3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH Hide Contents Lingua italiana HOME Products & services Process design tools Prode Properties Prode OPC interface Applications Fluid properties Multiphase flash PHASE ENVELOPE Dew, Bubble point Distillation Hydrate formation Prode HED Prode Valves Consulting Documents Downloads Contact Prode Prode Properties Properties of pure fluids and mixtures, multi phase equilibria, process simulation, software Title : phase envelope, diagram, curve, curves, natural gas dew point, hydrate formation, Excel Matlab Mathcad software Download the free student edition, includes both 32 and 64 bit versions for Microsoft Windows Documentation, includes software installation and detailed description with application examples Do you need assistance or wish to discuss applications ? Contact Prode Application example : vaporliquidliquid phase envelope Prode Properties can calculate different types of phase diagrams vaporliquid phase envelope / phase diagram. vaporliquidliquid phase envelope / phase diagram. vaporliquidsolid phase envelope / phase diagram. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP for example the first. to access the Stream editor from Excel Properties menu select Edit Properties The Stream editor includes several pages. options) for all streams which you need to define. from the first page you can select a stream (Properties can store all the streams required to define a medium size plant) solve a series of flash operations and see the resulting compositions in the different phases. compositions etc. given a equilibrium pressure the Dew Point Temperature is the maximum temperature in VLE area Bubble Point. CricondenBar Pressure is the maximum pressure in VLE area Crcondentherm. in this page select the stream you wish to define. Matlab. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . Definitions Dew Point. given a equilibrium pressure the Bubble Point Temperature is the minimum temperature in VLE area CrcondenBar. models. 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. operating conditions. Prime or any compatible application including custom software.) Properties includes a Stream editor which permits to access all informations (as compositions. Mathcad. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH Prode Properties allows to create the diagrams directly in Excel. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP .15 H2S 0.7 CO2 0. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH In the second page you can define a new composition or modify an existing composition. in this example we define C1 0. The fourth page provides access to BIP (Binary Interaction Parameters) for the different models. here we define API Soave Redlick Kwong. you can enter specific values or click on "Load BIPs" button to get the predefined BIPs from databank.15 as molar fractions In the third page you can define the package (thermodynamic models and related options) . Now you are ready to use Properties for calculating all the properties which you need.ppp" if you wish that Properties utilizes this data as default (this is the normal . in this example for the pressure (first row) select Bar. 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. 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"). precisely to save data to a file. however there is still a last thing to do if you do not wish to lose all data when leaving a Excel page. 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.a . recommended option).. Once defined the stream you may wish to define the units which we wish to utilize in our problem. Properties saves on the file also the units of measurement so you can define different KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . in stream editor go then to the "Units" dialog here you can select the units which you need for a specific problem. you can define / modify many streams following the procedure described.. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH Finally we must save the new data. to save data to a file from Excel Properties menu select "Save a Archive" then select the file "def. To print a phase envelope you must define the stream (we select the first stream. Now you can calculate all the properties which you need with the units which you prefer for all the streams defined in that project. if required you can easily modify the code for printing a series of lines with specified liquid or vapor fraction.15 . vaporliquidliquid lines) from Prode Properties to Excel. finally click on the button "calculate phase diagram". the multiphase option instructs the procedure to generate a vaporliquidliquid phase envelope) we specify 0. Properties does all the work and the calculated equilibrium points including critical points. liquidliquidvapor.15 H2S 0.7 CO2 0. from Excel menu File>open . KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . For generating the phase envelope we?ll use a predefined Excel page distributed with Prode Properties. in Excel folder (Prode Properties installation) select the file phasenv. cricondentherm and cricondenbar are printed in Excel page for your analysis.3 value for liquid fraction. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH streams and different units in different projects. Second step: generate a vaporliquidliquid phase envelope in Excel.xls This page contains a little VBA code to tranfer the calculated equilibrium values (for the different vaporliquid. which we defined with composition C1 0. SRK as model and multiphase vapor+liquid option. the procedure allows to specify any value (from 0 dew line to 1 bubble line) for phase fractions. Note that Prode Properties calculates the TRUE critical points (not the estimated values). CricondenBar and CricondenTherm are available in Excel. herebelow the example of a line with 0. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . Prode Properties includes a proprietary procedure based on Gibbs minimization method.05 liquid fraction. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH The phase envelope for this mixture shows a three phase area (notice the second line near the liquidliquidvapor bubble line and the third liquidvaporliquid line The calculated values for Critical Points. herebelow is the example of the mixture with composition Methane 0. The bubble line is a three phase (liquidliquidvapor) line. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH The VaporLiquidLiquid phase envelope constitutes the ideal tool to investigate the phase equilibria for mixtures of hydrocarbons + water The example shows the phase envelope for a 12 components (hydrocarbons + water) mixture. a vaporliquid line connects the end of the liquidliquidvapor line with critical point.05 KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP .9 H2S 0.1 model API Soave Redlick Kwong. notice the large three phase area where liquid water is present. the blue line shows a liquid fraction of 0. the dew line doesn't stop at critical point but continues. Note that even simple compositions can show a complex behaviour. methods StrCTp() and StrCTt() returns the pressure (or temperature) of the CricondenTherm (the equilibrium point with maximum temperature). CricondenBar and CricondenTherm in Excel cells. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH Note that Prode Properties includes methods for calculating critical points. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . 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). 1) refers to the stream 1 and first critical point detected.1) =PfTF(2.1.0.999 nButane 0.0. int state. to calculate the points on the dew line we use the method: double p = PfTF(integer stream.B1.2) =PfTF(2. the same would be by setting the state as gas and phase fraction as 1. in B2 we enter the macro =StrTc(1. double pf. we enter this macro in B1.0) the fourth (1) is the state (in Properties 0 = gas. then in cells B2.001) shows up to four saturation point pressures at the same temperature Observe the dew line.1. 2 = solid) and the last is the required position (we require the points 13 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. the red line below the critical point.B1.1) to calculate the critical temperature in the same way. B3.1. there are up to three different equilibrium points at the same temperature (the area around 190 K).3) where the first value (2) is the stream which we defined. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH To get the value of critical pressure enter the macro =StrPc(1.B1. int n) In cell B1 we define a value for the equilibrium temperature (190. B4 we enter the macros =PfTF(2. in cells B3 and B4 we enter the macros = StrCBp(1) for CricodenBar pressure and = StrCTt(1) for CricodenTherm temperature.208 K) . KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP .0. 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.1) where (1. the second (cell B1) represents the temperature. 1 = liquid. double t. The phase envelope for this mixture (Methane 0. the third (0) is the phase fraction (with 0 we specify 0% liquid or a point on dew line. Van Der WaalsPlatteeuw) additional models as Pitzer. NRTL for electrolyte solutions. van der Waals and complex mixing rules to combine equations of state with activity models Huron Vidal Wong Sandler ( WS ) Michelsen ( MHV2 ) Tassios et al. for example >>StrPc(1) will return the true critical pressure of stream 1. density and enthalpy) Benedict Webb Rubin (Starling) BWRS Steam Tables IAPWS 95 ISO 18453 (GERG 2004) ISO 20765 (AGA 8 model) LeeKesler (Plocker) LKP CPA Cubic Plus Association (SRK and PR variants) Hydrates (Cubic Plus Association. if you wish to obtain additional properties as cricondentherm. density and enthalpy) PengRobinson (standard and extended version with parameters calculated for best fitting of vapor pressure. Prode Properties will calculate the phase envelope and print the result on Matlab. GERG (2008) etc. in Matlab command line type >>phaseenvelope(1) where (1) is the number of stream. absorbers. technical features overview (Windows version) Entirely written in C++ (since first edition. KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . the user can add new components and BIPs Proprietary 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. PC SAFT (with association). cricondenbar or critical points just enter the name of Properties method in Matlab. base version includes Regular Wilson NRTL UNIQUAC UNIFAC SoaveRedlichKwong (standard and extended version with parameters calculated for best fitting of vapor pressure. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH For calculating and printing the phase envelope we?ll use a predefined script distributed with Prode Properties. fractionations. 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. Prode Properties. ( 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 transfer Procedure for solving staged columns Rigorous solution of distillation columns. Comprehensive set of thermodynamic models. . Nonhomogeneous Nonequilibrium 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 transfer Procedure 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. includes isochoric flash Flash at given volume (V) and T multiphase vaporliquidsolid. includes isochoric flash Flash at given volume (V) and enthalpy (H) multiphase vaporliquidsolid Flash at given volume (V) and entropy (S) multiphase vaporliquidsolid Flash at given enthalpy (H) and entropy (S) multiphase vaporliquidsolid Rigorous (True) critical point plus Cricondentherm and Cricondenbar Complete set of properties for different states gas density vapor density liquid density solid 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/cv liquid cp/cv Gas heating value Gas Wobbe index Gas Specific gravity gas Joule Thomson coefficients vapor Joule Thomson coefficients liquid Joule Thomson coefficients gas Isothermal compressibility vapor Isothermal compressibility liquid Isothermal compressibility gas Volumetric expansivity vapor Volumetric expansivity KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . gas separator. Procedure for calculating hydrate formation temperature and hydrate formation pressure hydrate phase equilibria based on different Van Der WaalsPlatteeuw models Procedure for solving polytropic compression with phase equilibria Huntington method for gas phase Proprietary method for solving a polytropic process with phase equilibria Procedure for solving isentropic nozzle (safety. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH strippers. includes adiabatic flash Flash at given entropy (S) and P multiphase vaporliquidsolid.. Homogeneous Nonequilibrium NHNE. liquid separator) ** Functions for accessing component data in database (the user can define mixing rules) gas / vaporliquidsolid fugacity plus derivatives vs. relief valve with single and two phase flow) HEM. temperature pressure composition gas / vaporliquidsolid enthalpy plus derivatives vs. includes isentropic flash Flash at given volume (V) and P multiphase vaporliquidsolid. solves up to 5 different points Flash at given enthalpy (H) and P multiphase vaporliquidsolid. isothermal flash Flash at given phase fraction and P (or T). Homogeneous Equilibrium HNEDS. temperature pressure composition gas / vaporliquidsolid entropy plus derivatives vs. temperature pressure composition Flash at Bubble and Dew point specifications and P (or T) Flash at given temperature (T) and pressure (P) multiphase vaporliquidsolid. includes isentropic flash Flash at given entropy (S) and T multiphase vaporliquidsolid. temperature pressure composition gas / vaporliquidsolid molar volume plus derivatives vs. includes adiabatic flash Flash at given enthalpy (H) and T multiphase vaporliquidsolid. chemical. petrochemical. hydrocarbon. air conditioning. physical. Matlab. 3KDVHHQYHORSHGLDJUDPFXUYHFXUYHV([FHO0DWODEVRIWZDUH liquid Volumetric expansivity gas Speed of sound vapor Speed of sound liquid Speed of sound vapor + liquid (HEM) Speed of sound gas Viscosity vapor Viscosity liquid Viscosity gas Thermal conductivity vapor Thermal conductivity liquid Thermal conductivity gas compressibility factor vapor compressibility factor liquid Surface tension Typical applications Fluid properties in Excel. thermophysical properties Process simulation Heat / Material Balance Process Control Process Optimization Equipments Design Separations Instruments Design Realtime applications petroleum refining. natural gas. mechanical industry KWWS ZZZSURGHFRPHQSKDVHHQYHORSHKWP . pharmaceutical. Mathcad and other Windows and UNIX (**) applications Thermodynamics. energy.