Vapor pressures of binary mixtures of hexane + 1-butanol, + 2-butanol, + 2-methyl-1-propanol, or +2-methyl-2-propanol at 298.15 K

Rodrı́guez, V.D.; Pardo, Juan I.; López, M.; Royo, F.M.; Urieta, José S.

doi:10.1021/je00011a003

Cited by 34 publications

(23 citation statements)

References 5 publications

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“…The rupture of hydrogen bonds of butanol isomers and the breaking of dipole-dipole interactions of 1-chlorobutane predominate over the formation of new interactions between molecules of butanol and chlorobutane. Our results are also in good concordance with previously reported VLE data for the constituent binary mixtures at T = 298.15 K [19,23,24,26]. The biggest G E values correspond to mixtures with small mole fractions of chlorobutane, revealing that n-hexane is very efficient breaking the hydrogen bonds of the pure butanols, while butanol-chlorobutane interactions partially compensate the rupture of the selfinteractions.…”

Section: Resultssupporting

confidence: 92%

“…To our knowledge, there is not any isothermal VLE study on the ternary systems presented here, although there are some previous reports on the constituent binary systems at different temperatures: 1-butanol + n-hexane [14][15][16][17][18][19], 2-butanol + n-hexane [19][20][21][22], 1-butanol or 2-butanol + 1-chlorobutane [23,24], and n-hexane + 1-chlorobutane [25,26].…”

Section: Introductionmentioning

confidence: 99%

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(Vapour+liquid) equilibrium and excess Gibbs functions of ternary mixtures containing 1-butanol or 2-butanol, n-hexane, and 1-chlorobutane at T=298.15K

Martı́nez

Bandrés

Ballesteros

et al. 2009

The Journal of Chemical Thermodynamics

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Section: Resultssupporting

confidence: 92%

Section: Introductionmentioning

confidence: 99%

(Vapour+liquid) equilibrium and excess Gibbs functions of ternary mixtures containing 1-butanol or 2-butanol, n-hexane, and 1-chlorobutane at T=298.15K

Martı́nez

Bandrés

Ballesteros

et al. 2009

The Journal of Chemical Thermodynamics

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“…Solid black symbols represent the liquid phase, and open symbols represent the vapor phase. Literature data: ( P – x )orange triangle, (Prasad et al at 342.45 K); ( P – x – y )( x 1  orange ×, y 1  orange +), (Berro et al at 332.53 K); ( P – x – y ) ( x 1  orange circle, y 1  ornage open circle (calculated)), (Rodriguez et al at 289.15 K); orange square, ( P – x )(Lecat at 341.42 K).…”

Section: Results and Discussionmentioning

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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“…or empirical correlations were chosen carefully by thorough studies of literature (Ambrose and Ghiasse, 1987;ASME Steam Tables, 1993;Daubert and Danner, 1992;Garriza et al, 2002;Hansch and Leo, 1979;Harvey and Lemon, 2004;Reid et al 1987;Rodriguez et al 1993;Tsonopoulos, 1974). p of hexane and butanol were calculated from the temperature dependent correlation by Daubert and Danner (1992), and of water from the ASME Tables (1993) …”

Section: Water -Butanolmentioning

confidence: 99%

Universal liquid mixture model for vapor-liquid and liquid-liquid equilibria in hexane-butanol-water system over the temperature range 10 - 100 °C

Islam¹,

Kabadi²

2011

Chemical and Process Engineering

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This is an extended research of the paper conducted to obtain a universal set of interaction parameters of the model NRTL over the temperature range 10 -100 °C for hexanebutanol-water system; meaning for binary pairs hexane-butanol, butanol-water and hexane-water; and for ternary system hexane-butanol-water. Thorough investigations of data selections for all binary pairs (Vapor-Liquid Equilibrium (VLE), Liquid-Liquid Equilibrium (LLE)), infinite dilution activity coefficient (γ ∞ ), infinite dilution distribution coefficient (D sw ), excess enthalpy (H E ), and for ternary system (LLE of hexane-butanol-water) were carried out. Finally quadratic temperature dependent interaction parameters were estimated regressing all the mentioned data and in each case calculated results were compared with literature values. The comparisons showed an overall percentage of error within 15% for the mentioned phase equilibrium calculations.

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Vapor pressures of binary mixtures of hexane + 1-butanol, + 2-butanol, + 2-methyl-1-propanol, or +2-methyl-2-propanol at 298.15 K

Cited by 34 publications

References 5 publications

(Vapour+liquid) equilibrium and excess Gibbs functions of ternary mixtures containing 1-butanol or 2-butanol, n-hexane, and 1-chlorobutane at T=298.15K

(Vapour+liquid) equilibrium and excess Gibbs functions of ternary mixtures containing 1-butanol or 2-butanol, n-hexane, and 1-chlorobutane at T=298.15K

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

Universal liquid mixture model for vapor-liquid and liquid-liquid equilibria in hexane-butanol-water system over the temperature range 10 - 100 °C

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