Ternary systems fluid phase equilibria

Gauter, K., Florusse, LJ., Peters, CJ. and de Swaan Aarons, J. (1996) Classification of and transformations between types of fluid phase behavior in selected ternary systems. Fluid Phase Equilibria, 116,445-453. 

Klante, D. (1999) Fluid phase equilibrium investigations of binary and ternary aqueous systems with a diamond anvil cell up to 25 kbar (in German), Doctoral dissertation, University of Bochum, Germany. 

Bernatova, S. Wichterle, I. Isothermal vapour-liquid equilibrium in the binary tert-butanol or 2,2,4-trimethylpentane + l-tert-butoxy-2-propanol, and in the ternary tert-butanol + 2,2,4-trimethylpentane + l-tert-butoxy-2-propanol systems Fluid Phase Equilib. 2001,189, 111-118... 

Zafarani-Moattar MX, Jafari P (2013) Phase diagrams for liquid-liquid and liquid-solid equilibrium of the ternary polyethylene glycol + di-sodium hydrogen citrate + water system. Fluid Phase Equil 337 224-233... 

Hwang, I.-C. Lim, H.-M. Park, S.-J. Han, K.-J. Park, I.-H. Isothermal vapor-hquid equilibrium at 303.15 K and excess molar volumes at 298.15 K for the ternary system of propyl vinyl ether + 1-propanol + 2,2,4-trimethyl-pentane and its binary sub-systems. Fluid Phase Equihb. 2007, 259, 146-152. 

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). 

The basic for developing a high pressure liquid extraction unit is the phase equilibrium for the (at least) ternary system, made up of compound A and compound B, which have to be separated by the supercritical fluid C. Changing pressure and temperature influences on one hand the area of the two phase region, where extraction takes place, and on the other hand the connodes, representing the equilibrium between extract and raffinate phase. 

The equilibrium interfaces of fluid systems possess one variant chemical potential less than isolated bulk phases with the same number of components. This is due to the additional condition of heterogeneous equilibrium and follows from Gibbs phase rule. As a result, the equilibrium interface of a binary system is invariant at any given P and T, whereas the interface between the phases a and /3 of a ternary system is (mono-) variant. However, we will see later that for multiphase crystals with coherent boundaries, the situation is more complicated. 

We note that even short-range interactions may, however, allow a mean-field scenario, if the system has a tricritical point, where three phases are in equilibrium. A well-known example is the 3He-4He system, where a line of critical points of the fluid-superfluid transition meets the coexistence curve of the 3He-4He liquid-liquid transition at its critical point [33]. In D = 3, tricriticality implies that mean-field theory is exact [11], independently from the range of interactions. Such a mechanism is quite natural in ternary systems. For one or two components it would require a further line of hidden phase transitions that meets the coexistence curve at or near its critical point. 

A recirculation apparatus for the determination of high pressure phase equilibrium data for mixtures of water, polar organic liquids and supercritical fluids was constructed and operated for binary and ternary systems with supercritical carbon dioxide. 

The system carbon dioxide - acetone - water was investigated at 313 and 333 K. The system demonstrates several of the general characteristics of phase equilibrium behavior for ternary aqueous systems with a supercritical fluid. These include an extensive LLV region that appears at relatively low pressures. Carbon dioxide exhibits a high selectivity for acetone over water and can be used to extract acetone from dilute aqueous solutions. 

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. 

Ehsan Sheikholeslamzadeh and Sohrab Rohani. Vapour-liquid and vapour-liquid-liquid equilibrium modeling for binary, ternary, and quaternary systems of solvents. Fluid Phase Equilibria, 333, 97-105. 

Yao S, Guan Y, Zhu Z. Investigation of phase equilibrium for ternary systems containing ethanol, water and carbon dioxide at elevated pressures. Fluid Phase Equilibria 1994 99 249-259. 

In figure 3.29c the pressure has now been increased to a value greater than the critical pressure for the SCF-B mixture. The SCF is now miscible in all proportions with B, and the binodal curve no longer intersects the SCF-B binary axis of the ternary diagram. Even at this elevated pressure, the SCF still remains virtually insoluble in A, as would be the case if the supercritical fluid were a low molecular weight hydrocarbon and component A were water (Culberson and McKetta, 1951). As shown in figure 3.29c, the binodal curve intersects the SCF-A binary axis in two locations. The tie lines for the ternary system now indicate that a liquid phase, mostly a mixture of A and B, is in equilibrium with a fluid phase, mainly the SCF with component B. 

ZAF Zafarani-Moatlar, M.T., Hamzehzadeh, S., and Hosseinzadeh, S., Phase diagrams for liquid-hquid equilibrium of ternary poly(ethylene glycol) + disodium tartrate aqueous system and vapor-liquid equilibrium of constituting binary aqueous systerrrs at r = (298.15, 308.15, and 318.15) K. Experiment and correlation. Fluid Phase Equil, 268, 142, 2008. 

Chamorro, C. R.j Segovia, J. J. Martin, M. C. Montero, E. A. Villamanan, M. A. Phase equilibrium properties of binary and ternary systems containing tert-amyl methyl ether (TAME) as oxygenate additive and gasoline substitution hydrocarbons at 313.15 K Fluid Phase Equilib. 1999, i56,73-87... 

Gomis, V., Font, A., and Saquete, M.D., "Vapour-Liquid-Liquid and Vapour-Liquid Equilibrium of the System Water + Ethanol + Fleptane at 101 3 kPa," Fluid Phase Equilibria, Vol. 248, 2006, pages 206 to 210. This research reports that a ternary azeotrope is formed when the binary azeotrope (entry 456 in Ref 3, Table A 2-2, 48% alcohol) is contacted with water The boiling point of the ternary azeotrope is 3 C less. 

Ternary system consists of one volatile and two nonvolatile components, such phenomena as an azeotropy in liquid-gas equilibria and a formation of binary or ternary compounds are absent. Solid phases of volatile and each non-volatile components are completely immiscible and have the eutectic relations in equilibrium with fluid phases, whereas the solid phases of non-volatile components form a continuous solid solution. 

Liquid-liquid equilibrium (LEE) data of ternary systems are required for the design of liquid extraction processes. Also, there is a constant need for phase equilibrium data of these systems for simulation and optimize of separation equipment, valuable information about the molecular interactions, macroscopic behavior of fluid ntixtures, and can be used to test and improve thermodynamic models for calculating and predicting fluid-phase equilibria. 

Goemert M, Sadowski G (2008) Phase-equilibrium measurement and modeling of the PMMA/MMA/carbon dioxide ternary system. J Supercrit Fluids 46 218-225... 

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