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To separate the mixture of dimethyl carbonate and methanol, two deep eutectic solvents (DESs), choline chloride with glycerol and ethylene glycol, with the molar ratio of 1:2 were prepared to separate dimethyl carbonate from the mixture by liquid−liquid extraction. The liquid−liquid equilibrium (LLE) data for the ternary systems of dimethyl carbonate + methanol + DESs were determined at temperature of 298.15 and 308.15 K under 101.3 KPa. The measured tie-line data were validated by the Bachman equation, and the correlation coefficients (R 2 ) were all close to 1. Meanwhile, the distribution coefficient and selectivity were calculated from the experimental results. The LLE experimental data were correlated using the nonrandom two-liquid (NRTL) model, and the correlated results agree well with the LLE experimental data. Also, the parameters of the NRTL model were regressed.

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BACKGROUND: 2,2,3,3-tetrafluoro-1-propanol (TFP) is a good solvent that is applied in the electronic industry. To recover TFP from its aqueous solution, conventional distillation cannot be adopted because TFP and water can form a minimum azeotrope. RESULTS: In this work, extractive distillation is applied to separate the azeotropic mixture of TFP and water using 1-ethyl-3-methylimidazolium acetate ([EMIM][Ac]) as an entrainer. Based on the analysis of residual curve map, three processes are designed to separate the mixture. Extractive distillation processes (EDP) I and II consist of an extractive column and two flashes, and EDP III consists of an extractive column, a flash, and a stripper. For evaluating the three processes, total annual cost (TAC), CO 2 emissions and global energy consumption (GEC) are considered into the objective function. CONCLUSION:The simulated results show that EDP III with an extractive column, a flash, and a stripper can provide better economic and environmental benefits. Water can be obtained from the extractive column with a molar purity of 99.7%. TFP can be separated from the top of the flash and stripper with a molar purity of 99.7%. Furthermore, the control structure with two-point temperature for EDP III is explored and it shows good responses for the disturbances of feed flow rate and composition.