Vapor–Liquid Equilibrium Measurements of Ethanol and <i>n</i>-Nonane or <i>n</i>-Decane Binary Mixtures with Large Relative Volatility

Narasigadu, Caleb; Moodley, Kuveneshan; Raal, J. David

doi:10.1021/acs.jced.7b00875

Cited by 3 publications

(3 citation statements)

References 26 publications

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“…In this work, the VLE data of isoamyl dl -lactate and isoamyl alcohol were measured at three pressures (25.0, 50.0, and 101.3 kPa). The consistency of the equilibrium data was checked by the Wisniak , method and the van Ness − test. Meanwhile, the experimental data were correlated with the NRTL, Wilson, and UNIQUAC − models to estimate the parameters.…”

Section: Introductionmentioning

confidence: 99%

Isobaric Vapor–Liquid Equilibrium for Binary System of Isoamyl dl-Lactate and Isoamyl Alcohol at 25.0, 50.0, and 101.3 kPa

Zeng

2019

J. Chem. Eng. Data

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Isobaric vapor–liquid equilibrium (VLE) data for the binary system of isoamyl dl-lactate and isoamyl alcohol were measured at 25.0, 50.0, and 101.3 kPa in a modified Rose equilibrium still. The mixtures do not represent azeotropes. The determined experimental data were checked by Wisniak and van Ness tests to verify their thermodynamic consistency. Meanwhile, the Wilson, NRTL, and UNIQUAC models are adopted to correlate the VLE data, and the parameters of the three models were regressed. The UNIQUAC model showed the best fit to the experimental values relative to the Wilson and NRTL models, and it had the lowest root-mean-square deviations of equilibrium temperature (T) and mole fraction of the vapor phase (y 1), with the value of 1.54 K and 0.0234, respectively.

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Section: Introductionmentioning

confidence: 99%

Isobaric Vapor–Liquid Equilibrium for Binary System of Isoamyl dl-Lactate and Isoamyl Alcohol at 25.0, 50.0, and 101.3 kPa

Zeng

2019

J. Chem. Eng. Data

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“…Oxygenates such as lower alcohols are byproducts of petroleum processing from both the Fischer–Tropsch process and crude processing, and must be recovered to improve fuel quality and to valorize the alcohols produced. In previous studies, , our research unit has presented vapor–liquid equilibrium (VLE) measurements characterizing mixtures of lower alcohols with alkanes; however, such behaviors of lower alcohols, such as propanol isomers, with alkenes such as oct-1-ene are not available in sufficient quantity in the literature . This limits the development and optimization of processes for alcohol + alkene separation such as conventional, extractive, and azeotropic distillation.…”

Section: Introductionmentioning

confidence: 99%

Vapor–Liquid Equilibrium (P–T–x–y) Measurements and Modeling of propan-1-ol/propan-2-ol + oct-1-ene in the Range of T = (313.2–353.2) K

Moodley

2022

J. Chem. Eng. Data

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In this work, the isothermal vapor–liquid equilibrium (VLE) behavior was measured for systems consisting of propan-1-ol/propan-2-ol with oct-1-ene using a dynamic glass apparatus. The temperatures measured included (T = 313.2, 333.2, 353.2) K, which resulted in sub-atmospheric total pressures. The systems exhibit highly nonideal azeotropic behavior and large relative volatilities. The VLE data were correlated using the combined (γ-Φ) method, with the nonrandom two-liquid (NRTL) or universal quasi-chemical (UNIQUAC) activity coefficient models employed to account for the nonideality of the liquid phase, and the virial equation of state to describe the nonideality of the vapor phase. The nonrandom two-liquid model with the virial equation of state performed better than the UNIQUAC model with the virial equation of state in fitting the experimental data. The data for all systems were found to be thermodynamically consistent according to the area, point, and infinite dilution tests.

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“…Phase equilibrium data for alcohol + water/alkane systems are useful for the design of separation units, as these systems are commonly encountered in the petroleum industry as byproducts of reforming reactions . A common method for the measurement of such data is the use of circulating stills (dynamic method) that operate similar to a distillation column under total reflux. − At equilibrium, phase samples are analyzed by gas chromatography (GC) to establish the equilibrium composition. This method requires a substantial number of man-hours for operation as the gas chromatograph must be calibrated for each component pair to be measured, and phase sampling is time consuming.…”

Section: Introductionmentioning

confidence: 99%

Isothermal Vapor–Liquid Equilibrium Measurements for Alcohol + Water/n-Hexane Azeotropic Systems Using Both Dynamic and Automated Static-Synthetic Methods

et al. 2019

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Isothermal vapor–liquid equilibrium measurements (pressure– temperature–liquid and vapor composition) were conducted for water (1) + propan-1-ol (2), n-hexane (1) + butan-2-ol (2), and n-hexane (1) + 2-methyl-propan-1-ol (2) at three temperatures, each using a dynamic moderate pressure equilibrium still. Additionally, pressure–temperature-overall composition measurements for the first two systems were conducted for the intermediate temperatures using a newly automated static-synthetic apparatus to confirm the operability of the automation scheme and to compare the model predictions of the vapor-phase compositions from the processed pressure–temperature–liquid composition data by the static-synthetic method with the experimental vapor compositions measured by the dynamic method. The automation scheme was developed and implemented on the original static total pressure vapor–liquid equilibrium apparatus of Raal et al. (Fluid Phase Equilib. 2011, 310, 156–165) using the LabVIEW graphical programming language. In comparison to the manual operating mode, this scheme improved the efficiency of operation by reducing the man-hours involved and minimized the associated uncertainty with the measurement procedure with respect to liquid composition. Once executed, the control scheme requires approximately 2 days to produce a single 40-data point (pressure–temperature–liquid composition) isotherm and minimizes human intervention to 2–3 h in comparison to a 2-week long measurement procedure in the nonautomated operating mode and in excess of 3 weeks using the dynamic method with analysis by gas chromatography. All experimental data were modeled using the γ–Φ approach with the NRTL and UNIQUAC activity coefficient models and the virial equation of state with the Hayden and O’Connell correlation. For the pressure–temperature–liquid and vapor composition data measured, thermodynamic consistency testing was performed. The data sets passed the point test with 0.01 tolerance and the area test with 10% tolerance. Experimental vapor-phase compositions obtained by phase sampling in the dynamic method compared reasonably well with the predictions from the pressure–temperature–liquid composition data measured by the automated static-synthetic method.

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Vapor–Liquid Equilibrium Measurements of Ethanol and n-Nonane or n-Decane Binary Mixtures with Large Relative Volatility

Cited by 3 publications

References 26 publications

Isobaric Vapor–Liquid Equilibrium for Binary System of Isoamyl dl-Lactate and Isoamyl Alcohol at 25.0, 50.0, and 101.3 kPa

Isobaric Vapor–Liquid Equilibrium for Binary System of Isoamyl dl-Lactate and Isoamyl Alcohol at 25.0, 50.0, and 101.3 kPa

Vapor–Liquid Equilibrium (P–T–x–y) Measurements and Modeling of propan-1-ol/propan-2-ol + oct-1-ene in the Range of T = (313.2–353.2) K

Isothermal Vapor–Liquid Equilibrium Measurements for Alcohol + Water/n-Hexane Azeotropic Systems Using Both Dynamic and Automated Static-Synthetic Methods

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