Peng-Robinson (PR)¶

Peng-Robinson cubic equation of state (1976) with the van der Waals one-fluid mixing rules and binary interaction parameters k_ij from the databank. The general-purpose package for hydrocarbons, natural gas and light gases.

DWSIM.Thermodynamics.PropertyPackages.PengRobinsonPropertyPackage
Assembly DWSIM.Thermodynamics.dll · Object ← PropertyPackage ← PengRobinsonPropertyPackage
Name in the flowsheet Peng-Robinson (PR) · FluentAPI PropertyPackages.PengRobinson

Scope¶

The general-purpose equation of state of DWSIM for hydrocarbons and the light gases that come with them (N₂, CO₂, H₂S, H₂): natural gas, gas processing, refinery light ends, compression and expansion, high-pressure vapor-liquid equilibrium. The same equation gives the fugacity coefficients of both phases, so the package works from vacuum to well above the critical pressure of the mixture.

The Peng-Robinson (1976) equation, P = RT/(V - b) - a(T)/[V(V + b) + b(V - b)], takes the co-volume b = 0.07780 RT_c/P_c and the attraction parameter a = 0.45724 (R²T_c²/P_c) α(T), with α = [1 + m(1 - T_r^1/2)]² and m = 0.37464 + 1.54226ω - 0.26992ω². Mixtures use the van der Waals one-fluid rules, a_m = ΣΣ x_ix_j(a_ia_j)^1/2(1 - k_ij) and b_m = Σ x_ib_i. The cubic in Z has up to three roots; the liquid takes the smallest and the vapor the largest. Enthalpy and entropy are the ideal-gas values (from the ideal gas heat capacity) plus the departure functions of the equation.

Parameters. T_c, P_c and ω come from the compound database. The binary interaction parameters k_ij come from a databank shipped with DWSIM; a pair that is not in it has k_ij = 0. They can be changed in the package editor, or from code with ConfigurePR(c => c.WithKij(...)) as in the example, and are saved with the flowsheet.

Liquid density. By default the liquid density comes from the experimental data of the compound, or the Rackett equation where there are none. The equation-of-state density, with the Peneloux volume translation, is an option of the package settings. The volume shift corrects the liquid molar volume and leaves the phase equilibrium unchanged.

Derivatives. The package provides analytical temperature and composition derivatives of the fugacity coefficients, which the vapor-fraction flashes and the rigorous column solvers use.

Limitations¶

Two-parameter cubic equations predict liquid molar volumes poorly, which is why the default liquid density comes from correlations.
Polar and associating liquids (water with alcohols, glycols, acids) are outside the model. Use NRTL or UNIQUAC at low pressure, or the CPA and SAFT models of ThermoPack.
A missing k_ij is zero. For pairs that matter (CO₂, H₂S, N₂ or H₂ with hydrocarbons; methane with heavy ends) check that the databank has a value.
A stream with a single compound (mole fraction above 0.99999) is flashed on the vapor pressure curve of the compound database, so its saturation pressure is that of the correlation.
For heavy hydrocarbons (ω above 0.49) Peng-Robinson 1978 gives better vapor pressures with the same parameters.

Example¶

This code runs on every build of this site, and the output below is what it printed.

Python

gas = ["Methane", "Ethane", "Propane", "N-butane", "N-pentane", "N-hexane"]
z = [0.88, 0.06, 0.03, 0.015, 0.01, 0.005]          # mole fractions
fs = (Flowsheet.Create("PengRobinsonExample")
      .WithCompounds(*gas)
      .WithPropertyPackage(PropertyPackages.PengRobinson))

methane = (fs.AddMaterialStream("Methane")
           .At(Q.Celsius(25.0), Q.Bar(50.0))
           .SetCompoundMolarFlow("Methane", 1.0))
cold = fs.AddMaterialStream("Gas at -20 C").At(Q.Celsius(-20.0), Q.Bar(50.0))
dew = fs.AddMaterialStream("Dew point").WithPressure(Q.Bar(50.0)).WithVaporFraction(1.0)
for name, x in zip(gas, z):
    cold.SetCompoundMolarFlow(name, x)
    dew.SetCompoundMolarFlow(name, x)

# the same gas with kij(methane, n-hexane) = 0 in place of the databank value, set through
# the typed package configuration (an extension method, called as a static method from Python)
fs0 = PropertyPackageConfigExtensions.WithPropertyPackage(
    Flowsheet.Create("NoKij").WithCompounds(*gas), PropertyPackages.PengRobinson,
    Action[PropertyPackageBuilder](lambda pp: pp.ConfigurePR(
        Action[PRConfig](lambda c: c.WithKij("Methane", "N-hexane", 0.0)))))
dew0 = fs0.AddMaterialStream("Dew point").WithPressure(Q.Bar(50.0)).WithVaporFraction(1.0)
for name, x in zip(gas, z):
    dew0.SetCompoundMolarFlow(name, x)

fs.Solve()
fs0.Solve()

pr = list(fs.Inner.PropertyPackages.Values)[0].__implementation__
kij = pr.m_pr.InteractionParameters["Methane"]["N-hexane"].kij
m, s = methane.Object.Phases[2].Properties, cold.Object
print(f"Methane density      = {m.density:.2f} kg/m3 (Z = {m.compressibilityFactor:.4f})")
print(f"Vapor fraction       = {s.Phases[2].Properties.molarfraction:.4f} (gas at -20 C)")
print(f"Vapor density        = {s.Phases[2].Properties.density:.2f} kg/m3")
print(f"Methane in liquid    = {s.Phases[3].Compounds['Methane'].MoleFraction:.4f} (mole fraction)")
print(f"Dew point            = {dew.Object.GetTemperature() - 273.15:.2f} C (kij methane/n-hexane = {kij:.4f})")
print(f"Dew point, kij = 0   = {dew0.Object.GetTemperature() - 273.15:.2f} C")

Output

Methane density      = 35.63 kg/m3 (Z = 0.9082)
Vapor fraction       = 0.9451 (gas at -20 C)
Vapor density        = 54.72 kg/m3
Methane in liquid    = 0.3333 (mole fraction)
Dew point            = 23.97 C (kij methane/n-hexane = 0.0400)
Dew point, kij = 0   = 23.81 C

DWSIM 10.2.11.0, generated 2026-10-08.

Property methods¶

How the package calculates each property, as it reports it in PropertyMethodsInfo (the property package editor shows the same list).

Property	Method
Vapor fugacity	Peng-Robinson EOS
Liquid fugacity	Peng-Robinson EOS
Vapor enthalpy, entropy, Cp/Cv	Peng-Robinson EOS
Liquid enthalpy, entropy, Cp/Cv	Peng-Robinson EOS
Vapor density	Peng-Robinson EOS (+VT)
Liquid density	Peng-Robinson EOS (+VT) / Experimental / Rackett / COSTALD
Vapor viscosity	Experimental / Lucas / Jossi-Stiel-Thodos
Liquid viscosity	Experimental / Letsou-Stiel
Vapor thermal conductivity	Experimental / Ely-Hanley
Liquid thermal conductivity	Experimental / Latini
Surface tension	Experimental / Brock-Bird
Solid density	Experimental Data / User-Defined
Solid enthalpy, entropy, Cp/Cv	Experimental Solid Cp / From Liquid Phase Enthalpy + Enthalpy of Fusion

Default flash algorithm: Universal.

Configuration saved with the flowsheet¶

The package writes its settings to the simulation file (SaveData) and reads them back on load (LoadData). The elements below are the ones this package adds to those of every property package, as written for the example.

Element	Content in the example	What it holds
`InteractionParameters`	14 `InteractionParameter` entries (`Compound1`, `Compound2`, `Value`)	k_ij (`Value`) of the pairs of the flowsheet compounds, from the databank or entered in the package editor

First InteractionParameter of InteractionParameters in the example

<InteractionParameter Compound1="Methane" Compound2="Ethane" Value="-0.0033" />

Settings common to every property package, as saved for the example

Element	Value
`Type`	65 characters
`ComponentName`	`Peng-Robinson (PR)`
`ComponentDescription`
`Tag`	`Peng-Robinson (PR)`
`UseHenryConstants`	`true`
`AutoEstimateMissingNRTLUNIQUACParameters`	`true`
`UseImmiscibleListForLiquid2InitialEstimates`	`true`
`SingleCompoundCheckThreshold`	`0.99999`
`OverrideKvalFugCoeff`	`false`
`OverrideEnthalpyCalculation`	`false`
`OverrideEntropyCalculation`	`false`
`LiquidDensityCalculationMode_Subcritical`	`Rackett_and_ExpData`
`LiquidDensityCalculationMode_Supercritical`	`Rackett_and_ExpData`
`LiquidDensity_CorrectExpDataForPressure`	`true`
`LiquidDensity_UsePenelouxVolumeTranslation`	`true`
`LiquidViscosityCalculationMode_Subcritical`	`ExpData`
`LiquidViscosityCalculationMode_Supercritical`	`Letsou_Stiel`
`LiquidViscosity_CorrectExpDataForPressure`	`true`
`LiquidViscosity_MixingRule`	`MoleAverage`
`VaporPhaseFugacityCalculationMode`	`Ideal`
`SolidPhaseFugacityCalculationMethod`	`FromLiquidFugacity`
`SolidPhaseFugacity_UseIdealLiquidPhaseFugacity`	`false`
`SolidPhaseEnthalpy_UsesCp`	`false`
`EnthalpyEntropyCpCvCalculationMode`	`LeeKesler`
`LiquidEnthalpyEntropyCpCvCalculationMode_EOS`	`EOS`
`LiquidFugacity_UsePoyntingCorrectionFactor`	`true`
`ActivityCoefficientModels_IgnoreMissingInteractionParameters`	`false`
`IgnoreVaporFractionLimit`	`false`
`IgnoreSalinityLimit`	`false`
`CalculateAdditionalMaterialStreamProperties`	`true`
`FlashCalculationApproach`	`NestedLoops`
`DisplayMissingCompoundPropertiesWarning`	`false`
`ForcedSolids`	`[]`
`PropertyOverrides`	`{}`
`FlashSettings`	36 `Setting` entries

Learn more¶

API members¶

Public members declared by this class. Inherited members are documented on the base classes.

Constructors¶

PengRobinsonPropertyPackage()

C#VB.NET

public PengRobinsonPropertyPackage()

Public Sub New()

PengRobinsonPropertyPackage(bool)

Parameter	Type	Description
`comode`	`Boolean`

C#VB.NET

public PengRobinsonPropertyPackage(bool comode)

Public Sub New(comode As Boolean)

Properties¶

DisplayDescription

C#VB.NET

public override string DisplayDescription { get; }

Public Overrides ReadOnly Property DisplayDescription As String

DisplayName

C#VB.NET

public override string DisplayName { get; }

Public Overrides ReadOnly Property DisplayName As String

ImplementsAnalyticalDerivatives

C#VB.NET

public override bool ImplementsAnalyticalDerivatives { get; }

Public Overrides ReadOnly Property ImplementsAnalyticalDerivatives As Boolean

MobileCompatible

C#VB.NET

public override bool MobileCompatible { get; }

Public Overrides ReadOnly Property MobileCompatible As Boolean

Popular

C#VB.NET

public override bool Popular { get; }

Public Overrides ReadOnly Property Popular As Boolean

Methods¶

AUX_CM(object)

Parameter	Type	Description
`Vx`	`Object`

C#VB.NET

public double AUX_CM(object Vx)

Public Function AUX_CM(Vx As Object) As Double

AUX_CM(Phase)

Parameter	Type	Description
`Phase`	`Phase`

C#VB.NET

public double AUX_CM(Phase Phase)

Public Function AUX_CM(Phase As Phase) As Double

AUX_VAPDENS(double, double)

Parameter	Type	Description
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double AUX_VAPDENS(double T, double P)

Public Overrides Function AUX_VAPDENS(T As Double, P As Double) As Double

AUX_Z(double[], double, double, PhaseName)

Parameter	Type	Description
`Vx`	`Double[]`
`T`	`Double`
`P`	`Double`
`state`	`PhaseName`

C#VB.NET

public override double AUX_Z(double[] Vx, double T, double P, PhaseName state)

Public Overrides Function AUX_Z(Vx As Double(), T As Double, P As Double, state As PhaseName) As Double

CalcIsothermalCompressibility(IPhase)

Parameter	Type	Description
`p`	`IPhase`

C#VB.NET

public override double CalcIsothermalCompressibility(IPhase p)

Public Overrides Function CalcIsothermalCompressibility(p As IPhase) As Double

CalcJouleThomsonCoefficient(IPhase)

Parameter	Type	Description
`p`	`IPhase`

C#VB.NET

public override double CalcJouleThomsonCoefficient(IPhase p)

Public Overrides Function CalcJouleThomsonCoefficient(p As IPhase) As Double

ConfigParameters()

C#VB.NET

public override void ConfigParameters()

Public Overrides Sub ConfigParameters()

DisplayEditingForm()

C#VB.NET

public override void DisplayEditingForm()

Public Overrides Sub DisplayEditingForm()

DW_CalcCompPartialVolume(Phase, double, double)

Parameter	Type	Description
`phase`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override void DW_CalcCompPartialVolume(Phase phase, double T, double P)

Public Overrides Sub DW_CalcCompPartialVolume(phase As Phase, T As Double, P As Double)

DW_CalcCp_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcCp_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcCp_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

DW_CalcCv_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcCv_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcCv_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

DW_CalcdKdComposition(double[], double[], double, double, State, string): Composition (mole-number) derivative of the equilibrium K-values, d(K_i)/dn_j, with respect to the mole numbers of...

Composition (mole-number) derivative of the equilibrium K-values, d(K_i)/dn_j, with respect to the mole numbers of the phase indicated by withRespectTo (State.Liquid perturbs Vx, State.Vapor perturbs Vy), on a total-moles = 1 basis. Returns an (nc x nc) matrix. Base implementation is a finite difference; EOS/activity packages override it using the analytical d(ln phi)/dn (or d(ln gamma)/dx) building blocks.

Parameter	Type	Description
`Vx`	`Double[]`
`Vy`	`Double[]`
`T`	`Double`
`P`	`Double`
`withRespectTo`	`State`
`type`	`String`

C#VB.NET

public override double[,] DW_CalcdKdComposition(double[] Vx, double[] Vy, double T, double P, State withRespectTo, string type = "LV")

Public Overrides Function DW_CalcdKdComposition(Vx As Double(), Vy As Double(), T As Double, P As Double, withRespectTo As State, type As String = "LV") As Double(,)

DW_CalcdKdT(double[], double[], double, double, string)

Parameter	Type	Description
`Vx`	`Double[]`
`Vy`	`Double[]`
`T`	`Double`
`P`	`Double`
`type`	`String`

C#VB.NET

public override double[] DW_CalcdKdT(double[] Vx, double[] Vy, double T, double P, string type = "LV")

Public Overrides Function DW_CalcdKdT(Vx As Double(), Vy As Double(), T As Double, P As Double, type As String = "LV") As Double()

DW_CalcdLnFugCoeffdn(double[], double, double, State): Composition (mole-number) derivative of the natural logarithm of the fugacity coefficients, d(ln phi_i)/dn_j, for...

Composition (mole-number) derivative of the natural logarithm of the fugacity coefficients, d(ln phi_i)/dn_j, for the given phase, evaluated on a total-moles = 1 basis. Returns an (nc x nc) matrix. Base implementation is a finite difference in mole numbers; EOS/activity packages override this with the closed-form partial-molar expression.

Parameter	Type	Description
`Vx`	`Double[]`
`T`	`Double`
`P`	`Double`
`st`	`State`

C#VB.NET

public override double[,] DW_CalcdLnFugCoeffdn(double[] Vx, double T, double P, State st)

Public Overrides Function DW_CalcdLnFugCoeffdn(Vx As Double(), T As Double, P As Double, st As State) As Double(,)

DW_CalcdLnFugCoeffdT(double[], double, double, State): Temperature derivative of the natural logarithm of the fugacity coefficients, d(ln phi_i)/dT, for the given phase.

Temperature derivative of the natural logarithm of the fugacity coefficients, d(ln phi_i)/dT, for the given phase. Base implementation is a forward finite difference; EOS/activity packages override this with a closed-form expression. Distinct from DW_CalcdFugCoeffdT, which returns d(phi)/dT (not the logarithm).

Parameter	Type	Description
`Vx`	`Double[]`
`T`	`Double`
`P`	`Double`
`st`	`State`

C#VB.NET

public override double[] DW_CalcdLnFugCoeffdT(double[] Vx, double T, double P, State st)

Public Overrides Function DW_CalcdLnFugCoeffdT(Vx As Double(), T As Double, P As Double, st As State) As Double()

DW_CalcEnergyFlowMistura_ISOL(double, double)

Parameter	Type	Description
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcEnergyFlowMistura_ISOL(double T, double P)

Public Overrides Function DW_CalcEnergyFlowMistura_ISOL(T As Double, P As Double) As Double

DW_CalcEnthalpy(Array, double, double, State): Calculates the enthalpy of a mixture.

Calculates the enthalpy of a mixture.

Parameter	Type	Description
`Vx`	`Array`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature (K)
`P`	`Double`	Pressure (Pa)
`st`	`State`	State enum indicating the state of the mixture (liquid or vapor).

C#VB.NET

public override double DW_CalcEnthalpy(Array Vx, double T, double P, State st)

Public Overrides Function DW_CalcEnthalpy(Vx As Array, T As Double, P As Double, st As State) As Double

DW_CalcEnthalpyDeparture(Array, double, double, State): Calculates the enthalpy departure of a mixture.

Calculates the enthalpy departure of a mixture.

Parameter	Type	Description
`Vx`	`Array`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature (K)
`P`	`Double`	Pressure (Pa)
`st`	`State`	State enum indicating the state of the mixture (liquid or vapor).

C#VB.NET

public override double DW_CalcEnthalpyDeparture(Array Vx, double T, double P, State st)

Public Overrides Function DW_CalcEnthalpyDeparture(Vx As Array, T As Double, P As Double, st As State) As Double

DW_CalcEntropy(Array, double, double, State): Calculates the entropy of a mixture.

Calculates the entropy of a mixture.

Parameter	Type	Description
`Vx`	`Array`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature (K)
`P`	`Double`	Pressure (Pa)
`st`	`State`	State enum indicating the state of the mixture (liquid or vapor).

C#VB.NET

public override double DW_CalcEntropy(Array Vx, double T, double P, State st)

Public Overrides Function DW_CalcEntropy(Vx As Array, T As Double, P As Double, st As State) As Double

DW_CalcEntropyDeparture(Array, double, double, State): Calculates the entropy departure of a mixture.

Calculates the entropy departure of a mixture.

Parameter	Type	Description
`Vx`	`Array`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature (K)
`P`	`Double`	Pressure (Pa)
`st`	`State`	State enum indicating the state of the mixture (liquid or vapor).

C#VB.NET

public override double DW_CalcEntropyDeparture(Array Vx, double T, double P, State st)

Public Overrides Function DW_CalcEntropyDeparture(Vx As Array, T As Double, P As Double, st As State) As Double

DW_CalcFugCoeff(Array, double, double, State): Calculates fugacity coefficients for the specified composition at the specified conditions.

Calculates fugacity coefficients for the specified composition at the specified conditions.

Parameter	Type	Description
`Vx`	`Array`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature in K
`P`	`Double`	Pressure in Pa
`st`	`State`	Mixture state (Liquid or Vapor)

C#VB.NET

public override double[] DW_CalcFugCoeff(Array Vx, double T, double P, State st)

Public Overrides Function DW_CalcFugCoeff(Vx As Array, T As Double, P As Double, st As State) As Double()

DW_CalcFugCoeff(double[], double, double): Calculates fugacity coefficients for the specified composition at the specified conditions.

Calculates fugacity coefficients for the specified composition at the specified conditions.

Parameter	Type	Description
`Vz`	`Double[]`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature in K
`V`	`Double`	Volume in m3/mol

C#VB.NET

public override double[] DW_CalcFugCoeff(double[] Vz, double T, double V)

Public Overrides Function DW_CalcFugCoeff(Vz As Double(), T As Double, V As Double) As Double()

DW_CalcK_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcK_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcK_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

DW_CalcMassaEspecifica_ISOL(Phase, double, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`
`pvp`	`Double`

C#VB.NET

public override double DW_CalcMassaEspecifica_ISOL(Phase Phase1, double T, double P, double pvp = 0)

Public Overrides Function DW_CalcMassaEspecifica_ISOL(Phase1 As Phase, T As Double, P As Double, pvp As Double = 0) As Double

DW_CalcMM_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcMM_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcMM_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

DW_CalcOverallProps()

C#VB.NET

public override void DW_CalcOverallProps()

Public Overrides Sub DW_CalcOverallProps()

DW_CalcP(double[], double, double): Calculates system pressure for the specified temperature, volume and composition.

Calculates system pressure for the specified temperature, volume and composition.

Parameter	Type	Description
`Vz`	`Double[]`	Vector of doubles containing the molar composition of the mixture.
`T`	`Double`	Temperature in K
`V`	`Double`	Volume in m3/mol

C#VB.NET

public override double DW_CalcP(double[] Vz, double T, double V)

Public Overrides Function DW_CalcP(Vz As Double(), T As Double, V As Double) As Double

DW_CalcPhaseProps(Phase)

Parameter	Type	Description
`Phase`	`Phase`

C#VB.NET

public override void DW_CalcPhaseProps(Phase Phase)

Public Overrides Sub DW_CalcPhaseProps(Phase As Phase)

DW_CalcProp(string, Phase): Provides a wrapper function for CAPE-OPEN CalcProp/CalcSingleProp functions.

Provides a wrapper function for CAPE-OPEN CalcProp/CalcSingleProp functions.

Parameter	Type	Description
`property`	`String`	The property to be calculated.
`phase`	`Phase`	The phase where the property must be calculated for.

C#VB.NET

public override void DW_CalcProp(string property, Phase phase)

Public Overrides Sub DW_CalcProp([property] As String, phase As Phase)

DW_CalcPVAP_ISOL(double)

Parameter	Type	Description
`T`	`Double`

C#VB.NET

public override double DW_CalcPVAP_ISOL(double T)

Public Overrides Function DW_CalcPVAP_ISOL(T As Double) As Double

DW_CalcTensaoSuperficial_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcTensaoSuperficial_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcTensaoSuperficial_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

DW_CalcViscosidadeDinamica_ISOL(Phase, double, double)

Parameter	Type	Description
`Phase1`	`Phase`
`T`	`Double`
`P`	`Double`

C#VB.NET

public override double DW_CalcViscosidadeDinamica_ISOL(Phase Phase1, double T, double P)

Public Overrides Function DW_CalcViscosidadeDinamica_ISOL(Phase1 As Phase, T As Double, P As Double) As Double

GetModel()

C#VB.NET

public override object GetModel()

Public Overrides Function GetModel() As Object

RET_KIJ(string, string)

Parameter	Type	Description
`id1`	`String`
`id2`	`String`

C#VB.NET

public double RET_KIJ(string id1, string id2)

Public Function RET_KIJ(id1 As String, id2 As String) As Double

RET_VC()

C#VB.NET

public double[] RET_VC()

Public Function RET_VC() As Double()

RET_VKij()

C#VB.NET

public override double[,] RET_VKij()

Public Overrides Function RET_VKij() As Double(,)

RET_VS()

C#VB.NET

public double[] RET_VS()

Public Function RET_VS() As Double()

ReturnCriticalPoints()

C#VB.NET

public ArrayList ReturnCriticalPoints()

Public Function ReturnCriticalPoints() As ArrayList

RunPostMaterialStreamSetRoutine()

C#VB.NET

public override void RunPostMaterialStreamSetRoutine()

Public Overrides Sub RunPostMaterialStreamSetRoutine()

SupportsComponent(ICompoundConstantProperties)

Parameter	Type	Description
`comp`	`ICompoundConstantProperties`

C#VB.NET

public override bool SupportsComponent(ICompoundConstantProperties comp)

Public Overrides Function SupportsComponent(comp As ICompoundConstantProperties) As Boolean

Fields¶

ClassId

C#VB.NET

public const string ClassId = "2A322AB7-2256-495d-86C7-797AD19FDE22"

Public Const ClassId As String = "2A322AB7-2256-495d-86C7-797AD19FDE22"

m_pr

C#VB.NET

public PengRobinson m_pr

Public m_pr As PengRobinson

prn

C#VB.NET

public PR prn

Public prn As PR