In azeotropic distillation the added component, or entrainer, is taken overhead with one of two or more components being separated in a distillation column. If a second liquid phase forms upon condensing the overhead vapors, the entrainer-rich phase is refluxed or recycled back to the col umn. The other liquid phase is discarded, recycled to some suitable point in the plant, or processed further to recover dissolved components before being discarded. Methods pre sented earlier by one of the authors are applied to calculate two and three phase equilibria required in a computer pro gram for calculating azeotropic distillations. A brief descrip tion of the program is given; a sample output is listed and described. Calculated results for dehydrating aqueous etha nol mixtures are compared for the entrainers, n-pentane, benzene, and diethyl ether. Column flows, heat loads, and stage requirements are lowest for n-pentane. The entrain ers are rated in decreasing order of suitability: n-pentane, benzene, and diethyl ether.T^Vistribution of components between separable phases is the basis for **** most commonly used separation methods. Regardless of the type of separation step, its design depends on accurate distribution coefficients for the components between the contacting phases. These are given in compositions or more fundamental properties of the equilibrium phases.In distillation the components are distributed between separable vapor and liquid phases. The distribution coefficients or Κ values are the ratios of the vapor-liquid compositions in the equilibrium phases.They are expressed as the liquid phase activity coefficients, γ/s, the vapor 64 Downloaded by GEORGETOWN UNIV on August 25, 2015 |
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