Liquid–liquid equilibrium for the ternary systems water+2-methyl-1-propanol+butyl acetate and water+2-methyl-2-propanol+butyl acetate at (298.15 and 323.15)K

Xu, Dongmei; Wu, Chunxia; Zhang, Qing; Zhang, Huan; Wang, Yinglong; Gao, Jun

doi:10.1016/j.fluid.2014.08.014

Cited by 25 publications

(12 citation statements)

References 27 publications

(27 reference statements)

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“…2 Many papers about the LLE containing alcohols and water have been reported recent years [2][3][4][5][6][7][8][9][10][11][12][13][14][15][16][17][18][19][20][21]. Some researchers among these papers present the influences of traditional organic solvent on the LLE of alcohols and water [3][4][5][6][7]14].…”

Section: Accepted Manuscriptmentioning

confidence: 99%

Liquid–liquid equilibria for ternary mixtures of water + 2-propanol + 1-alkyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ionic liquids at 298.15 K

Liu

Zhang

et al. 2016

Fluid Phase Equilibria

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Section: Accepted Manuscriptmentioning

confidence: 99%

Liquid–liquid equilibria for ternary mixtures of water + 2-propanol + 1-alkyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ionic liquids at 298.15 K

Liu

Zhang

et al. 2016

Fluid Phase Equilibria

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“…Butyl acetate is an excellent organic solvent, , which has been widely applied in the production of cellulose acetate butyrate, chlorinated rubber, polystyrene, and used in petroleum processing and pharmaceutical processes. , Generally, butyl acetate can be synthesized by the esterification reaction of acetic acid with 1-butanol. , Because butyl acetate and 1-butanol can form an azeotrope with the minimum boiling point at atmospheric pressure, , it is difficult to purify butyl acetate from the azeotropic mixture of 1-butanol and butyl acetate by traditional distillation.…”

Section: Introductionmentioning

confidence: 99%

Liquid–Liquid Equilibrium Measurements and Correlation for Ternary Systems (Butyl Acetate + 1-Butanol + Ethylene Glycol/1,3-Propanediol/Ethanolamine) at 298.15 K

et al. 2019

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For separation of the azeotropic mixture butyl acetate and 1butanol, ethylene glycol, 1,3-propanediol, and ethanolamine were chosen as the extractants. The phase equilibria for the ternary systems (butyl acetate + 1-butanol + ethylene glycol/1,3-propanediol/ethanolamine) were investigated, and the liquid−liquid equilibrium (LLE) data were determined at 298.15 K and 101.3 kPa. During the LLE measurement, the equilibrium was achieved when the prepared ternary mixture was stirred for 2 h and settled for 12 h. To evaluate the extraction capacity of the solvents, the distribution constant (D) and selectivity (S) were calculated. From the comparison of the values of D and S, ethanolamine is the best extractive solvent among the three solvents. In the meantime, the nonrandom twoliquid (NRTL) and the universal quasi-chemical (UNIQUAC) models were applied to correlate the LLE data for the systems. The values of the root mean square deviations between the experimental LLE data and calculated values were less than 0.01. Also, the binary interaction parameters of the NRTL and UNIQUAC models were optimized.

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“…Liquid-liquid equilibrium experiments for the mixture (DESs + isopropanol + water) were performed at different temperatures under 101.3 kPa. For detailed procedures and apparatus, refer to the literatures (Xu et al 2014). The cloud point method (Letcher et al 1986) was applied in the process of pre-experiment to make the compositions of each component cover the range of the heterogeneous phase entirely.…”

Section: Apparatus and Proceduresmentioning

confidence: 99%

Separation of isopropanol from its aqueous solution with deep eutectic solvents: liquid–liquid equilibrium measurement and thermodynamic modeling

Meng

Liu

et al. 2020

Braz. J. Chem. Eng.

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In this work, to separate the azeotrope of isopropanol and water using liquid-liquid extraction, two deep eutectic solvents (DESs) were prepared with methyl trioctyl ammonium chloride and (1-hexanol/1-decanol), which were characterized by 1 H NMR and were adopted as extractants. The liquid-liquid equilibrium data for the mixtures (DESs + isopropanol + water) were determined at 298.15 K and 308.15 K. The distribution ratio (D) and separation factor (S) were obtained to judge the extraction performance for the selected DESs. The calculated values of D and S showed that the separation of the mixture isopropanol and water by the DESs is feasible. In addition, the experimental data were successfully fitted by the NRTL model with the RMSD values less than 0.0080. The parameters of the NRTL model were optimized, which is helpful for the separation design and simulation.

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Liquid–liquid equilibrium for the ternary systems water+2-methyl-1-propanol+butyl acetate and water+2-methyl-2-propanol+butyl acetate at (298.15 and 323.15)K

Cited by 25 publications

References 27 publications

Liquid–liquid equilibria for ternary mixtures of water + 2-propanol + 1-alkyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ionic liquids at 298.15 K

Liquid–liquid equilibria for ternary mixtures of water + 2-propanol + 1-alkyl-3-methylimidazolium bis(trifluoromethylsulfonyl)imide ionic liquids at 298.15 K

Liquid–Liquid Equilibrium Measurements and Correlation for Ternary Systems (Butyl Acetate + 1-Butanol + Ethylene Glycol/1,3-Propanediol/Ethanolamine) at 298.15 K

Separation of isopropanol from its aqueous solution with deep eutectic solvents: liquid–liquid equilibrium measurement and thermodynamic modeling

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