Isobaric vapor-liquid equilibrium for chloroform + isopropanol + 1,3-dimethylimidazolium dimethylphosphate at 101.3 kPa

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As there is an azeotropic point between methanol and ethyl formate, they cannot be completely separated by ordinary distillation. In this paper, extractive distillation was applied and dimethyl sulfoxide (DMSO) and ethylene glycol (EG) were used as entrainers. Vapor−liquid equilibrium (VLE) data for methanol−ethyl formate, methanol−ethyl formate−DMSO, and methanol− ethyl formate−EG were measured at 101.3 kPa, and the NRTL model was applied for data fitting. It was found that the experimental value and the calculated value were accordant well through the deviation value. Then, the NRTL model was used for simulation by Aspen Plus to achieve the separation goal, and it verified the feasibility of the experimental scheme.

Section: Resultsmentioning

confidence: 99%

Vapor–Liquid Equilibrium Experiment and Process Simulation for Methanol and Ethyl Formate at 101.3 kPa

Han

Wang

et al. 2021

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“…Because the experiment was carried out in a low pressure, the presence of ILs in the gas phase could be ignored. When the system reached equilibrium, the gas phase could be considered an ideal gas. − The formulas for γ i and α 12 are shown below. …”

Section: Resultsmentioning

confidence: 99%

Vapor–Liquid Equilibrium Experiment for Butanone and Ethyl Acetate at 101.3 kPa

Wang

Jin

et al. 2021

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The formation of azeotrope brings severe challenges to the separation of butanone and ethyl acetate, two important chemical raw materials. In this article, two ionic liquids, 1-hexyl-3-methylimidazolium bis[(trifluoromethyland ethylene glycol (EG) were selected as entrainers to separate butanone and ethyl acetate. Vapor−liquid equilibrium data of butanone−ethyl acetate−[EMIM]-[NTf 2 ], butanone−ethyl acetate−[HMIM][NTf 2 ], and butanone−ethyl acetate−EG were measured at atmospheric pressure. The results show that the three extractants can effectively break the azeotrope of butanone−ethyl acetate, and the significant salt effect makes [EMIM][NTf 2 ] and [HMIM][NTf 2 ] show better separation ability than EG.Then, a non-random two liquid (NRTL) thermodynamic model was further used to fit the experimental data, and the average relative deviation was only 0.033, indicating that the NRTL model can well describe the influence of these three entrainers on the phase equilibrium behavior of butanone−ethyl acetate.

“…Meanwhile, the initial molar concentration of ILs in the liquid phase could be obtained with the mass of acetonitrile, ethanol, and ILs. Similar experimental methods were employed in our published literature studies. − …”

Section: Experimental and Computational Methodsmentioning

confidence: 96%

Vapor–Liquid Equilibrium for Acetonitrile + Ethanol with Imidazole-Based Ionic Liquids as Entrainers at 101.3 kPa

Yue,

Lu,

Chen

et al. 2024

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Vapor–liquid equilibrium (VLE) data for the ternary system of acetonitrile + ethanol + ionic liquids (ILs) were obtained at 101.3 kPa, and used ILs were 1-butyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ([BMIM][NTf2]), 1-ethyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ([EMIM][NTf2]), and 1-butyl-3-methylimidazolium diethylphosphate ([BMIM][DEP]). The nonrandom two-liquid (NRTL) model was used to correlate the VLE data and fitted well, indicating that the minimum mole fractions of [BMIM][NTf2], [EMIM][NTf2], and [BMIM][DEP] to eliminate the azeotrope was 0.053, 0.063, and 0.065, respectively. These ILs led to an outstanding “salting-in” effect on ethanol, and the salting effect on acetonitrile was inapparent. Higher concentrations of ILs signified a stronger salt effect as well as higher equilibrium temperatures. The results indicated that [BMIM][NTf2], [EMIM][NTf2], and [BMIM][DEP] could be used as good candidate entrainers to separate acetonitrile and ethanol in extractive distillation.