Fluid phase equilibrium vapor-liquid equilibria

Galivel - Solastiuk F., S. Laugier and D. Richon, "Vapor-Liquid Equilibrium Data for the Propane-MethanoI-C02 System", Fluid Phase Equilibria, 28, 73-85 (1986). 

Hong, J.H. and Kobayashi, R., "vapor-Liquid Equilibrium Studies for the carbon Dioxide-Methanol System", Fluid Phase Equilibria. 41,269-276 (1988). 

Schwartzentruber J., F. Galivel-Solastiuk and H. Renon, "Representation of the Vapor-Liquid Equilibrium of the Ternary System Carbon Dioxide-Propane-Methanol and its Binaries with a Cubic Equation of State. A new Mixing Rule", Fluid Phase Equilibria, 38,217-226 (1987). 

As pointed out in the previous chapter, the separation of a homogeneous fluid mixture requires the creation of another phase or the addition of a mass separation agent. Consider a homogeneous liquid mixture. If this liquid mixture is partially vaporized, then another phase is created, and the vapor becomes richer in the more volatile components (i.e. those with the lower boiling points) than the liquid phase. The liquid becomes richer in the less-volatile components (i.e. those with the higher boiling points). If the system is allowed to come to equilibrium conditions, then the distribution of the components between the vapor and liquid phases is dictated by vapor-liquid equilibrium considerations (see Chapter 4). All components can appear in both phases. 

Bobbo, S.,Fedele, L., Camporese, R., Stryjek, R. (2000c) Isothermal vapor-liquid equilibrium for the three binary systems 1,1,1,2,3,3-hexafluoropropane with dimethyl ether or propane, and 1,1,1,3,3,3-hexafluoropropane with dimethyl ether. Fluid Phase Equilibria 174, 3-12. 

Bobbo, S., Stryjek, R., Elvassore, N., Bertucco, A. (1998) A recirculation apparatus for vapor-liquid equilibrium measurements of refrigerants. Binary mixtures ofR600a, R134a andR236fa. Fluid Phase Equilibria 150-151, 343-352. 

J. Vorholz et al., Vapor + liquid equilibrium of water, carbon dioxide, and the binary system, water + carbon dioxide, from molecular simulation. Fluid Phase Equilib. 170, 203 (2000)... 

If a fluid composed of more than one component (e.g., a solution of ethanol and water, or a crude oil) partially or totally changes phase, the required heat is a combination of sensible and latent heat and must be calculated using more complex thermodynamic relationships, including vapor-liquid equilibrium calculations that reflect the changing compositions as well as mass fractions of the two phases. 

In Chap. 6 we treated the thermodynamic properties of constant-composition fluids. However, many applications of chemical-engineering thermodynamics are to systems wherein multicomponent mixtures of gases or liquids undergo composition changes as the result of mixing or separation processes, the transfer of species from one phase to another, or chemical reaction. The properties of such systems depend on composition as well as on temperature and pressure. Our first task in this chapter is therefore to develop a fundamental property relation for homogeneous fluid mixtures of variable composition. We then derive equations applicable to mixtures of ideal gases and ideal solutions. Finally, we treat in detail a particularly simple description of multicomponent vapor/liquid equilibrium known as Raoult s law. 

Bian, B., Y. Wang, J. Shi, E. Zhao, and B.C.-Y. Lu. 1993. "Simultaneous Determination of Vapor-Liquid Equilibrium and Molar Volumes for Coexisting Phases up to the Critical Temperature with a Static Method", Fluid Phase Equil., 90 177-187. 

Huron, M.-J., G.-N. Dufour, and J. Vidal. 1978. "Vapor-Liquid Equilibrium and Critical Locus Curve Calculations with the Soave Equation for Hydrocarbon Systems with Carbon Dioxide and Hydrogen Sulphide" Fluid Phase Equil., 1 247-265. 

Ohgaki, K. and Katayama, T. 1977. "Isothermal Vapor-Liquid Equilibrium Data for the Ethane-Carbon Dioxide System at High Pressure" Fluid Phase Equil., 1 27-32. 

Zielkiewicz, J. Oracz, P. Vapor-liquid equilibrium in the ternary system Ai,V-dimethylformamide-methanol-water at 313.15 K. Fluid Phase Equilib. 1990, 59, 279-290. 

Rarey, J. R. Gmehling, 1. Computer-operated differential static apparatus for the measurement of vapor—liquid equilibrium data. Fluid Phase Equilib. 1993, 83, 279-287. 

Wilsak, R.A. Campbell, S.W. Thodos, G. Vapor-liquid equilibrium measurements for the n-pentane-methanol system at 372.7, 397.7, and 422.6 K. Fluid Phase Equilib. 1987, 33, 157-171. 

Blanco, A.M. Ortega, J. Experimental study of miscibility, density, and isobaric vapor-liquid equilibrium values of mixtures of methanol in hydrocarbons (C5, C6). Fluid Phase Equilib. 1996, 122, 207-222. 

Boukouvalas, C., Spiliotis, N., Coutsikos, P., and Tzouvaras, N., 1994. Prediction of vapor-liquid equilibrium with the LCVM model. A linear combination of the Huron-Vidal and Michelsen mixing rules coupled with the original UNIFAC and the t-mPR equation of state. Fluid Phase Eq., 92 75-106. 

Galivel-Solastiuk, F., Laugier, S., and Richon, D 1986. Vapor-liquid equilibrium data for the propane-methanoTcarbon dioxide system. Fluid Phase Eq., 28 73-85. 

Hong, J. H., and Kobayashi, R., 1988. Vapor-liquid equilibrium studies for the carbon dioxide-methanol system. Fluid Phase Eq., 41 269-276. 

Pividal, K. A., Sterner, C., Sandler, S. 1., and Orbey, H., 1992. Vapor-liquid equilibrium from infinite dilution activity coefficients Measurement and prediction of oxygenated fuel additives with alkanes. Fluid Phase Eq., 72 227-249. 

Shapiro, A., and Stenby, E. (2001) Thermod5mamics of the multicomponent vapor-liquid equilibrium under capillary pressure difference. Fluid Phase Equilibria 178, 17-32. 

While an enormous variety of phase equilibria exist, if we restrict ourselves to fluids, we need consider only the possible presence of a vapor and one or more liquid phases. The case most commonly encountered in chemical engineering (for example, in distillation) is vapor-liquid equilibrium (VLE). Multiple liquid phases (such as oil and water) can be in equilibriinn, so one... 

Hutchenson, K. W., J. R. Roebers, and M. C. Thies. 1990. Vapor-liquid equilibrium for phenanthrene-toluene mixtures at elevated temperatures and pressures. J. Fluid Phase Equil. 60 309-317. 

In this section we consider how one uses an equation of state to identify the states of vapor-liquid equilibrium in a pure fluid. The starting point is the equality of molar Gibbs energies in the coexisting phases. 

Keshtkar, a., Jalali, F. Moshfeghian, M. 1997. Evaluation of vapor-liquid equilibrium of CO2 binary systems using UNIQUAC-based Huron-Vidal mixing rules. Fluid Phase Equilibria, 140(1/2), 107-128. 

To date little or no thermodynamic modeling of the phase behavior of the ligand/C02 or metal chelate/C02 systems has been conducted. However, in order for supercritical fluid extraction to be considered as a possible replacement for organic solvent extraction, accurate models must be developed to predict the phase behavior of these systems to allow for both equipment and process design. Equation of state (EOS) modeling was chosen here to model the vapor-liquid equilibrium of the P-diketone/C02 systems studied. Cubic EOSs are the most widely used in modeling high pressure and supercritical fluid systems. This is... 

SA2 Sato, Y., Tsuboi, A., Sorakubo, A., Takishima, S., Masuoka, H., and Ishikawa, T., Vapor-liquid equilibrium ratios for hexane at irrfinite dilution in ethylene + impact polypropylene copolymer and propylene + impact polypropylene copolymer. Fluid Phase Equil, 170, 49, 2000. 

The new supplementary volume is again divided into the seven chapters as used before (1) Introduction, (2) Vapor-Liquid Equilibrium (VLE) Data and Gas Solubilities of Copolymer Solutions, (3) Liquid-Liquid Equilibrium (LLE) Data of Copolymer Solutions, (4) High-Pressure Fluid Phase Equilibrium (HPPE) Data of Copolymer Solutions, (5) Enthalpy Changes for Copolymer Solutions, (6) PVT Data of Copolymers and Solutions, and (7) Second Virial Coefficients (A2) of Copolymer Solutions. Finally, appendices quickly route the user to the desired datasets. 

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