Separation of azeotrope 2,2,3,3-tetrafluoro-1-propanol and water by extractive distillation using ionic liquids: Vapor-liquid equilibrium measurements and interaction analysis

Liquid-liquid phase equilibrium and interaction exploration for separation of azeotrope (2,2,3,3-tetrafluoro-1-propanol + water) with two imidazolium-based ionic liquids

“…Li et al [16] applied extractive distillation to separate TFP and water with N-methyl pyrrolidone, N, N-dimethyl formamide and N-methyl formamide as the entrainers. In addition, Diao et al [17] also applied extractive distillation but chose the different entrainers [EMIM][Ac] and [EMIM][Cl] to recover TFP from its aqueous solution.…”

Effect and Mechanism of 1-Hexyl-3-methylimidazolium-Based Ionic Liquids on the Isobaric Vapor–Liquid Equilibria of Methanol + Acetonitrile at 101.3 kPa

“…This work adopted the NRTL model to calculate the activity coefficients (γ i ) for the binary system (methanol + acetonitrile) and the ternary systems {methanol + acetonitrile + ([HMIM]­[BF 4 ] or [HMIM]­[OTF])} because of its mathematical simplicity and precision. − The nonrandomness parameter of the NRTL model (α ij ) and the energy parameter of the NRTL model (Δ g ij and Δ g ji ) could be regressed through minimizing the function shown below where γ i exp and γ i calc denote the experimental and calculated activity coefficients, respectively, and N is the number of the experiment.…”

Process design, evaluation and control for separation of 2,2,3,3‐tetrafluoro‐1‐propanol and water by extractive distillation using ionic liquid 1‐ethyl‐3‐methylimidazolium acetate

“…The NRTL model is adopted to describe the non-ideality of liquid phase, which is usually applied to correlate the vapor-liquid equilibrium (VLE) data concerning the ILs compared to the predictive UNIFAC 31 and UNIFAC-Lei 24 models. The binary interaction parameters of the NRTL model for IL-TFP, IL-water, 30 and TFP-water 5 are listed in Supporting Information, Table S1. Meanwhile, the critical properties 32 and ideal gas heat capacity (CPIG) 33 are presented in the Supporting Information, Tables S2 and S3.…”

“…[27][28][29] In this paper, three extractive distillation processes with 1-ethyl-3-methylimidazolium acetate ([EMIM][Ac]) as a proper entrainer are designed based on the previous experimental work, which has shown that IL [EMIM][Ac] can effectively eliminate the azeotropic point of the mixture TFP and water. 5,30 To obtain high purity TFP and recycle [EMIM][Ac], three processes are optimized and compared by total annual cost (TAC), CO 2 emissions, and global energy consumption (GEC). A process is proposed by adjusting the temperature of the entrainer through the stages of stripper and the flow rate of air without a heat exchanger to save on operation costs.…”