Download - L7 Phase Equilibria

  • Termodinamica de HidrocarburosGeneralized Phase Equilibria

  • Phase EquilibriumEvolution

  • The Concept of EquilibriumEquilibrium indicates static conditions, the absence of change In thermodynamics is taken to mean not only the absence of change, but the absence of any tendency to change. A system existing in equilibrium is one in which under such conditions that there is no tendency for a change to state to occur.

  • The Concept of EquilibriumTendencies toward a change are caused by a driving force of any kind

    Equilibrium means the absence of any driving force, or that all forces are in exact balance.

  • Driving Forces Typical driving forces include:

    mechanical forces such as pressure on a piston tend to cause energy transfer as work temperature differences tend to cause the flow of heat chemical potentials tend to cause mass transfer from one phase to another or cause substances to react chemically.

  • Phase Equilibrium and the Phase RuleIn reservoir engineering applications we assume that reservoir fluids are at equilibrium, we do not say how long the equilibrium will last. As a reservoir block changes pressure due to production (injection) we assume that equilibrium is reached instantly. Fluid properties in reservoir cells are evaluated using a sequence of connected equilibrium stages.

  • Phase RuleIt tells us the number of independent variables required to fully characterize a systemIt does not tell us which variables to select

  • Generalization of the phase rule for Nc non reacting components

  • Phase Equilibrium and the Phase RuleThus for non-reacting systems

    F = # of variables # of Independent equations relating these variables

  • First Law and Fundamental Thermodynamic Relationships Closed Systems The system does not exchange matter with the surroundings, but it can exchange energy. The first law is a generalization of the conservation of energy

  • Compression and expansion work in a gas container indicating the convention used for heat and work

    Heat and Work Sign Convention

  • First Law and Fundamental Thermodynamic RelationshipsFor a reversible process, dQ = TdSt thus,

    If the work of expansion or compression is the only kind of work allowed then:

  • First Law and Fundamental Thermodynamic RelationshipsReplacing work and heat expressions


  • First Law and Fundamental Thermodynamic RelationshipsSince

    Thus one can identify,

    Define: Mt = nM with M = U, H, A, G, S

  • Other Thermodynamic FunctionsThe relationship among these properties is:

    Flow processesPhase equilibria

  • Differentials of Thermodynamic FunctionsExpressions similar to

    The same relationships hold for the intensive properties (M = Mt /n)

  • Key ConceptThe (Ut ,Ht ,Ft ,Gt ,St ) are STATE properties which means independent of path.

  • State FunctionsPressureTemperature

  • Open Systems For an open system, Ut, Ht, Ft, and Gt, will also depend on the concentration of each of the components. The number of moles of each specie may change due to:

    Chemical reaction within systemInterchange of matter with surroundingsInterchange and chemical reaction.

  • Open SystemsThe functional form of Ut, Ht, Ft, and G t for open systems are,

  • Open SystemsThe differential form of the thermodynamic functions are

  • Open SystemsThe differential form of the above equations are,

  • Open SystemsDefine the chemical potential of component " i " as

    Most well-known

  • Second Law and the Equilibrium Criteria

  • Second Law and the Equilibrium CriteriaThe criteria of equilibrium of a system can also be stated in terms of Ut, Ht, Ft, and Gt as follows

    The internal energy, Ut, must be a minimum at constant St, Vt, and ni.The enthalpy, Ht, must be a minimum at constant St, P, and ni.The Helmholtz free energy, Ft, must be a minimum at constant T, Vt, and ni.The Gibbs free energy, Gt, must be a minimum at constant T, P, and ni.

  • Chemical and Phase Equilibria Criteria for an Open System Using Intensive Properties

    Gas SystemLiquid systemopen

  • Open System: Derivation of Equilibrium ConditionsVariation of internal energy for liquid system is

    Variation of internal energy for gas system is

  • Derivation of Equilibrium ConditionsGas + Liquid systems make a closed system and the total energy is

    thus for a closed system at equilibrium

  • Derivation of Equilibrium ConditionsFrom mass conservation

    replace in


  • Auxiliary Thermodynamic Functions The mole fractions are also thermodynamic functions

  • Phase Equilibria ModelsCan be classified according to:

    the type of fluids (hydrocarbons, alcohols, electrolytes, water and other non-hydrocarbon species)

    pressure and temperature ranges of interest.

  • Phase Equilibria Models for Low-pressure ranges, such as those of separator and surface conditions High-pressures ranges which apply to the reservoir. Type of reservoir fluid, whether a black oil or a volatile oil, also determines the type of Phase equilibrium model

  • Residual PropertiesDefine the residual properties for mathematical convenience as the difference between the actual (real) property minus the same property, evaluated at the same pressure, temperature, and composition, but evaluated using the ideal gas equation.

  • VLE

    We will start with the simpler models first, the ones for lower pressures Single Component & Multicomponent

  • Residual PropertiesThat is

    MR = M-MigM=U, H, G, S, F (F is A in American Notation)

    M:Real Property @ (T, P) of the system MR: Residual PropertyMig: Property @ (T, P) of the system evaluated as if the fluid were an ideal gas Note: there is no TR or PR

  • Residual PropertiesRecall for a constant composition closed system

  • Residual PropertiesNote that the properties used in these equations are intensive properties, that is the volume is the molar volume G and S are expressed in BTU/lb-mol and BTU/lb-mol-R, respectively, (or in cal/g-mol, cal/g-mol K in the SI system of units).

  • Gibbs Residual EnergyAt constant temperature,

    Divide by RT

  • Gibbs Residual EnergyFrom previous lectures we had:


  • Phase Equilibrium of a Single ComponentRecall

  • Predicted Isotherms from a cubic EOS

  • Phase Equilibrium Single ComponentFor constant temperature,

    At equilibrium P1=P5=Ps

  • Phase Equilibrium of a Single ComponentBy inspection,

    And also,

  • Maxwell Equal Area Rule

  • VLE in Dimensionless or Reduced FormWrite the EOS in dimensionless form using Tr=T/Tc, Pr=P/Pc, Vr=V/Vc, and the values for a and b found from the critical constraints

  • VLE in Dimensionless or Reduced FormFor Van der Waals EOS


  • VLE in Dimensionless or Reduced Formand

  • Application of Equal Area Rule

    At T constant


  • VLE in Dimensionless or Reduced FormReplacing and integrating

    Since P is constant,


  • VLE in Dimensionless or Reduced Form

  • VLE in Dimensionless or Reduced FormFrom integral tables,


  • VLE in Dimensionless or Reduced FormHave three equations to work with


    Maxwell Equal Area Rule


    unknowns Prs, Vrl, Vrg.

  • VLE at low pressuresWe will see first models that apply ONLY for low pressures

  • Systems of Variable Composition: Ideal BehaviorApplications to low pressuresSimplifications

    the gas phase behaves as an Ideal Gas the liquid phase exhibits Ideal Solution Behavior.

  • Systems of Variable Composition: Ideal Behavior

    The equilibrium criteria between 2 phases a and b is,

  • Systems of Variable Composition: Ideal BehaviorThus, at constant T and P,

  • Systems of Variable Composition: Ideal Behavior

    Simplest VLE model (IG+IS) imply that

    IG: molecular interactions are zero, molecules have no volume.

    IS: forces of attraction/repulsion between molecules are the same regardless of molecular species. Volumes are additive (Amagats Law).

  • Forces between molecular species

    A AB BA B

  • Ideal Gas MixtureThe pressure in a vessel containing an ideal gas mixture (n) or a single gas component (nk) is

  • Systems of Variable Composition: Ideal Behavior

    Pk is the partial pressure of component k, and by definition

  • Systems of Variable Composition: Ideal BehaviorGeneralize this principle to any thermodynamic property for an ideal gas mixture

  • A total thermodynamic property (nU, nG, nS, nH, nF) of an ideal gas mixture is the S of the total properties of the individual species each evaluated at the T of the mixture and at its own partial pressure.

  • Derive Equilibrium Relations Begin with an ideal gas

    The enthalpy of an ideal gas is independent of pressure, thus

  • Derive Equilibrium Relations

    For the entropy, we must express

  • Derive Equilibrium RelationsRecall Maxwell Rules

    For ideal gas,

  • Derive Equilibrium Relationsat constant temperature,

  • Derive Equilibrium RelationsWe also know from ideal averaging applied to entropy,

  • Derive Equilibrium RelationsSubstituting,

    the entropy change of mixing the ideal gases is not zero

  • Derive Equilibrium RelationsNow, we can build the expression for the Gibbs energy for an ideal gas.


  • Derive Equilibrium RelationsExpressed in terms of n (yk=nk/n),

  • Derive Equilibrium RelationsRecall,

  • Derive Equilibrium RelationsTherefore,

  • Ideal SolutionFollowing the same reasoning as for gases, we have that,

    Here, Si and Gi are the properties of the pure species in the liquid state at the T and P of the mixture.

  • Raoults LawIt is a combination of IG + IS models. VLE for a mixture of Nc components

  • Raoults LawThus, at T and P,

    The right hand side of this Eq. indicates pure species properties evaluated at the equilibrium T and P of the mixture

  • Raoults Law

    As we seen before for a pure component,

    So, this leads to Raoults Law!

  • Equilibrium RatioVapor-Liquid Equilibrium ratio is defined as

    There are several correlations and models for KiFrom Raults law (ideal model )


  • Equilibrium RatioREAD papers placed in module 3 folder for other composition-independent k-value models (we will have exercises using them)Compositional dependence in considered when using EOS but K-values become implicit

  • Bubble Point Evaluation Under Raoults law, the bubble point has a linear dependence with the vapor pressures of the pure components.

    Once the bubble point pressure is found, the equilibrium vapor compositions are found from Raoults law.

  • Deviations from Raoult's lawThe dew point curve (lower black curve) in is always curved regardless whether the mixture is ideal or not. The red curves in indicate deviations from Raoult's law. When the bubble point curve is above the straight line, we will have positive deviations from Raoult's Law. When the bubble point curve is below the straight line, we will have negative deviations from Raoult's Law. This happens for non-ideal mixtures and may lead to azeotropy.










  • Dew Point CalculationAt the dew point the overall fluid composition coincides with the gas composition. That is.

  • Statement of EquilibriumPT123IG/IS Raoults law

  • Bubble Point Evaluation The bubble point pressure at a given T is

  • Dew Point CalculationFind DP pressure and equilibrium liquid compositions

  • Types of Phase Equilibria Calculations

  • Bubble Point Temperature given P We must follow an iterative procedure.

    Bubble point temperature enters into the equation non-linearly

  • Bubble Point Temperature Find TB pressure and equilibrium gas compositions

  • Bubble Point TemperatureThe problem is that we do not know yet at what temperature to evaluate the pure component vapor pressures. See the following diagram

  • Bubble Point TemperatureFor well-behaved systems (no azeotropes), the searched temperature will be bounded by the highest and lowest saturation temperature of the components in the mixture at the selected system pressure.

  • Bubble Point Temperature











  • Bubble Point Temperature Procedure1. Evaluate and at the given pressure P, which is a saturation pressure.

    2. Choose your first guess bubble point temperature as

  • Bubble Point Temperature Procedure3. Define a relative volatility using a reference substance such that all relative volatilities are either > 0 or < 0 (i.e. monotonically increasing or decreasing).

    with the saturation pressures evaluated at the guess temperature evaluated in (2)

  • Bubble Point Temperature Procedure4. Expand the volatility as

    with T from step 2.

  • Bubble Point Temperature Procedure5. Write the bubble point equation in terms of volatilities and a reference vapor pressure (lowest or highest)For a binary, you would have only one volatility

    Guessed vapor pressure

  • Bubble Point Temperature ProcedureThus

    this is your first guess saturation pressure for the reference component (here 2) at the first guess temperature evaluated in step 1. From this saturation pressure use the Antoine equation to find an updated bubble point temperature (step 1).

  • Bubble Point Temperature Procedure

    From the saturation pressure evaluated in use the Antoine equation to find a new temperature

  • Bubble Point Temperature ProcedureThis new T new new iterate until two successive temperatures do not change by a specified tolerance.

    The Excel file provided in our WEB site illustrates this procedure for a ternary mixture. You can modify it and extend it to multicomponents.

  • Dew Point Temperature ProcedureYou can follow a very similar reasoning as the one developed for the bubble point and devise the algorithm required to solve this problem using relative volatilities

  • Flash CalculationsIn this type of calculations, the work-horse of reservoir simulation packages, the objective is to:

    find fraction of vapor vaporized and equilibrium gas and liquid compositions given the overall mixture composition, P and T.

  • Flash CalculationsStart with the equilibrium equation

    Material balance

  • Flash CalculationsNow replace either liquid or gas compositions using equilibrium equation

    Here replaced xi

  • Flash CalculationsRearrange and sum over all compositions

  • Separation process

  • Flash CalculationsObjective function (flash function) is

  • Flash CalculationsThere are several equivalent expressions for the flash function




    (c) is the best well behaved for numerical solution (Rachford- Rice function)

  • Flash CalculationsOnce fv is found the equilibrium gas and liquid compositions are evaluated from


  • VLE Examples

  • But .Raoults model will NOT work well in these casesthen what ?

  • Equations of State(EOS)