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This paper shows how knowledge of the univolatility and nidistribution line location and residue curve analysis help to assess the feasibility of batch extractive rectifying or stripping distillation of azeotropic mixtures by using an intermediate boiling entrainer. We consider five minimum boiling (minT) azeotropic mixtures AB with entrainer E, namely, acetone−heptane with benzene, methanol−toluene with triethylamine, methyl acetate−cyclohexane with carbon tetrachloride, dichloromethane−ethanol with acetone, and ethyl acetate−heptane with benzene; and one maximum boiling (maxT) azeotropic mixture, namely, chloroform−ethyl acetate with either 2-chlorobutane, isobutylchloride, bromopropane, or bromochloromethane. All ternary diagrams A−B−E belong to the 1.0-1b class, for which all three possible univolatility, !AB, !BE, and !AE, and unidistribution lines, KA, KB, and KE can exist. With application of the general feasibility criterion of Rodriguez-Donis et al. (Ind. Eng. Chem. Res. 2009, 48 (7), 3544−3559), both azeotropic components, A and B, accomplish the criterion, and they can be recovered, A in an\udextractive rectifier and B in an extractive stripper. The process efficiency of each alternative depends strongly on the location of\udthe !AB univolatility line interception with the triangle edge, and also depends on the !BE (!AE) in the minT (maxT) case and of\udthe unidistribution line KE closeness to the (E−B) (A−E) edge. Besides, choice of the rectification of A instead of the stripping of\udB is set by the ratio of !AE/!BE, the ratio of relative volatility variation of the binary mixtures between A or B and E

Thermodynamic Insights on the Feasibility of Homogeneous Batch Extractive Distillation. 4. Azeotropic Mixtures with Intermediate Boiling Entrainer