bubble_pressure(model::EoSModel, T, x, method = ChemPotBubblePressure())

Calculates the bubble pressure and properties at a given temperature. Returns a tuple, containing:

• Bubble Pressure [Pa]
• liquid volume at Bubble Point [m³]
• vapour volume at Bubble Point [m³]
• Gas composition at Bubble Point

By default, uses equality of chemical potentials, via ChemPotBubblePressure

bubble_temperature(model::EoSModel, p, x,method::BubblePointMethod = ChemPotBubbleTemperature())

Calculates the bubble temperature and properties at a given pressure. Returns a tuple, containing:

• Bubble Temperature [K]
• liquid volume at Bubble Point [m³]
• vapour volume at Bubble Point [m³]
• Gas composition at Bubble Point

By default, uses equality of chemical potentials, via ChemPotBubbleTemperature

dew_pressure(model::EoSModel, T, y,method = ChemPotDewPressure())

Calculates the dew pressure and properties at a given temperature. Returns a tuple, containing:

• Dew Pressure [Pa]
• liquid volume at Dew Point [m³]
• vapour volume at Dew Point [m³]
• Liquid composition at Dew Point

By default, uses equality of chemical potentials, via ChemPotDewPressure

dew_temperature(model::EoSModel, p, y, method = ChemPotDewTemperature())

calculates the dew temperature and properties at a given pressure. Returns a tuple, containing:

• Dew Temperature [K]
• liquid volume at Dew Point [m³]
• vapour volume at Dew Point [m³]
• Liquid composition at Dew Point

By default, uses equality of chemical potentials, via ChemPotDewTemperature

azeotrope_pressure(model::EoSModel, T; v0 = x0_azeotrope_pressure(model,T))

calculates the azeotrope pressure and properties at a given temperature. Returns a tuple, containing:

• Azeotrope Pressure [Pa]
• liquid volume at Azeotrope Point [m³]
• vapour volume at Azeotrope Point [m³]
• Azeotrope composition

azeotrope_temperature(model::EoSModel, T; v0 = x0_bubble_pressure(model,T,[0.5,0.5]))

Calculates the azeotrope temperature and properties at a given pressure. Returns a tuple, containing:

• Azeotrope Temperature [K]
• liquid volume at Azeotrope Point [m³]
• vapour volume at Azeotrope Point [m³]
• Azeotrope composition

LLE_pressure(model::EoSModel, T, x; v0 = x0_LLE_pressure(model,T,x))

calculates the Liquid-Liquid equilibrium pressure and properties at a given temperature.

Returns a tuple, containing:

• LLE Pressure [Pa]
• liquid volume of composition x₁ = x at LLE Point [m³]
• liquid volume of composition x₂ at LLE Point [m³]
• Liquid composition x₂

LLE_temperature(model::EoSModel, p, x; T0 = x0_LLE_temperature(model,p,x))

calculates the Liquid-Liquid equilibrium temperature and properties at a given pressure.

Returns a tuple, containing:

• LLE Pressure [Pa]
• liquid volume of composition x₁ = x at LLE Point [m³]
• liquid volume of composition x₂ at LLE Point [m³]
• Liquid composition x₂

VLLE_pressure(model::EoSModel, T; v0 = x0_LLE_pressure(model,T))

calculates the Vapor-Liquid-Liquid equilibrium pressure and properties of a binary mixture at a given temperature.

Returns a tuple, containing:

• VLLE Pressure [Pa]
• Liquid volume of composition x₁ at VLLE Point [m³]
• Liquid volume of composition x₂ at VLLE Point [m³]
• Vapour volume of composition y at VLLE Point [m³]
• Liquid composition x₁
• Liquid composition x₂
• Liquid composition y

VLLE_temperature(model::EoSModel, p; T0 = x0_LLE_temperature(model,p))

calculates the Vapor-Liquid-Liquid equilibrium temperature and properties of a binary mixture at a given temperature.

Returns a tuple, containing:

• VLLE temperature [K]
• Liquid volume of composition x₁ at VLLE Point [m³]
• Liquid volume of composition x₂ at VLLE Point [m³]
• Vapour volume of composition y at VLLE Point [m³]
• Liquid composition x₁
• Liquid composition x₂
• Liquid composition y

crit_mix(model::EoSModel,z;v0=x=x0_crit_mix(model,z))

Returns the critical mixture point at a ginven composition.

Returns a tuple, containing:

• Critical Mixture Temperature [K]
• Critical Mixture Pressure [Pa]
• Critical Mixture Volume [m³]

UCEP_mix(model::EoSModel;v0=x0_UCEP_mix(model))

Calculates the Upper Critical End Point of a binary mixture.

returns:

• UCEP Temperature [K]
• UCEP Pressure [Pa]
• liquid volume at UCEP Point [m³]
• vapour volume at UCEP Point [m³]
• liquid molar composition at UCEP Point
• vapour molar composition at UCEP Point

UCST_mix(model::EoSModel,T;v0=x0_UCST_mix(model,T))

Calculates the Upper critical solution point of a mixture at a given Temperature.

returns:

• UCST Pressure [Pa]
• volume at UCST Point [m³]
• molar composition at UCST Point

gibbs_solvation(model::EoSModel, T; threaded=true, vol0=(nothing,nothing))

Calculates the solvation free energy as:

g_solv = -R̄*T*log(K)

where the first component is the solvent and second is the solute.

cross_second_virial(model,T,z)

Default units: [m^3]

Calculates the second cross virial coefficient (B₁₂) of a binary mixture, using the definition:

B̄ = x₁^2*B₁₁ + 2x₁x₂B₁₂ + x₂^2*B₂₂
B₁₂ = (B̄ - x₁^2*B₁₁ - x₂^2*B₂₂)/2x₁x₂

!!! info composition-dependent The second cross virial coefficient calculated from a equation of state can present a dependency on composition [1], but normally, experiments for obtaining the second virial coefficient are made by mixing the same volume of two gases. you can calculate B12 in this way by using (Clapeyron.equivolcrosssecond_virial)[@ref]

References

1. Jäger, A., Breitkopf, C., & Richter, M. (2021). The representation of cross second virial coefficients by multifluid mixture models and other equations of state. Industrial & Engineering Chemistry Research, 60(25), 9286–9295. doi:10.1021/acs.iecr.1c01186

equivol_cross_second_virial(model::EoSModel,T,p_exp = 200000.0)

calculates the second cross virial coefficient, by simulating the mixing of equal volumes of pure gas, at T,P conditions. The equal volume of each pure gas sets an specific molar amount for each component. Details of the experiment can be found at [1].

Example

model = SAFTVRQMie(["helium","neon"])
B12 = equivol_cross_second_virial(model,)

References

1. Brewer, J., & Vaughn, G. W. (1969). Measurement and correlation of some interaction second virial coefficients from − 125° to 50°C. I. The Journal of Chemical Physics, 50(7), 2960–2968. doi:10.1063/1.1671491

sle_solubility(model::CompositeModel, p, T, z; solute)

Calculates the solubility of each component within a solution of the other components, at a given temperature and composition. Returns a matrix containing the composition of the SLE phase boundary for each component. If solute is specified, returns only the solubility of the specified component.

Can only function when solid and fluid models are specified within a CompositeModel.

sle_solubility(model::CompositeModel, p, T, z; solute)

Calculates the solubility of each component within a solution of the other components, at a given temperature and composition. Returns a matrix containing the composition of the SLE phase boundary for each component. If solute is specified, returns only the solubility of the specified component.

Can only function when solid and fluid models are specified within a CompositeModel.

slle_solubility(model::CompositeModel, p, T)

Calculates the phase boundary for solid-liquid-liquid equilibriumm of a ternary mixture, at a given temperature and pressure. Returns a matrix containing the composition of the two liquids phases.

Can only function when solid and liquid models are specified within a CompositeModel and when the third component is the solute.

eutectic_point(model::CompositeModel, p)

Calculates the eutectic point of a binary mixture (at a given pressure). Returns a tuple containing the eutectic temperature and the composition at the eutectic point.

Can only function when solid and liquid models are specified within a CompositeModel.

ChemPotBubblePressure(kwargs...)

Function to compute bubble_pressure via chemical potentials. It directly solves the equality of chemical potentials system of equations.

Inputs:

• y0 = nothing: optional, initial guess for the vapor phase composition
• p0 = nothing: optional, initial guess for the bubble pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• max_iters = 10000: optional, maximum number of iterations
• nonvolatiles = nothing: optional, Vector of strings containing non volatile compounds. those will be set to zero on the vapour phase.

FugBubblePressure(kwargs...)

Function to compute bubble_pressure via fugacity coefficients. First it uses successive substitution to update the phase composition and a outer newtown loop to update the pressure. If no convergence is reached after itmax_newton iterations, the system is solved using a multidimensional non-linear system of equations.

Inputs:

• y0 = nothing: optional, initial guess for the vapor phase composition
• p0 = nothing: optional, initial guess for the bubble pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• itmax_newton = 10: optional, number of iterations to update the pressure using newton's method
• itmax_ss = 5: optional, number of iterations to update the liquid phase composition using successive substitution
• tol_x = 1e-8: optional, tolerance to stop successive substitution cycle
• tol_p = 1e-8: optional, tolerance to stop newton cycle
• tol_of = 1e-8: optional, tolerance to check if the objective function is zero.
• nonvolatiles = nothing: optional, Vector of strings containing non volatile compounds. those will be set to zero on the vapour phase.

ActivityBubblePressure(kwargs...)

Function to compute bubble_pressure using Activity Coefficients. On activity coefficient models it solves the problem via succesive substitucion. On helmholtz-based models, it uses the Chapman approximation for activity coefficients.

Inputs:

• gas_fug = true: if the solver uses gas fugacity coefficients. on ActivityModel is set by default to false
• poynting = true: if the solver use the poynting correction on the liquid fugacity coefficients. on ActivityModel is set by default to false
• y0 = nothing: optional, initial guess for the vapor phase composition
• p0 = nothing: optional, initial guess for the bubble pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• itmax_ss = 40: optional, maximum number of sucesive substitution iterations

ChemPotBubbleTemperature(kwargs...)

Function to compute bubble_temperature via chemical potentials. It directly solves the equality of chemical potentials system of equations.

Inputs:

• y = nothing: optional, initial guess for the vapor phase composition.
• T0 = nothing: optional, initial guess for the bubble temperature [K].
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• max_iters = 10000: optional, maximum number of iterations
• nonvolatiles = nothing: optional, Vector of strings containing non volatile compounds. those will be set to zero on the vapour phase.

FugBubbleTemperature(kwargs...)

Method to compute bubble_temperature via fugacity coefficients. First it uses successive substitution to update the phase composition and a outer newtown loop to update the temperature. If no convergence is reached after itmax_newton iterations, the system is solved using a multidimensional non-linear system of equations.

Inputs:

• y = nothing: optional, initial guess for the vapor phase composition.
• T0 = nothing: optional, initial guess for the bubble temperature [K].
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• itmax_newton = 10: optional, number of iterations to update the temperature using newton's method
• itmax_ss = 5: optional, number of iterations to update the liquid phase composition using successive substitution
• tol_x = 1e-8: optional, tolerance to stop successive substitution cycle
• tol_T = 1e-8: optional, tolerance to stop newton cycle
• tol_of = 1e-8: optional, tolerance to check if the objective function is zero.
• nonvolatiles: optional, Vector of strings containing non volatile compounds. those will be set to zero on the vapour phase.

ActivityBubbleTemperature(kwargs...)

Function to compute bubble_temperature using Activity Coefficients. On activity coefficient models it solves the problem via succesive substitucion. On helmholtz-based models, it uses the Chapman approximation for activity coefficients.

Inputs:

• gas_fug = true: if the solver uses gas fugacity coefficients. on ActivityModel is set by default to false
• poynting = true: if the solver use the poynting correction on the liquid fugacity coefficients. on ActivityModel is set by default to false
• y0 = nothing: optional, initial guess for the vapor phase composition
• T0 = nothing: optional, initial guess for the bubble temperature [K]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• itmax_ss = 40: optional, maximum number of sucesive substitution iterations

ChemPotDewPressure(kwargs...)

Function to compute dew_pressure via chemical potentials. It directly solves the equality of chemical potentials system of equations.

Inputs:

• x0 = nothing: optional, initial guess for the liquid phase composition
• p0 = nothing: optional, initial guess for the dew pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• max_iters = 10000: optional, maximum number of iterations
• noncondensables = nothing: optional, Vector of strings containing non condensable compounds. those will be set to zero on the liquid phase.

FugDewPressure(kwargs...)

Method to compute dew_pressure via fugacity coefficients. First it uses successive substitution to update the phase composition and a outer newtown loop to update the pressure. If no convergence is reached after itmax_newton iterations, the system is solved using a multidimensional non-linear system of equations.

Inputs:

• x0 = nothing: optional, initial guess for the liquid phase composition
• p0 = nothing: optional, initial guess for the dew pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• itmax_newton = 10: optional, number of iterations to update the pressure using newton's method
• itmax_ss = 5: optional, number of iterations to update the liquid phase composition using successive substitution
• tol_x = 1e-8: optional, tolerance to stop successive substitution cycle
• tol_p = 1e-8: optional, tolerance to stop newton cycle
• tol_of = 1e-8: optional, tolerance to check if the objective function is zero.
• noncondensables = nothing: optional, Vector of strings containing non condensable compounds. those will be set to zero on the liquid phase.

ActivityDewPressure(kwargs...)

Function to compute dew_pressure using Activity Coefficients. On activity coefficient models it solves the problem via succesive substitucion. On helmholtz-based models, it uses the Chapman approximation for activity coefficients.

Inputs:

• gas_fug = true: if the solver uses gas fugacity coefficients. on ActivityModel is set by default to false
• poynting = true: if the solver use the poynting correction on the liquid fugacity coefficients. on ActivityModel is set by default to false
• x0 = nothing: optional, initial guess for the liquid phase composition
• p0 = nothing: optional, initial guess for the dew pressure [Pa]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• itmax_ss = 40: optional, maximum number of sucesive substitution iterations

ChemPotDewTemperature(kwargs...)

Function to compute dew_temperature via chemical potentials. It directly solves the equality of chemical potentials system of equations.

Inputs:

• x0 = nothing: optional, initial guess for the liquid phase composition
• T0 =nothing: optional, initial guess for the dew temperature [K]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• max_iters = 10000: optional, maximum number of iterations
• noncondensables = nothing: optional, Vector of strings containing non condensable compounds. those will be set to zero on the liquid phase.

FugDewTemperature(kwargs...)

Method to compute dew_temperature via fugacity coefficients. First it uses successive substitution to update the phase composition and a outer newtown loop to update the temperature. If no convergence is reached after itmax_newton iterations, the system is solved using a multidimensional non-linear system of equations.

Inputs:

• x0 = nothing: optional, initial guess for the liquid phase composition
• T0 = nothing: optional, initial guess for the dew temperature [K]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• itmax_newton = 10: optional, number of iterations to update the temperature using newton's method
• itmax_ss = 5: optional, number of iterations to update the liquid phase composition using successive substitution
• tol_x = 1e-8: optional, tolerance to stop successive substitution cycle
• tol_T = 1e-8: optional, tolerance to stop newton cycle
• tol_of = 1e-8: optional, tolerance to check if the objective function is zero.
• noncondensables = nothing: optional, Vector of strings containing non condensable compounds. those will be set to zero on the liquid phase.

ActivityDewTemperature(kwargs...)

Function to compute dew_temperature using Activity Coefficients. On activity coefficient models it solves the problem via succesive substitucion. On helmholtz-based models, it uses the Chapman approximation for activity coefficients.

Inputs:

• gas_fug = true: if the solver uses gas fugacity coefficients. on ActivityModel is set by default to false
• poynting = true: if the solver use the poynting correction on the liquid fugacity coefficients. on ActivityModel is set by default to false
• x0 = nothing: optional, initial guess for the liquid phase composition
• T0 = nothing: optional, initial guess for the dew temperature [K]
• vol0 = nothing: optional, initial guesses for the liquid and vapor phase volumes
• atol = 1e-8: optional, absolute tolerance of the non linear system of equations
• rtol = 1e-12: optional, relative tolerance of the non linear system of equations
• itmax_ss = 40: optional, maximum number of sucesive substitution iterations

gibbs_duhem(model,V,T,z=[1.0])

performs a Gibbs-Duhem check on the input conditions:

∑zᵢμᵢ - G ≈ 0

Where G is the total gibbs energy. it can help diagnose if a user-defined eos is consistent.

return |∑zᵢμᵢ - G|, ∑zᵢμᵢ and G at the specified conditions.

isstable(model,V,T,z)::Bool

Performs stability tests for a (V,T,z) pair, and warn if any tests fail. returns true/false.

Checks:

• mechanical stability: isothermal compressibility is not negative.
• diffusive stability: all eigenvalues of ∂²A/∂n² are positive.
• chemical stability: there isn't any other combinations of compositions at p(V,T),T that are more stable than the input composition.

VT_mechanical_stability(model,V,T,z = SA[1.0])::Bool

Performs a mechanical stability for a (V,T,z) pair, returns true/false. Checks if isothermal compressibility is not negative.

VT_diffusive_stability(model,V,T,z)::Bool

Performs a diffusive stability for a (V,T,z) pair, returns true/false. Checks if all eigenvalues of ∂²A/∂n² are positive.

VT_chemical_stability(model,V,T,z)::Bool

Performs a chemical stability check using the tangent plane distance criterion, using the tpd function

tpd(model,p,T,z;break_first = false,lle = false,tol_trivial = 1e-5, di = nothing)

Calculates the Tangent plane distance function (tpd). It returns:

• a vector with trial phase compositions where tpd < 0
• a vector with the tpd values
• a vector with symbols indicating the phase of the input composition
• a vector with symbols indicating the phase of the trial composition

It iterates over each two-phase combination, starting from pure trial compositions, it does succesive substitution, then Gibbs optimization.

If the vectors are empty, then the procedure couldn't find a negative tpd. That is an indication that the phase is (almost) surely stable.

tp_flash(model, p, T, n, method::TPFlashMethod = DETPFlash())

Routine to solve non-reactive multicomponent flash problem. The default method uses Global Optimization. see DETPFlash

Inputs:

• T, Temperature
• p, Pressure
• n, vector of number of moles of each species

Outputs - Tuple containing:

• xᵢⱼ, Array of mole fractions of species j in phase i
• nᵢⱼ, Array of mole numbers of species j in phase i, [mol]
• G, Gibbs Free Energy of Equilibrium Mixture [J]

DETPFlash(; numphases = 2,
max_steps = 1e4*(numphases-1),
population_size =20,
time_limit = Inf,
verbose = false,
logspace = false,
equilibrium = :auto)

Method to solve non-reactive multicomponent flash problem by finding global minimum of Gibbs Free Energy via Differential Evolution.

User must assume a number of phases, numphases. If true number of phases is smaller than numphases, model should predict either (a) identical composition in two or more phases, or (b) one phase with negligible total number of moles. If true number of phases is larger than numphases, a thermodynamically unstable solution will be predicted.

The optimizer will stop at max_steps evaluations or at time_limit seconds

The equilibrium keyword allows to restrict the search of phases to just liquid-liquid equilibria (equilibrium = :lle). the default searches for liquid and gas phases.

RRTPFlash{T}(;kwargs...)

Method to solve non-reactive multicomponent flash problem by Rachford-Rice equation.

Only two phases are supported. if K0 is nothing, it will be calculated via the Wilson correlation.

Keyword Arguments:

• equilibrium = equilibrium type ":vle" for liquid vapor equilibria, ":lle" for liquid liquid equilibria
• K0 (optional), initial guess for the constants K
• x0 (optional), initial guess for the composition of phase x
• y0 = optional, initial guess for the composition of phase y
• vol0 = optional, initial guesses for phase x and phase y volumes
• K_tol = tolerance to stop the calculation
• max_iters = number of Successive Substitution iterations to perform
• nacc = accelerate successive substitution method every nacc steps. Should be a integer bigger than 3. Set to 0 for no acceleration.
• noncondensables = arrays with names (strings) of components non allowed on the liquid phase. In the case of LLE equilibria, corresponds to the x phase
• nonvolatiles = arrays with names (strings) of components non allowed on the vapour phase. In the case of LLE equilibria, corresponds to the y phase

MichelsenTPFlash{T}(;kwargs...)

Method to solve non-reactive multicomponent flash problem by Michelsen's method.

Only two phases are supported. if K0 is nothing, it will be calculated via the Wilson correlation.

Keyword Arguments:

• equilibrium = equilibrium type ":vle" for liquid vapor equilibria, ":lle" for liquid liquid equilibria
• K0 (optional), initial guess for the constants K
• x0 (optional), initial guess for the composition of phase x
• y0 = optional, initial guess for the composition of phase y
• vol0 = optional, initial guesses for phase x and phase y volumes
• K_tol = tolerance to stop the calculation
• ss_iters = number of Successive Substitution iterations to perform
• nacc = accelerate successive substitution method every nacc steps. Should be a integer bigger than 3. Set to 0 for no acceleration.
• second_order = wheter to solve the gibbs energy minimization using the analytical hessian or not
• noncondensables = arrays with names (strings) of components non allowed on the liquid phase. In the case of LLE equilibria, corresponds to the x phase
• nonvolatiles = arrays with names (strings) of components non allowed on the vapour phase. In the case of LLE equilibria, corresponds to the y phase

MultiPhaseTPFlash(;kwargs...)

Method to solve non-reactive multiphase (np phases), multicomponent (nc components) flash problem.

The flash algorithm uses successive stability tests to find new phases [1], and then tries to solve the system via rachford-rice and succesive substitution for nc * np * ss_iters iterations.

If the Rachford-Rice SS fails to converge, it proceeds to solve the system via gibbs minimization in VT-space using lnK-β-ρ as variables [3].

The algorithm finishes when SS or the gibbs minimization converges and all resulting phases are stable.

If the result of the phase equilibria is not stable, then it proceeds to add/remove phases again, for a maximum of phase_iters iterations.

Keyword Arguments:

• K0 (optional), initial guess for the constants K
• x0 (optional), initial guess for the composition of phase x
• y0 (optional), initial guess for the composition of phase y
• n0 (optional), initial guess for all compositions. it can be a matrix or a vector of vectors.
• K_tol = sqrt(eps(Float64)), tolerance to stop the calculation (norm(lnK,1) < K_tol)
• ss_iters = 4, number of Successive Substitution iterations to perform
• nacc = 3, accelerate successive substitution method every nacc steps. Should be a integer bigger than 3. Set to 0 for no acceleration.
• second_order = true, whether to solve the gibbs energy minimization using the analytical hessian or not. If set to false, the gibbs minimization will be done using L-BFGS.
• full_tpd = false, whether to start with a simple K-split or using an intensive TPD search first.
• max_phases = typemax(Int), the algorithm stops if there are more than min(max_phases,nc) phases
• phase_iters = 20, the maximum number of solve-add/remove-phase iterations

References

1. Thermopack - Thermodynamic equilibrium algorithms reimplemented in a new framework. (2020, September 08). https://github.com/thermotools/thermopack. Retrieved May 4, 2024, from https://github.com/thermotools/thermopack/blob/main/docs/memo/flash/flash.pdf
2. Okuno, R., Johns, R. T. T., & Sepehrnoori, K. (2010). A new algorithm for Rachford-Rice for multiphase compositional simulation. SPE Journal, 15(02), 313–325. doi:10.2118/117752-pa
3. Adhithya, T. B., & Venkatarathnam, G. (2021). New pressure and density based methods for isothermal-isobaric flash calculations. Fluid Phase Equilibria, 537(112980), 112980. doi:10.1016/j.fluid.2021.112980

MCFlashJL(; method = MultiComponentFlash.SSIFlash(), storage = nothing, V = NaN, K = nothing, kwargs.... )

Uses MultiComponentFlash.jl two-phase flash solver. allows passing storage to minimize allocations. That storage can be created by calling MultiComponentFlash.flash_storage(model,p,T,z,method::MCFlashJL)

numphases(method::TPFlashMethod)

Return the number of phases supported by the TP flash method. by default its set to 2. it the method allows it, you can set the number of phases by doing method(;numphases = n).

supports_reduction(method::TPFlashMethod)::Bool

Checks if a TP Flash method supports index reduction (the ability to prune model components with compositions lower than a threshold). All current Clapeyron methods support index reduction, but some methods that alllow passing a cache could have problems