Abstract

In the first part of this work, a model-free technique for treating ternary systems was presented. The procedure avoids the use of empirical activity coefficient models by generating numerically vapor-phase concentrations, activity coefficients, and excess Gibbs energy values directly from [T, P, x] data. Here we illustrate the use of the method as a complementary tool for modeling and assessing multicomponent vapor-liquid equilibrium data. Guidelines are given for fitting bubble surfaces and for treating azeotropic systems. In addition, reasonable approximations are outlined for handling ternary systems for which excess volume or enthalpy data are not available. Examples are presented for experimental isothermal and isobaric systems.