Phase Envelope, Diagram, Curve, Curves, Excel Matlab Software

8/17/2019 Phase Envelope, Diagram, Curve, Curves, Excel Matlab Software

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Prode PropertiesProperties of pure fluids and mixtures, multi phase equilibria,process simulation, software

Title : phase envelope, diagram, curve, curves, natural gas dew point, hydrateformation, Excel Matlab Mathcad software

Download the free student edition, includes both 32 and 64 bitversions for Microsoft Windows

Documentation, includes software installation and detaileddescription with application examples

Do you need assistance or wish to discuss applications ?Contact Prode

Application example : vapor-liquid-liquid phase envelope

Prode Properties can calculate different types of phase diagrams

vapor-liquid phase envelope / phase diagram.

vapor-liquid-liquid phase envelope / phase diagram.

vapor-liquid-solid phase envelope / phase diagram.

http://www.prode.com/en/contact.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/docs/pppman.pdfhttp://www.prode.com/docs/pppman.pdfhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/hed.htmhttp://www.prode.com/en/hydrate.htmhttp://www.prode.com/en/dewpointnaturalgashydrocarbons.htmhttp://www.prode.com/en/ppp.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/docs/pppman.pdfhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/contact.htmhttp://www.prode.com/en/download.htmhttp://www.prode.com/en/valves.htmhttp://www.prode.com/en/hed.htmhttp://www.prode.com/en/hydrate.htmhttp://www.prode.com/en/distillationcolumn.htmhttp://www.prode.com/en/dewpointnaturalgashydrocarbons.htmhttp://www.prode.com/en/phaseenvelope.htmhttp://www.prode.com/en/multiphase.htmhttp://www.prode.com/en/properties.htmhttp://www.prode.com/en/opcgashydrocarbon.htmhttp://www.prode.com/en/ppp.htmhttp://www.prode.com/http://www.prode.com/it/default.htm


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Prode Properties allows to create the diagrams directly in Excel, Matlab, Mathcad, Prime

or any compatible application including custom software.

Definitions

Dew Point, given a equilibrium pressure the Dew Point Temperature is the

maximum temperature in VLE area

Bubble Point, given a equilibrium pressure the Bubble Point Temperature is the

minimum temperature in VLE areaCrcondenBar, CricondenBar Pressure is the maximum pressure in VLE area

Crcondentherm, Cricondentherm temperature is the maximum temperature in

VLE area

Step by Step instruction to create a phase diagram with Excel /Matlab / Mathcad

First step: define the stream (components, compositions etc.)

Properties includes a Stream editor which permits to access all informations (as

compositions, operating conditions, models, options) for all streams which you need todefine, to access the Stream editor from Excel Properties menu select Edit Properties

The Stream editor includes several pages, from the first page you can select a stream

(Properties can store all the streams required to define a medium size plant) solve aseries of flash operations and see the resulting compositions in the different phases, in

this page select the stream you wish to define, for example the first.


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Finally we must save the new data, in the first page click on "Save" button, note that

you can redefine the name of the stream as you wish (editing the cell near the button

"Save"), you can define / modify many streams following the procedure described.Once defined the stream you may wish to define the units which we wish to utilize in our

problem, in stream editor go then to the "Units" dialog

here you can select the units which you need for a specific problem, in this example forthe pressure (first row) select Bar.a , notice that unit for temperature is K (but you can

set the units which you prefer) then click on Ok button to accept new values and leave

the Properties editor.

Now you are ready to use Properties for calculating all the properties which you need,however there is still a last thing to do if you do not wish to lose all data when leaving a

Excel page, precisely to save data to a file, to save data to a file from Excel Properties

menu select "Save a Archive"

then select the file "def.ppp" if you wish that Properties utilizes this data as default (thisis the normal , recommended option), differently set a different name (you can for

example define different names for different projects) but you will need to load that

specific Archive before to make calc's for that project and since Excel reloads Properties

with any new page this may result tedious...

Properties saves on the file also the units of measurement so you can define different


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streams and different units in different projects.

Now you can calculate all the properties which you need with the units which you preferfor all the streams defined in that project.

Second step: generate a vapor-liquid-liquid phase envelope inExcel.

For generating the phase envelope we?ll use a predefined Excel page distributed with

Prode Properties, from Excel menu File->open , in Excel folder (Prode Properties

installation) select the file phasenv.xls

This page contains a little VBA code to tranfer the calculated equilibrium values (for the

different vapor-liquid, liquid-liquid-vapor, vapor-liquid-liquid lines) from Prode Properties

to Excel, if required you can easily modify the code for printing a series of lines withspecified liquid or vapor fraction. To print a phase envelope you must define the stream

(we select the first stream, which we defined with composition C1 0.7 CO2 0.15 H2S

0.15 , SRK as model and multiphase vapor+liquid option, the multiphase option instructs

the procedure to generate a vapor-liquid-liquid phase envelope) we specify 0.3 value forliquid fraction, finally click on the button "calculate phase diagram".

Properties does all the work and the calculated equilibrium points including critical

points, cricondentherm and cricondenbar are printed in Excel page for your analysis.


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The Vapor-Liquid-Liquid phase envelope constitutes the ideal tool to investigate thephase equilibria for mixtures of hydrocarbons + water

The example shows the phase envelope for a 12 components (hydrocarbons + water)

mixture, notice the large three phase area where liquid water is present.

Note that even simple compositions can show a complex behaviour, herebelow is the

example of the mixture with composition Methane 0.9 H2S 0.1 model API Soave Redlick

Kwong.The bubble line is a three phase (liquid-liquid-vapor) line, a vapor-liquid line connects

the end of the liquid-liquid-vapor line with critical point, the dew line doesn't stop at

critical point but continues, the blue line shows a liquid fraction of 0.05


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Note that Prode Properties includes methods for calculating critical points, CricondenBarand CricondenTherm in Excel cells, see the paragraph "Methods for thermodynamic calc?

s" in operating manual for the details.

methods StrPc() and StrTc() returns the critical pressure (or temperature) of the

nth (from 1 to 5) critical point found.methods StrCBp() and StrCBt() returns the pressure (or temperature) of the

CricondenBar (the equilibrium point with maximum pressure).

methods StrCTp() and StrCTt() returns the pressure (or temperature) of the

CricondenTherm (the equilibrium point with maximum temperature).


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To get the value of critical pressure enter the macro =StrPc(1,1) where (1,1) refers tothe stream 1 and first critical point detected, we enter this macro in B1, in B2 we enter

the macro =StrTc(1,1) to calculate the critical temperature in the same way, in cells B3

and B4 we enter the macros = StrCBp(1) for CricodenBar pressure and = StrCTt(1) for

CricodenTherm temperature.

The phase envelope for this mixture (Methane 0.999 n-Butane 0.001) shows up to foursaturation point pressures at the same temperature

Observe the dew line, the red line below the critical point, there are up to three different

equilibrium points at the same temperature (the area around 190 K), if you add the

saturation point on the bubble line (black line) we have a total of four saturation point

pressures at a given temperature, to calculate the points on the dew line we use the

method:

double p = PfTF(integer stream, double t, double pf, int state, int n)

In cell B1 we define a value for the equilibrium temperature (190.208 K) , then in cells

B2, B3, B4 we enter the macros

=PfTF(2,B1,0,1,1)

=PfTF(2,B1,0,1,2)

=PfTF(2,B1,0,1,3)

where the first value (2) is the stream which we defined, the second (cell B1) represents

the temperature, the third (0) is the phase fraction (with 0 we specify 0% liquid or a

point on dew line, the same would be by setting the state as gas and phase fraction as

1.0) the fourth (1) is the state (in Properties 0 = gas, 1 = liquid, 2 = solid) and the lastis the required position (we require the points 1-3 along the dew line)

For additional infrmation about how to calculate equilibrium points go to the page Dew

Points Natural Gas Hydrocarbons

Print a phase envelope in Matlab.

http://www.prode.com/en/dewpointnaturalgashydrocarbons.htm


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For calculating and printing the phase envelope we?ll use a predefined script distributed

with Prode Properties, in Matlab command line type>>phaseenvelope(1)

where (1) is the number of stream.

Prode Properties will calculate the phase envelope and print the result on Matlab, if youwish to obtain additional properties as cricondentherm, cricondenbar or critical points

just enter the name of Properties method in Matlab, for example

>>StrPc(1)

will return the true critical pressure of stream 1.

Prode Properties, technical features overview (Windowsversion)

Entirely written in C++ (since first edition, 1993)Up to 100 different streams with up to 50 components per stream (user can

redefine)

Several compilations of chemical data and BIPs are available, the user can add

new components and BIPsProprietary compilation with data for more than 1600 chemicals and

30000 BIPs

flexible database format (support for up to 30 different correlations)

works with all majour standards including DIPPR.

Comprehensive set of thermodynamic models, base version includesRegular

Wilson

NRTL

UNIQUAC

UNIFACSoave-Redlich-Kwong (standard and extended version with parameters

calculated for best fitting of vapor pressure, density and enthalpy)

Peng-Robinson (standard and extended version with parameters

calculated for best fitting of vapor pressure, density and enthalpy)Benedict Webb Rubin (Starling) BWRS

Steam Tables IAPWS 95

ISO 18453 (GERG 2004)

ISO 20765 (AGA 8 model)

Lee-Kesler (Plocker) LKPCPA Cubic Plus Association (SRK and PR variants)

Hydrates (Cubic Plus Association, Van Der Waals-Platteeuw)

additional models as Pitzer, NRTL for electrolyte solutions, PC SAFT (with

association), GERG (2008) etc.

van der Waals and complex mixing rules to combine equations of state withactivity models

Huron Vidal

Wong Sandler ( WS )

Michelsen ( MHV2 )

Tassios et al. ( LCVM )Base and Extended EOS versions with parameters calculated to fit experimental

data from DIPPR and DDB

Selectable units of measurement

Procedure for solving fluid flow including multi phase equilibria and heat transferProcedure for solving staged columns

Rigorous solution of distillation columns, fractionations, absorbers,


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strippers...Procedure for calculating hydrate formation temperature and hydrate formationpressure

hydrate phase equilibria based on different Van Der Waals-Platteeuw

models

Procedure for solving polytropic compression with phase equilibria

Huntington method for gas phaseProprietary method for solving a polytropic process with phase equilibria

Procedure for solving isentropic nozzle (safety, relief valve with single and two

phase flow)

HEM, Homogeneous Equilibrium

HNE-DS, Homogeneous Non-equilibriumNHNE, Non-homogeneous Non-equilibrium

Procedure for simulating fluid flow in piping (pipelines) with heat transfer

Beggs and Brill and proprietary methods for single phase and multiphase

fluid flow with heat transferProcedure for fitting BIP to measured VLE / LLE / SLE data points (data

regression)

Procedure for fitting BIP to VLE values calculated with UNIFAC

Functions for simulating operating blocks (mixer, gas separator, liquid separator)

**Functions for accessing component data in database (the user can define mixing

rules)

gas / vapor-liquid-solid fugacity plus derivatives vs. temperature pressure

composition

gas / vapor-liquid-solid enthalpy plus derivatives vs. temperature pressurecomposition

gas / vapor-liquid-solid entropy plus derivatives vs. temperature pressure

composition

gas / vapor-liquid-solid molar volume plus derivatives vs. temperature pressurecomposition

Flash at Bubble and Dew point specifications and P (or T)

Flash at given temperature (T) and pressure (P) multiphase vapor-liquid-solid,

isothermal flash

Flash at given phase fraction and P (or T), solves up to 5 different pointsFlash at given enthalpy (H) and P multiphase vapor-liquid-solid, includes

adiabatic flash

Flash at given enthalpy (H) and T multiphase vapor-liquid-solid, includes

adiabatic flash

Flash at given entropy (S) and P multiphase vapor-liquid-solid, includesisentropic flash

Flash at given entropy (S) and T multiphase vapor-liquid-solid, includes

isentropic flash

Flash at given volume (V) and P multiphase vapor-liquid-solid, includes isochoricflash

Flash at given volume (V) and T multiphase vapor-liquid-solid, includes isochoric

flash

Flash at given volume (V) and enthalpy (H) multiphase vapor-liquid-solid

Flash at given volume (V) and entropy (S) multiphase vapor-liquid-solidFlash at given enthalpy (H) and entropy (S) multiphase vapor-liquid-solid

Rigorous (True) critical point plus Cricondentherm and Cricondenbar

Complete set of properties for different states

gas density

vapor density

liquid densitysolid density

gas Isobaric specific heat (Cp)

vapor Isobaric specific heat (Cp)liquid Isobaric specific heat (Cp)

gas Isochoric specific heat (Cv)

vapor Isochoric specific heat (Cv)

liquid Isochoric specific heat (Cv)

gas cp/cvliquid cp/cv

Gas heating value

Gas Wobbe index

Gas Specific gravity

gas Joule Thomson coefficients

vapor Joule Thomson coefficientsliquid Joule Thomson coefficients

gas Isothermal compressibility

vapor Isothermal compressibilityliquid Isothermal compressibility

gas Volumetric expansivity

vapor Volumetric expansivity


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liquid Volumetric expansivity

gas Speed of soundvapor Speed of sound

liquid Speed of sound

vapor + liquid (HEM) Speed of sound

gas Viscosity

vapor Viscosityliquid Viscosity

gas Thermal conductivity

vapor Thermal conductivity

liquid Thermal conductivity

gas compressibility factorvapor compressibility factor

liquid Surface tension

Typical applications

Fluid properties in Excel, Matlab, Mathcad and other Windows and UNIX (**)

applicationsThermodynamics, physical, thermophysical properties

Process simulation

Heat / Material Balance

Process Control

Process OptimizationEquipments Design

Separations

Instruments Design

Realtime applicationspetroleum refining, natural gas, hydrocarbon, chemical, petrochemical,

pharmaceutical, air conditioning, energy, mechanical industry

Phase Envelope, Diagram, Curve, Curves, Excel Matlab Software

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