Isobaric vapor–liquid equilibrium for ethyl acetate + ethanol with ionic liquids [MMIM][DMP] and [OMIM][PF6] as entrainers

Yue, Kun; Zhou, Guowei

doi:10.1016/j.molliq.2021.118404

Cited by 12 publications

(7 citation statements)

References 39 publications

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“…And p-x 1 -y 1 and y-x diagrams are displayed in Figures – . The relative volatility α ij was computed by the following equation: α ij = K i K j = y i x i y j x j …”

Section: Resultsmentioning

confidence: 99%

Vapor–Liquid Equilibrium of Monoterpene-Sesquiterpene System Containing Resin Acid

Wang,

Wei,

Xie

et al. 2024

Ind. Eng. Chem. Res.

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The phase equilibrium relationships of resin systems are indispensable for resin tapping, distillation, and investigating the release of terpenes in biogenic volatile organic compounds (BVOCs). Herein, we obtained the vapor–liquid equilibrium (VLE) data of monoterpene-sesquiterpene systems that contain resin acid by a headspace gas chromatography (HS-GC). There is no azeotropic behavior between terpenes, and abietic acid was found to inhibit the volatilization and separation of terpenes. Furthermore, the saturated vapor pressure of the systems almost triples when the experimental temperature increases from 313.15 to 333.15 K, which may exacerbate terpene emissions in ecosystems. Additionally, the thermodynamic consistency of the VLE values was confirmed by van Ness test, and the experimental data were correlated using NRTL, UNIQUAC, and Wilson activity coefficient models, while the Conductor-like Screening Model for Real Solvents (COSMO-RS) model was utilized for predictions. All of the data satisfy thermodynamic consistency, and the correlation results and prediction results demonstrate good adherence of the activity coefficient models to experimental values and the positive capacity of COSMO-RS in predicting the VLE relationship for the pine resin systems, respectively.

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“…And p-x 1 -y 1 and y-x diagrams are displayed in Figures – . The relative volatility α ij was computed by the following equation: α ij = K i K j = y i x i y j x j …”

Section: Resultsmentioning

confidence: 99%

Vapor–Liquid Equilibrium of Monoterpene-Sesquiterpene System Containing Resin Acid

Wang,

Wei,

Xie

et al. 2024

Ind. Eng. Chem. Res.

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“…In this work, the experiment was carried out under low and negative pressure. When equilibrium is reached, the gas phase could be considered an ideal gas. , The VLE formula is as follows: p y i = x i γ i p i s The formula for calculating the relative volatility is as follows: α 12 = ( y 1 x 1 ) / ( y 2 x 2 ) The measured isobaric VLE data and activity coefficients (γ i ) for the binary 2-MADE (1) + DMA (2) mixture at 101.3, 50.0, 30.0, and 10.0 kPa are reported in Table , which shows that the activity coefficients are all greater than 1. This binary system is a positive deviation system of Raoult’s law at different pressures.…”

Section: Resultsmentioning

confidence: 99%

Isobaric Vapor–Liquid Equilibrium of Binary Mixtures of 2-Methylpentanedioic Acid Dimethyl Ester and Dimethyl Adipate at 101.3, 50.0, 30.0, and 10.0 kPa

Wang,

Zhao,

Han

et al. 2024

J. Chem. Eng. Data

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The vapor pressures of pure 2-methylpentanedioic acid dimethyl ester (2-MADE) and dimethyl adipate (DMA) at corresponding temperatures were measured by a rose-type vapor–liquid equilibrium still and compared with those in the literature. The isobaric vapor–liquid phase equilibrium (VLE) of binary mixtures of 2-MADE and DMA at 101.3, 50.0, 30.0, and 10.0 kPa were measured in the same still. It is verified by the Fredenslund test and the Van Ness test that all data are consistent with thermodynamics. NRTL, UNIQUAC, and Wilson models were used to regress the experimental data, and the deviation between the experimental data and the model was small. These models are suitable for the binary mixed system.

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“…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

J. Chem. Eng. Data

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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.

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Isobaric vapor–liquid equilibrium for ethyl acetate + ethanol with ionic liquids [MMIM][DMP] and [OMIM][PF6] as entrainers

Cited by 12 publications

References 39 publications

Vapor–Liquid Equilibrium of Monoterpene-Sesquiterpene System Containing Resin Acid

Vapor–Liquid Equilibrium of Monoterpene-Sesquiterpene System Containing Resin Acid

Isobaric Vapor–Liquid Equilibrium of Binary Mixtures of 2-Methylpentanedioic Acid Dimethyl Ester and Dimethyl Adipate at 101.3, 50.0, 30.0, and 10.0 kPa

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

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