Example 1 Ideal Ternary System

In this example, the effect of a selective membrane on the ternary mixture undergoing a reversible chemical reaction in ideal liquid phase is considered  

The relative volatilities are ccba = 5 and acA = 3, and the chemical equilibrium constant Keq = 5. 

In a kinetically controlled chemical reaction (Da = 1 Fig. 4.27(b)), the stable node moves from the pure A vertex into the composition triangle. In an equilibrium-controlled chemical reaction (Da — °° Fig. 4.27(c)), the reaction approaches its chemical equilibrium, and therefore the stable node is located on the equilibrium surface. 

At kinetically controlled reactive conditions (Da = 1), Fig. 4.28(b) shows that the stable node moves into the composition triangle, as in reactive distillation (Fig. 4.27(b)). This point is termed the kinetic arheotrope because its location in the phase diagram depends on the membrane mass transfer resistances and also on the rate of chemical reaction. The kinetic arheotrope moves towards the B vertex with increasing C-selectivity of the membrane. At infinite Damkohler number, the system is chemical equilibrium-controlled (Fig. 4.28(c)), and therefore the arheotrope is located exactly on the chemical equilibrium curve. In this limiting case, it is called a reactive arheotrope . 

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P8.10 Determine the solid-liquid equilibrium temperature of the ideal ternary system m-xylene (l)-o-xylene (2)-p-xylene (3) for a composition ofxi = 0.1 and X2 =0.1 with the help of the melting temperatures and enthalpies of fusion given in Example 8.4 in the textbook. Which component will crystallize ... 

The present paper is concerned with mixtures composed of a highly nonideal solute and a multicomponent ideal solvent. A model-free methodology, based on the Kirkwood—Buff (KB) theory of solutions, was employed. The quaternary mixture was considered as an example, and the full set of expressions for the derivatives of the chemical potentials with respect to the number of particles, the partial molar volumes, and the isothermal compressibility were derived on the basis of the KB theory of solutions. Further, the expressions for the derivatives of the activity coefficients were applied to quaternary mixtures composed of a solute and an ideal ternary solvent. It was shown that the activity coefBcient of a solute at infinite dilution in an ideal ternary solvent can be predicted in terms of the activity coefBcients of the solute at infinite dilution in subsystems (solute + the individual three solvents, or solute + two binaries among the solvent species). The methodology could be extended to a system formed of a solute + a multicomponent ideal mixed solvent. The obtained equations were used to predict the gas solubilities and the solubilities of crystalline nonelectrolytes in multicomponent ideal mixed solvents. Good agreement between the predicted and experimental solubilities was obtained. 

Sundmacher and Qi (Chapter 5) discuss the role of chemical reaction kinetics on steady-state process behavior. First, they illustrate the importance of reaction kinetics for RD design considering ideal binary reactive mixtures. Then the feasible products of kinetically controlled catalytic distillation processes are analyzed based on residue curve maps. Ideal ternary as well as non-ideal systems are investigated including recent results on reaction systems that exhibit liquid-phase splitting. Recent results on the role of interfadal mass-transfer resistances on the attainable top and bottom products of RD processes are discussed. The third section of this contribution is dedicated to the determination and analysis of chemical reaction rates obtained with heterogeneous catalysts used in RD processes. The use of activity-based rate expressions is recommended for adequate and consistent description of reaction microkinetics. Since particles on the millimeter scale are used as catalysts, internal mass-transport resistances can play an important role in catalytic distillation processes. This is illustrated using the syntheses of the fuel ethers MTBE, TAME, and ETBE as important industrial examples. 

The problem of solvent selection is relatively complex and a thorough treatment requires considerable information. In addition to basic liquid-liquid equilibrium data, knowledge of the phase densities, viscosities, and the liquid-liquid interfacial tension is also important. Moreover, the economics of IXE systems are often dominated by the solvent regeneration costs. If, for example, solvent regeneration b to be accomplished by extractive or azeotropic distillation, then vapor-liquM equilibrinm data for the ternary system must also be available. Insofar as the most interesting LLE systems ate often ffiose whidi are least ideal, the generation of a physical property data base to complete cost analysis is usually a sigruficant problem. 

In the preceding sections, the feed phase and the extract phase were assumed to be insoluble over the range of solute concentrations. Therefore the process analysis and design of solvent extraction was simpler. However, in many systems, the feed phase (primary constituent A, for example water) and the extract phase (primary constituent is solvent B) have some degree of solubility in each other as the solute species C is transferred firom the feed phase to the extract phase. Therefore both phases are ternary mixtures with significant concentrations of species A and B. Analysis of such ternary systems of ideal stages is... 

For azeotropic distillation especially the systems are non-ideal which makes calculating vapor-liquid equilibrium properties more difficult than, for example, in distillation of mixtures of simple hydrocarbons. Work predicting the vapor-liquid equilibrium properties of ternary mixtures of... 

NPC is ideally suited for the analysis of compounds prone to hydrolysis because it employs nonaqueous solvents for the modulation of retention. An example of the use of NPC in the analysis of a hydrolysable analyte was demonstrated by Chevalier et al. [28] for quality control of the production of benorylate, an ester of aspirin. A major issue in benorylate production is the potential formation of impurities suspected of causing allergic side effects therefore monitoring of this step is critical to quality control. The presence of acetylsalicylic anhydride prohibited the use of RPLC since it can be easily hydrolyzed in the water-containing mobile phase. However, an analytical method based on the use of normal-phase chromatography with alkylnitrile-bonded silica as the stationary phase provided an ideal solution to the analysis. Optimal selectivity was achieved with a ternary solvent system hexane-dichloromethane-methanol, containing 0.2 v/v% of acetic acid to prevent the ionization of acidic function and to deactivate the residual silanols. The method was validated and determined to be reproducible based on precision, selectivity, and repeatability. 

There are two peculiarities of the ternary reciprocal system. The first one concerns the activities and the chemical potentials. Regardless of the way the solution was made up, the activities and chemical potentials of all the four constituents are defined and are the same no matter which of the three components were chosen. In our example for the Temkin s ideal solution a x = x +xx = 0.15, [Pg.132]

Such a process depends upon the difference in departure from ideally between the solvent and the components of the binary mixture to be separated. In the example given, both toluene and isooctane separately form nonideal liquid solutions with phenol, but the extent of the nonideality with isooctane is greater than that with toluene. When all three substances are present, therefore, the toluene and isooctane themselves behave as a nonideal mixture and then-relative volatility becomes high. Considerations of this sort form the basis for the choice of an extractive-distillation solvent. If, for example, a mixture of acetone (bp = 56.4 C) and methanol (bp = 64.7°Q, which form a binary azeotrope, were to be separated by extractive distillation, a suitable solvent could probably be chosen from the group of aliphatic alcohols. Butanol (bp = 117.8 Q, since it is a member of the same homologous series but not far removed, forms substantially ideal solutions with methanol, which are themselves readily separated. It will form solutions of positive deviation from ideality with acetone, however, and the acetone-methanol vapor-liquid equilibria will therefore be substantially altered in ternary mixtures. If butanol forms no azeotrope with acetone, and if it alters the vapor-liquid equilibrium of acetone-methanol sufficiently to destroy the azeotrope in this system, it will serve as an extractive-distillation solvent. When both substances of the binary mixture to be separated are themselves chemically very similar, a solvent of an entirely different chemical nature will be necessary. Acetone and furfural, for example, are useful as extractive-distillation solvents for separating the hydrocarbons butene-2 and a-butane. 

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