank DataReview Databank DataReview Databank DataReview Databank DataIncluding:Ideal gas heat of formation at 298.15 KgIdeal gas Gibbs free energy of formation at 298.15 KHeat of vaporization at TBNormal boiling pointStandard liquid volume at 60°FStandard liquid volume at 60 F….
Description of each parameter35
Pure Component Databank ParametersPure Component Databank ParametersPure Component Databank ParametersPure Component Databank Parameters
Help for Pure Component Databank Parameters 36
Pure Component Pure Component TemperatureTemperature‐‐Dependent PropertiesDependent Properties
CPIGDP‐1 ideal gas heat capacity
CPSDIP‐1 Solid heat capacity
DNLDIP‐1 Liquid density
DHVLDP‐1 Heat of vaporization
PLXANT 1 Extended Antoine EquationPLXANT‐1 Extended Antoine Equation
MULDIP Liquid viscosity
KLDIP Liquid thermal conductivityq y
SIGDIP Liquid surface tension
UFGRP UNIFAC functional group
37
Example: PLXANTExample: PLXANT‐‐1 1 (Extended Antoine Equation)(Extended Antoine Equation)
Corresponding Model
?
Click “↖?” and then click where you don’t know
?
38
Example: CPIGDPExample: CPIGDP‐‐1 1 (Ideal Gas Heat Capacity Equation)(Ideal Gas Heat Capacity Equation)
Corresponding Model
??
39
SummarySummarySummarySummary
So far, we have finished the basic settings including setup, components, and properties.This is enough to perform properties
l ianalysis.
40
File Formats in Aspen PlusFile Formats in Aspen PlusFile Formats in Aspen PlusFile Formats in Aspen Plus
File Type Extension Format Description
Document *.apw Binary File containing simulation input and results andi t di t i f tiintermediate convergence information
Backup *.bkp ASCII Archive file containing simulation input andresults
History *.his Text Detailed calculation history and diagnosticmessages
Problem * appdf Binary File containing arrays and intermediate
41
Problem Description
.appdf Binary File containing arrays and intermediateconvergence information used in the simulationcalculations
File Type CharacteristicsFile Type CharacteristicsFile Type CharacteristicsFile Type Characteristicsf l• Binary files
– Operating system and version specific– Not readable not printableNot readable, not printable
• ASCII files– Transferable between operating systems– Upwardly compatible– Contain no control characters, “readable”
N i d d b i d– Not intended to be printed• Text files
– Transferable between operating systemsTransferable between operating systems– Upwardly compatible– Readable, can be edited– Intended to be printed
42
Introduction to Aspen Plus – Part 2Properties Analysis in Aspen Plus
43
Overview of Property AnalysisOverview of Property AnalysisOverview of Property AnalysisOverview of Property AnalysisUse this form To generateUse this form To generate
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary maps showing phase envelope tie lines and azeotropes of ternaryTernary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of componentscomponents.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Ti li V B ili iTie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures
(Generic without flash calculations. Properties analysis of multi‐components (more than three) is also included.
44
RemindingRemindingRemindingReminding
• When you start properties analysis, you MUST specify components , properties model, and p y p p pcorresponding model parameters. (Refer to Part I)Part I)
45
Properties AnalysisProperties Analysis –– Pure ComponentPure ComponentProperties Analysis Properties Analysis –– Pure Component Pure Component Use this form To generate
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systemsy systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures without flash calculations. Properties analysis of multi‐components (more than three) is also included.
46
Properties AnalysisProperties Analysis –– Pure ComponentPure ComponentProperties Analysis Properties Analysis –– Pure Component Pure Component
47
Available PropertiesAvailable PropertiesAvailable PropertiesAvailable PropertiesProperty (thermodynamic) Property (transport)
Availability Free energy Thermal conductivityConstant pressureConstant pressure heat capacity Enthalpy Surface tension
Heat capacity ratio Fugacity coefficient ViscosityConstant volume heat Fugacity coefficientConstant volume heat
capacityFugacity coefficient pressure correction
Free energy departure Vapor pressure Free energy departure pressure correction Density
Enthalpy departure EntropyEnthalpy departure pressure correction Volume
Enthalpy of Sonic velocitypyvaporization Sonic velocity
Entropy departure 48
Example1: CP (Heat Capacity)Example1: CP (Heat Capacity)Example1: CP (Heat Capacity)Example1: CP (Heat Capacity)
1. Select property (CP)
4. Specify range of temperature
2. Select phase
p y g p
5 S if5. Specify pressureAdd “N-butyl-acetate”
3. Select component 6. Select property method
7. click Go to generate the results49
Example1: Calculation Results of CPExample1: Calculation Results of CPExample1: Calculation Results of CPExample1: Calculation Results of CP
Data results 50
Example2: H (Enthalpy)Example2: H (Enthalpy)Example2: H (Enthalpy)Example2: H (Enthalpy)
1. Select property (H)4. Specify range of temperature
2. Select phase
5. Specify pressure
3. Select component6 S l t t th d6. Select property method
7. click Go to generate the results51
Example: Calculation Results of HExample: Calculation Results of HExample: Calculation Results of HExample: Calculation Results of H
Data results
52
Properties AnalysisProperties Analysis –– Binary ComponentsBinary ComponentsProperties Analysis Properties Analysis –– Binary ComponentsBinary ComponentsUse this form To generate
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systemsy systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures without flash calculations. Properties analysis of multi‐components (more than three) is also included.
53
Properties AnalysisProperties Analysis –– Binary ComponentsBinary ComponentsProperties Analysis Properties Analysis –– Binary ComponentsBinary Components
Binary Component Properties AnalysisBinary Component Properties AnalysisBinary Component Properties AnalysisBinary Component Properties Analysis
Use this Analysis type To generate
Txy Temperature‐compositions diagram at constant pressure
Pxy Pressure‐compositions diagram at Pxy constant temperatureGibbs energy of mixing diagram as a function of liquid compositions. The A Ph i l P S hiGibbs energy of mixing Aspen Physical Property System uses this diagram to determine whether the binary system will form two liquid phases at a given temperature and pressureat a given temperature and pressure.
Example: TExample: T XYXYExample: TExample: T‐‐XYXY1. Select analysis type (Txy) 2. Select phase (VLE, VLLE)y yp ( y)
2. Select two component 5. Specify pressure
3. Select compositions basis
6 Select property method4. Specify composition range
6. Select property method
7. click Go to generate the results
Example: calculation result of TExample: calculation result of T XYXYExample: calculation result of TExample: calculation result of T‐‐XYXY
Data results
Example: Generate XY plotExample: Generate XY plotExample: Generate XY plotExample: Generate XY plot
Click “plot wizard” to generate XY plot
Example: Generate XY plot (cont’d)Example: Generate XY plot (cont’d)Example: Generate XY plot (cont d)Example: Generate XY plot (cont d)
Shortcoming of Binary AnalysisShortcoming of Binary AnalysisShortcoming of Binary AnalysisShortcoming of Binary Analysis
120Water-BuOH
100
110
90
100
T (o C
)
?0.0 0.2 0.4 0.6 0.8 1.0
70
80 ?
Bi A l i t t LLE d t b l t
Mole Fraction (Water)
Binary Analysis cannot generate LLE data below azeotrope.
Property AnalysisProperty Analysis –– GenericGenericProperty Analysis Property Analysis –– GenericGenericUse this form To generate
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systemsy systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures without flash calculations. Properties analysis of multi‐components (more than three) is also included.
61
Properties AnalysisProperties Analysis –– TernaryTernaryProperties Analysis Properties Analysis –– TernaryTernary
Ternary MapTernary MapTernary MapTernary Map
1 Select three component4. Select phase (VLE, LLE)
1. Select three component
5. Specify pressure2. Specify number of tie line
3. Select property method6. Specify temperature
(if LLE is slected)
7. click Go to generate the results
Calculation Result of Ternary Map (LLE)Calculation Result of Ternary Map (LLE)Calculation Result of Ternary Map (LLE)Calculation Result of Ternary Map (LLE)
D t ltData results
Property AnalysisProperty Analysis –– GenericGenericProperty Analysis Property Analysis –– GenericGenericUse this form To generate
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary systemsy systems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components.
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures without flash calculations. Properties analysis of multi‐components (more than three) is also included.
Generic analysis is used if properties analysis of mixture is performed.65
When to Use Generic AnalysisWhen to Use Generic AnalysisWhen to Use Generic Analysis When to Use Generic Analysis
Enthalpy of Mixtures?Water-BuOH
100
110
120
80
90
100
T (o C
)
LLE? Specific composition?660.0 0.2 0.4 0.6 0.8 1.0
70
80
Mole Fraction (Water)
LLE? Specific composition?
Property AnalysisProperty Analysis –– GenericGenericProperty Analysis Property Analysis –– GenericGeneric
Select Property analysis
67
Add New AnalysisAdd New AnalysisAdd New AnalysisAdd New Analysis
Select Generic
68
Specification of SystemSpecification of SystemSpecification of SystemSpecification of System
. Select “flash calculation” or not 3. Specify component flow
2. Select phase (VLE, LLE)
4 S if th di iti4. Specify the corresponding composition
69
Determine Adjusted VariablesDetermine Adjusted VariablesDetermine Adjusted VariablesDetermine Adjusted Variables
Specify feed condition
TemperaturePressureVapor fractionVapor fractionMole flowMass flowStdVol flowMole fractionMass fractionStdVol fraction
Specify range of adjusted variables70
Specify PropertySpecify Property‐‐Sets for Sets for Calculation ResultsCalculation Results
71
Add New PropertyAdd New Property Set (UserSet (User Defined)Defined)Add New PropertyAdd New Property‐‐Set (UserSet (User‐‐Defined)Defined)
Select Physical Property
Description72
Add New PropertyAdd New Property Set (cont’d)Set (cont’d)Add New PropertyAdd New Property‐‐Set (cont d)Set (cont d)If the system requires VLLE calculationIf the system requires VLLE calculation…
Select “Vapor” “1st liquid” “2nd liquid”
73
Specify PropertySpecify Property SetsSetsSpecify PropertySpecify Property‐‐SetsSets
74
Run Properties AnalysisRun Properties AnalysisRun Properties AnalysisRun Properties Analysis
Click ► to generate the resultsClick ► to generate the results
Check “simulation status”“Results Available” means convergency“Results Available” means convergency.
75
Example1: Calculation of Enthalpy Example1: Calculation of Enthalpy Change Change for binary mixturesfor binary mixtures
-60000 Molar ratio of Butanol/Water=1:1
-56000Temperature = 50oC
66000
-64000
-62000
/mol
)
Liquid Vapor
-64000-62000-60000-58000
mol
)
Liquid Vapor
-70000
-68000
-66000
Ent
halp
y (c
al/
-72000-70000-68000-66000
Ent
halp
y (c
al/m
40 50 60 70 80 90 100-74000
-72000
0.0 0.2 0.4 0.6 0.8 1.0-78000-76000-74000
ETemperature (oC) Mole fraction of Water in BuOH and Water
76
Search Physical Properties for Search Physical Properties for Enthalpy of Mixtures (HMX) Enthalpy of Mixtures (HMX)
Select HMX. Others are optimal.
Add Property-Set
77
Calculate Calculate of Enthalpy Change As of Enthalpy Change As Temperature Temperature VariesVaries
21 2
3
4
78
ReadRead Calculation ResultsCalculation ResultsRead Read Calculation ResultsCalculation Results
79
ExerciseExerciseExerciseExercise
-58000-56000
Temperature = 50oC
-66000-64000-62000-60000
cal/m
ol)
Liquid Vapor
-74000-72000-70000-68000
Ent
halp
y (c
0.0 0.2 0.4 0.6 0.8 1.0-78000-76000
Mole fraction of Water in BuOH and Water
80
Example 2: Example 2: Calculation of Calculation of LLE LLE for for Binary systemBinary system
120Water-BuOH
100
110
90
100
T (o C
)
80
0.0 0.2 0.4 0.6 0.8 1.070
Mole Fraction (Water)
81
Add New PropertyAdd New Property Set (cont’d)Set (cont’d)Add New PropertyAdd New Property‐‐Set (cont d)Set (cont d)
Select “Vapor” “1st liquid” “2nd liquid”
Specify System Variable and PropertySpecify System Variable and Property SetSetSpecify System, Variable and PropertySpecify System, Variable and Property‐‐SetSet1 2
Select Vapor-liquid-liquid
3
4
Calculation ResultsCalculation ResultsCalculation ResultsCalculation Results
110
120Water-BuOH
90
100
110
T (o C
)
0.0 0.2 0.4 0.6 0.8 1.070
80
Mole Fraction (Water)
Property AnalysisProperty Analysis –– Conceptual DesignConceptual DesignProperty Analysis Property Analysis –– Conceptual DesignConceptual DesignUse this form To generate
(Optional)
Pure Tables and plots of pure component properties as a function of temperature and pressure
Binary Txy Pxy or Gibbs energy of mixing curves for a binary systemBinary Txy, Pxy, or Gibbs energy of mixing curves for a binary system
Residue Residue curve maps
Ternary Ternary maps showing phase envelope, tie lines, and azeotropes of ternary Ternary y p g p p , , p ysystems
Azeotrope This feature locates all the azeotropes that exist among a specified set of components. p
Ternary MapsTernary diagrams in Aspen Distillation Synthesis feature: Azeotropes, Distillation boundary, Residue curves or distillation curves, Isovolatility curves, Tie lines Vapor curve Boiling pointTie lines, Vapor curve, Boiling point
Generic
Tables and plots of properties of either multi‐phase mixtures (for example, VLE, VLLE, LLE) resulting from flash calculations, or single‐phase mixtures without flash calculations Properties analysis of multi‐components (morewithout flash calculations. Properties analysis of multi‐components (more than three) is also included.
85
Conceptual DesignConceptual DesignConceptual DesignConceptual Design
Conceptual DesignConceptual DesignConceptual DesignConceptual Design
• Conceptual design enables the user to:1. Locate all the azeotropes (homogeneous and
heterogeneous) present in any multicomponent mixture2. Automatically compute distillation boundaries and
id f t i tresidue curve maps for ternary mixtures3. Compute multiple liquid phase envelopes (liquid‐liquid
and vapor liquid liquid) for ternary mixturesand vapor‐liquid‐liquid) for ternary mixtures4. Determine the feasibility of splits for distillation columns
Azeotrope AnalysisAzeotrope AnalysisAzeotrope AnalysisAzeotrope Analysis
Azeotrope AnalysisAzeotrope AnalysisAzeotrope AnalysisAzeotrope Analysis
1. Select components (at least two) 2. Specify pressure
3. Select property method
4 Select phase (VLE LLE)
6. click Report to generate the results
4. Select phase (VLE, LLE)
5. Select report Unit
Error MessageError MessageError MessageError Message
Close analysis input dialog box (pure or binary analysis)
Azeotrope Analysis ReportAzeotrope Analysis ReportAzeotrope Analysis ReportAzeotrope Analysis Report
Ternary MapsTernary MapsTernary MapsTernary Maps
Ternary MapsTernary MapsTernary MapsTernary Maps3 Select property method4. Select phase (VLE, LLE)1. Select three components3. Select property method
2. Specify pressure 5. Select report Unit
6. Click Ternary Plot to generate the results
6. Specify temperature of LLE (If liquid-liquid envelope is selected)
Ternary MapsTernary MapsTernary MapsTernary MapsChange pressure or temperaturetemperature
Ternary Plot Toolbar:Add Tie line, Curve, , ,Marker…
Introduction to Aspen Plus – Part 3 Running Simulation in Aspen Plus
95
Example 1: Calculate the mixing Example 1: Calculate the mixing properties of two stream properties of two stream
1 2 3 4Mole Flow kmol/hr
WATER 10 0 ? ?BUOH 0 9 ? ?BUAC 0 6 ? ?
Total Flow kmol/hr 10 15 ? ?C 0 80 ? ?Temperature C 50 80 ? ?
Pressure bar 1 1 1 10Enthalpy kcal/mol ? ? ? ?E t l/ l K ? ? ? ?Entropy cal/mol-K ? ? ? ?Density kmol/cum ? ? ? ?
96
Example 2: Flash SeparationExample 2: Flash SeparationExample 2: Flash SeparationExample 2: Flash Separation
120T
115
T-x T-y
Saturated Feed
T=105 CP=1atm
105
110
T (o C
)
P=1atmF=100 kmol/hrzwater=0.5 0.0 0.2 0.4 0.6 0.8 1.0
100
105
waterzHAc=0.5
What are flowrates and compositions of the two outlets?
xWater and yWater
What are flowrates and compositions of the two outlets?
Example 3: Dehydration of Acetic Example 3: Dehydration of Acetic Acid by Distillation Column Acid by Distillation Column (Optional)(Optional)
1 0
0.8
1.0
Reflux
0.4
0.6
y Wat
er
ratio ?
0 0
0.2Duty ?
0.0 0.2 0.4 0.6 0.8 1.00.0
xWater
SetupSetup –– SpecificationSpecificationSetup Setup –– SpecificationSpecification
Select Flowsheet
99
Reveal Model LibraryReveal Model LibraryReveal Model LibraryReveal Model Library
View|| Model LibraryView|| Model Libraryor press F10
100
Model Library: Mixer/SplitterModel Library: Mixer/SplitterModel Library: Mixer/SplitterModel Library: Mixer/Splitter
Model Description Purpose Use for
Mixer Stream mixer Combines multiple streams into one stream
Mixing tees. Stream mixing operations. g pAdding heat streams. Adding work streams
FSplit Stream splitter Divides feed based on splits Stream splitters BleedFSplit Stream splitter Divides feed based on splits specified for outlet streams
Stream splitters. Bleed valves
SSplit Substream splitter Divides feed based on splits Stream splitters PerfectSSplit Substream splitter Divides feed based on splits specified for each substream
Stream splitters. Perfect fluid‐solid separators
101
Model Library: Pressure ChangersModel Library: Pressure ChangersModel Library: Pressure ChangersModel Library: Pressure Changers
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Model Description Purpose Use forP h d li Ch t h th P d h d liPump Pump or hydraulic turbine
Changes stream pressure when the power requirement is needed or known
Pumps and hydraulic turbines
C Ch t h P l t iCompr Compressor or turbine
Changes stream pressure when power requirement is needed or known
Polytropic compressors, polytropic positive displacement compressors, isentropic compressorsisentropic compressors, isentropic turbines
Mcompr Multistage compressor or
Changes stream pressure across multiple stages with intercoolers
Multistage polytropiccompressors polytropiccompressor or
turbinemultiple stages with intercoolers. Allows for liquid knockout streams from intercoolers
compressors, polytropicpositive displacement compressors, isentropic compressors isentropiccompressors, isentropic turbines
Valve Valve pressure drop
Models pressure drop through a valve
Control valves and pressure changersdrop valve changers
Pipe Single segment pipe
Models pressure drop through a single segment of pipe
Pipe with constant diameter (may include fittings)
Pipeline Multiple segment Models pressure drop through a Pipeline with multiplePipeline Multiple segment pipeline
Models pressure drop through a pipe or annular space
Pipeline with multiple lengths of different diameter or elevation103
Adding a MixerAdding a MixerAdding a MixerAdding a Mixer
Click “one of icons” d th li k i th fl h t i dand then click again on the flowsheet window
Remark: The shape of the icons are meaningless
104
Adding Material StreamsAdding Material StreamsAdding Material StreamsAdding Material Streams
Click “Materials” and then click again on the flowsheet windowagain on the flowsheet window
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Adding Material Streams (cont’d)Adding Material Streams (cont’d)Adding Material Streams (cont d)Adding Material Streams (cont d)
When clicking the mouse on the flowsheet windowWhen clicking the mouse on the flowsheet window,arrows (blue and red) appear.
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Adding Material Streams (cont’d)Adding Material Streams (cont’d)Adding Material Streams (cont d)Adding Material Streams (cont d)
When moving the mouse on the arrows, some description appears.
Blue arrow: Water decant for Free water of dirty water
Red arrow(Left) Feed (Required; one ore more if mixing material
Red arrow(Right): Product (Required; if mixing material streams)of dirty water. if mixing material
streams)mixing material streams)
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Adding Material Streams (cont’d)Adding Material Streams (cont’d)Adding Material Streams (cont d)Adding Material Streams (cont d)
After selecting “Material Streams”, click and pull a stream line.Repeat it three times to generate three stream linesRepeat it three times to generate three stream lines.
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Reconnecting Material Streams Reconnecting Material Streams (Feed Stream)(Feed Stream)
Right Click on the stream and select Reconnect Destination
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Reconnecting Material Streams Reconnecting Material Streams (Product Stream)(Product Stream)
Right Click on the stream and select Reconnect Sourceselect Reconnect Source
B1
1
2
3
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Specifying Feed ConditionSpecifying Feed ConditionSpecifying Feed ConditionSpecifying Feed Condition
Right Click on the stream and select Inputand select Input
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Specifying Feed ConditionSpecifying Feed ConditionSpecifying Feed ConditionSpecifying Feed Condition
You must specify two of the following conditions:TemperaturepPressureVapor fraction
You can enter stream composition in terms of component flows, fractions, or concentrations.
If you specify component fractions, you must specify the total mole, If you specify component fractions, you must specify the total mole, mass, or standard liquid volume flow.
112
Specifying Feed Condition (cont’d)Specifying Feed Condition (cont’d)Specifying Feed Condition (cont d)Specifying Feed Condition (cont d)
1 2
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Specifying Input of MixerSpecifying Input of MixerSpecifying Input of MixerSpecifying Input of Mixer
Right Click on the block and select Input
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Specifying Input of Mixer (cont’d)Specifying Input of Mixer (cont’d)Specifying Input of Mixer (cont d)Specifying Input of Mixer (cont d)
Specify Pressure and valid phase
The corresponding description about this blank:Outlet pressure if value > 0Pressure drop if value ≦ 0
115
Run SimulationRun SimulationRun SimulationRun Simulation
Click ► to run the simulation
Run Start or continue calculations
Step Step through the flowsheet one block at a time
Stop Pause simulation calculations
Reinitialize Purge simulation results
Check “simulation status”“Required Input Complete” means the input is ready to run simualtionq p p p y
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Status of Simulation ResultsStatus of Simulation ResultsStatus of Simulation Results Status of Simulation Results
Message Means
Results available The run has completed normally, and results are presentpresent.
Results with warnings
Results for the run are present. Warning messages were generated during the l l i Vi h C l P l Hiesu ts t a gs calculations. View the Control Panel or History
for messages.
Results for the run are present. Error messages Results with errors were generated during the calculations. View the
Control Panel or History for messages.
Results for the run are present, but you have
Input Changed
p , ychanged the input since the results were generated. The results may be inconsistent with the current input.
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Control PannelControl PannelControl PannelControl Pannel
Click here
1.A message window showing the progress of the simulation by displaying the most recent messages from the calculationsrecent messages from the calculations
2.A status area showing the hierarchy and order of simulation blocks and convergenceorder of simulation blocks and convergence loops executed
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Stream ResultsStream ResultsStream ResultsStream Results
Right Click on the block andRight Click on the block and select Stream Results
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1 2 3Substream: MIXEDMole Flow kmol/hr
WATER 10 0 10BUOH 0 9 9BUOH 0 9 9BUAC 0 6 6
Total Flow kmol/hr 10 15 25Total Flow kg/hr 180.1528 1364.066 1544.218Total Flow cum/hr 0.18582 1.74021 1.870509Temperature C 50 80 70.08758Pressure bar 2 1 1V F 0 0 0Vapor Frac 0 0 0Liquid Frac 1 1 1Solid Frac 0 0 0
Enthalpy kcal/mol ‐67.81 ‐94.3726 ‐83.7476Pull down the list and select Enthalpy kcal/mol 67.81 94.3726 83.7476Enthalpy kcal/kg ‐3764.03 ‐1037.77 ‐1355.82Enthalpy Gcal/hr ‐0.6781 ‐1.41559 ‐2.09369Entropy cal/mol‐K ‐37.5007 ‐134.947 ‐95.6176
Pull down the list and select “Full” to show more properties results.
Entropy cal/gm‐K ‐2.0816 ‐1.48395 ‐1.54799Density kmol/cum 53.81564 8.619647 13.36534Density kg/cum 969.5038 783.851 825.5604Average MW 18 01528 90 93771 61 76874Average MW 18.01528 90.93771 61.76874
Liq Vol 60F cum/hr 0.1805 1.617386 1.797886120
Enthalpy and Entropy
Change Units of Calculation ResultsChange Units of Calculation ResultsChange Units of Calculation ResultsChange Units of Calculation Results
121
SetupSetup –– Defining Your Own Units SetDefining Your Own Units SetSetup Setup –– Defining Your Own Units Set Defining Your Own Units Set
122
SetupSetup –– Report OptionsReport OptionsSetup Setup –– Report OptionsReport Options
123
Stream Results with Format of Stream Results with Format of Mole FractionMole Fraction
124
Add Pump BlockAdd Pump BlockAdd Pump BlockAdd Pump Block
125
Add A Material StreamAdd A Material StreamAdd A Material StreamAdd A Material Stream
126
Connect StreamsConnect StreamsConnect StreamsConnect Streams
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PumpPump –– SpecificationSpecificationPump Pump –– Specification Specification
2. Specify pump outlet specificati
1. Select “Pump” or “turbine”
(pressure, power)
3. Efficiencies (Default: 1)
128
Run SimulationRun SimulationRun SimulationRun Simulation
Click ► to generate the resultsClick ► to generate the results
Check “simulation status”“Required Input Complete” q p p
129
Block Results (Pump)Block Results (Pump)Block Results (Pump)Block Results (Pump)
Right Click on the block and select Results
130
131
Streams ResultsStreams ResultsStreams ResultsStreams Results
132
Calculation Results Calculation Results (Mass and Energy Balances)(Mass and Energy Balances)
1 2 3 4Mole Flow kmol/hr
WATER 10 0 10 10BUOH 0 9 9 9BUAC 0 6 6 6
Total Flow kmol/hr 10 15 25 25C 0 80 0 09 1 20Temperature C 50 80 70.09 71.20
Pressure bar 1 1 1 10Enthalpy kcal/mol -67.81 -94.37 -83.75 -83.69 E t l/ l K 37 50 134 95 95 62 95 46Entropy cal/mol-K -37.50 -134.95 -95.62 -95.46 Density kmol/cum 969.50 783.85 825.56 824.29
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ExerciseExerciseExerciseExercise
1 2 3 4 5 6Mole Flow kmol/hrMole Flow kmol/hr
Water 10 0 0 ? ? ?Ethanol 0 5 0 ? ? ?
Methanol 0 0 15 ? ? ?Methanol 0 0 15 ? ? ?Total Flow kmol/hr 10 15 15 ? ? ?
Temperature C 50 70 40 ? ? ?Pressure bar 1 1 1 1 4 2essu e ba
Enthalpy kcal/mol ? ? ? ? ? ?Entropy cal/mol-K ? ? ? ? ? ?Density kmol/cum ? ? ? ? ? ?y
134Please use Peng-Robinson EOS to solve this problem.
Example 2: Flash SeparationExample 2: Flash SeparationExample 2: Flash SeparationExample 2: Flash Separation
120T
115
T-x T-y
Saturated Feed
T=105 CP=1atm
105
110
T (o C
)
P=1atmF=100 kmol/hrzwater=0.5 0.0 0.2 0.4 0.6 0.8 1.0
100
105
waterzHAc=0.5
What are flowrates and compositions of the two outlets?
xWater and yWater
What are flowrates and compositions of the two outlets?
Input ComponentsInput ComponentsInput ComponentsInput Components
Thermodynamic Model: NRTLThermodynamic Model: NRTL HOCHOCThermodynamic Model: NRTLThermodynamic Model: NRTL‐‐HOCHOC
Vapor ESHOCLiquid gammaq gLiquid enthalpyLiquid volume
Check Binary ParametersCheck Binary ParametersCheck Binary ParametersCheck Binary Parameters
Association parameters of HOCAssociation parameters of HOCAssociation parameters of HOCAssociation parameters of HOC
Binary Parameters of NRTLBinary Parameters of NRTLBinary Parameters of NRTLBinary Parameters of NRTL
Binary AnalysisBinary AnalysisBinary AnalysisBinary Analysis
TT xyxy plotplotTT‐‐xyxy plotplot
1. Select analysis type (Txy) 2. Select phase (VLE, VLLE)p ( , )
2. Select two component 5. Specify pressure
3 Select compositions basis 6. Select property method3. Select compositions basis
4. Specify composition range
7. click Go to generate the results
Calculation Result of TCalculation Result of T xyxyCalculation Result of TCalculation Result of T‐‐xyxy
Data results
GenerateGenerate xyxy plotplotGenerate Generate xyxy plotplot
GenerateGenerate xyxy plot (cont’d)plot (cont’d)Generate Generate xyxy plot (cont d)plot (cont d)
Flash SeparationFlash SeparationFlash SeparationFlash Separation
120T
115
T-x T-y
Saturated Feed
T=105 CP=1atm
105
110
T (o C
)
P=1atmF=100 kmol/hrzwater=0.5 0.0 0.2 0.4 0.6 0.8 1.0
100
105
waterzHAc=0.5
What are flowrates and compositions of the two outlets?
xWater and yWater
What are flowrates and compositions of the two outlets?
Add Block: Flash2Add Block: Flash2Add Block: Flash2Add Block: Flash2
Add Material StreamAdd Material StreamAdd Material StreamAdd Material Stream
Specify Feed ConditionSpecify Feed ConditionSpecify Feed ConditionSpecify Feed Condition
Saturated Feed(Vapor fraction=0)
P=1atmF=100 kmol/hrzwater=0.5zHAc=0.5
Block Input: Flash2Block Input: Flash2Block Input: Flash2Block Input: Flash2
Flash2: SpecificationFlash2: SpecificationFlash2: SpecificationFlash2: Specification
T=105 CP 1 tP=1atm
Required Input IncompleteRequired Input IncompleteRequired Input IncompleteRequired Input Incomplete
Connot click ► to run simulationConnot click ► to run simulation
Close binary analysis window
Required Input CompleteRequired Input CompleteRequired Input CompleteRequired Input Complete
Click ► to run simulationClick ► to run simulation
Stream ResultsStream ResultsStream ResultsStream Results
Stream Results (cont’d)Stream Results (cont’d)Stream Results (cont d)Stream Results (cont d)
42.658 kmol/hrzwater=0.501waterzHAc=0.409
T=105 CSaturated FeedP=1atmF=100 kmol/hr
P=1atm
F=100 kmol/hrzwater=0.5zHAc=0.5
57.342 kmol/hrzwater=0.432waterzHAc=0.568
Review Distillation SeparationReview Distillation SeparationReview Distillation SeparationReview Distillation Separation
1
McCabe- Thiele Graphical Method
RL D
Rectifying section: 0.8
1R
n n DR R
y x xV V
Stripping section:
0.6
y
1S
n n BS S
L By x xV V
pp g
0 2
0.4
0 0 2 0 4 0 6 0 8 10
0.2
0 0.2 0.4 0.6 0.8 1x
TradeTrade‐‐off Between off Between Capital Cost and Operating CostCapital Cost and Operating Cost
Shortcut Design:RR≈1.2×RRminNT ≈ 2×NTmin
Distillation SeparationDistillation SeparationDistillation SeparationDistillation Separation
• There are two degrees of freedom to manipulate d ll ddistillate composition and bottoms composition to manipulate the distillate andRR ? manipulate the distillate and bottoms compositions.
• If the feed condition and theIf the feed condition and the number of stages are given, how much of RR and QR are QR ?required to achieve the specification.
Add Block:Add Block: RadfracRadfracAdd Block: Add Block: RadfracRadfrac
Add Material StreamAdd Material StreamAdd Material StreamAdd Material Stream
FlowsheetFlowsheet Connectivity forConnectivity for RadFracRadFracFlowsheetFlowsheet Connectivity for Connectivity for RadFracRadFrac
RadFrac numbers stages from the top down, starting with the condenser (or starting with the top stage if there is no condenser).
Connect Material StreamConnect Material StreamConnect Material StreamConnect Material Stream
Specify Feed ConditionSpecify Feed ConditionSpecify Feed ConditionSpecify Feed Condition
Saturated Feed(Vapor fraction=0)
P=1.2atmF=100 kmol/hrzwater=0.5zHAc=0.5
Block Input:Block Input: RadfracRadfracBlock Input: Block Input: RadfracRadfrac
RadfracRadfrac: Configuration: ConfigurationRadfracRadfrac: Configuration: Configuration
RadfracRadfrac: Streams (Feed Location): Streams (Feed Location)RadfracRadfrac: Streams (Feed Location): Streams (Feed Location)
Types of Feed StageTypes of Feed StageTypes of Feed StageTypes of Feed Stage
Use this convention To introduce a feedAbove‐stage Between stages, above the designated stageg g , g gOn‐stage On the designated stage
On‐stage‐liquid On the designated stage, all‐liquid feed On stage liquid which is never flashed
On‐stage‐vapor On the designated stage, all‐vapor feed which is never flashedg p which is never flashed
Decanter To the decanter attached to the designated stagestage
RadfracRadfrac: Column Pressure: Column PressureRadfracRadfrac: Column Pressure: Column Pressure
Run SimulationRun SimulationRun SimulationRun Simulation
Click ► to run simulation
Check Convergence StatusCheck Convergence StatusCheck Convergence StatusCheck Convergence Status
Stream ResultsStream ResultsStream ResultsStream Results
D B
Change Reflux RatioChange Reflux RatioChange Reflux RatioChange Reflux Ratio
Click ► to run simulation
Increase RR from 2 to 2.5
D B
AgainAgainAgain…Again…
You can iterate RR until the specification is achievedYou can iterate RR until the specification is achieved.
Smarter WaySmarter WaySmarter WaySmarter Way
Aspen Plus provides a convenient function (Design Specs/Vary) which can iterate operating variables to meet the specification.
Add New Design SpecsAdd New Design SpecsAdd New Design SpecsAdd New Design Specs
Design Specs: SpecificationDesign Specs: SpecificationDesign Specs: SpecificationDesign Specs: Specification
Input current mole purity first
Design Specs: ComponentsDesign Specs: ComponentsDesign Specs: ComponentsDesign Specs: Components
Design Specs: Feed/Product StreamsDesign Specs: Feed/Product StreamsDesign Specs: Feed/Product StreamsDesign Specs: Feed/Product Streams
Add New VeryAdd New VeryAdd New VeryAdd New Very
Very: SpecificationsVery: SpecificationsVery: SpecificationsVery: Specifications
Not all variables cane be selected
Specify the range of the adjusted variable
Not all variables cane be selected.In this case, only reflux ratio and reboiler duty can be used.
Selection of Adjusted VariablesSelection of Adjusted VariablesSelection of Adjusted VariablesSelection of Adjusted Variables
The options of adjusted variables mustThe options of adjusted variables must correspond to the operating specification.
Run SimulationRun SimulationRun SimulationRun Simulation
Click ► to run simulationClick ► to run simulation
Check Convergence StatusCheck Convergence StatusCheck Convergence StatusCheck Convergence Status
Change Target of Mole PurityChange Target of Mole PurityChange Target of Mole PurityChange Target of Mole Purity
Click ► to run simulation
Increase Target from 0.95229424 to 0.99
Check Convergence StatusCheck Convergence StatusCheck Convergence StatusCheck Convergence Status
D B
Column Performance SummaryColumn Performance SummaryColumn Performance SummaryColumn Performance Summary
Summary of CondenserSummary of CondenserSummary of CondenserSummary of Condenser
I l d d d t di till t t fl t fl tiInclude condenser duty, distillate rate, reflux rate, reflux ratio
Summary ofSummary of ReboilerReboilerSummary of Summary of ReboilerReboiler
I l d b il d t b tt t b il t b il tiInclude reboiler duty, bottoms rate, boilup rate, boilup ratio
Column Profile: TPFQColumn Profile: TPFQColumn Profile: TPFQColumn Profile: TPFQ
Column Profile: Vapor CompositionColumn Profile: Vapor CompositionColumn Profile: Vapor CompositionColumn Profile: Vapor Composition
Column Profile: Liquid CompositionColumn Profile: Liquid CompositionColumn Profile: Liquid CompositionColumn Profile: Liquid Composition
Plot Wizard for Column ProfilePlot Wizard for Column ProfilePlot Wizard for Column ProfilePlot Wizard for Column Profile
Plot Wizard for Column Profile (cont’d)Plot Wizard for Column Profile (cont’d)Plot Wizard for Column Profile (cont d)Plot Wizard for Column Profile (cont d)
After entering the block, “Plot” appears.g , pp
Plot WizardPlot WizardPlot WizardPlot Wizard
Plot TypesPlot TypesPlot TypesPlot Types
Steps for Composition PlotSteps for Composition PlotSteps for Composition PlotSteps for Composition Plot
Composition ProfilesComposition ProfilesComposition ProfilesComposition Profiles
Temperature ProfilesTemperature ProfilesTemperature ProfilesTemperature Profiles
INTRODUCTION TO ASPEN PLUSINTRODUCTION TO ASPEN PLUSSome Tips and Others
202
Tips: NextTips: NextTips: NextTips: Next
Invokes the Aspen Plus expert system. Guides you through the steps required to complete your simulation.p q p y
Status message MeaningFlowsheet Not Complete
Flowsheet connectivity is incomplete. To find out why, click the Next button in the toolbar.
Required Input Not C l
Input specifications for the run are incomplete. Click Next h lb fi d h l h iComplete on the toolbar to find out how to complete the input
specifications, and to go to sheets that are incomplete.
203
Example: “NEXT”Example: “NEXT”Example: NEXTExample: NEXT
204
Tips: “What’s this”Tips: “What’s this”Tips: What s thisTips: What s this
Cli k “↖?” d th li k h d ’t kClick “↖?” and then click where you don’t know
?
205
Tips: “What’s this”Tips: “What’s this”Tips: What s thisTips: What s this
?
206
Tips: WindowTips: WindowTips: WindowTips: Window
If you are using You shouldWorkbook mode Click the Process Flowsheet tabFlowsheet as Wallpaper Click the flowsheet in the backgroundp p gNormal View Select the Process Flowsheet window
207
Help TopicsHelp TopicsHelp TopicsHelp Topics
Go to “Help”pSelect “Help Topics”
208
Help TopicsHelp TopicsHelp TopicsHelp Topics
U it O ti M d l R f M lUnit Operation Model Reference ManualPhysical Property Methods and ModelsPhysical Property Data Reference Manual
209
Help TopicsHelp TopicsHelp TopicsHelp TopicsCalculation of Properties Using an Equation-of-State Property Method
210
File Formats in Aspen PlusFile Formats in Aspen PlusFile Formats in Aspen PlusFile Formats in Aspen Plus
File Type Extension Format Description
Document *.apw Binary File containing simulation input and results andi t di t i f tiintermediate convergence information
Backup *.bkp ASCII Archive file containing simulation input andresults
History *.his Text Detailed calculation history and diagnosticmessages
Problem * appdf Binary File containing arrays and intermediate
211
Problem Description
.appdf Binary File containing arrays and intermediateconvergence information used in the simulationcalculations
File Type CharacteristicsFile Type CharacteristicsFile Type CharacteristicsFile Type Characteristicsf l• Binary files
– Operating system and version specific– Not readable not printableNot readable, not printable
• ASCII files– Transferable between operating systems– Upwardly compatible– Contain no control characters, “readable”
N i d d b i d– Not intended to be printed• Text files
– Transferable between operating systemsTransferable between operating systems– Upwardly compatible– Readable, can be edited– Intended to be printed
212
Access Aspen Plus SoftwareAccess Aspen Plus SoftwareAccess Aspen Plus SoftwareAccess Aspen Plus Software
• Please contact PC Teaching Assistant:Name: 侯冠宇
Phone: 02‐3366‐3005Email: chemeng@ntu edu twEmail: [email protected]: 101 電腦教室
213
如何進入講義下載及填寫問卷如何進入講義下載及填寫問卷如何進入講義下載及填寫問卷如何進入講義下載及填寫問卷