Effect of the quality of the vapor-liquid equilibrium (VLE) description on the results of the separation simulation considering real behavior of either liquid or both equilibrium phases was tested. Results of the column steady-state operation were compared with those obtained assuming different equilibrium models. An empirical AICHE correlation was adopted for the calculation of binary mass transfer coefficients at column trays. Non-equilibrium model of a column for extractive distillation accounting for the mass and heat transfer rates was composed according to the rigorous Maxwell-Stefan theory. As an example, separation of azeotrope formed by 2-methoxy-2-methylpropane and methanol was considered using butan-1-ol as an extractive solvent. ![]() Influence of model complexity on the separation equipment performance was investigated.
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