Infinite dilution activity coefficients of ethanol-n-alkanes mixtures

Cori, Laura; Delogu, Pietro

doi:10.1016/0378-3812(86)87044-3

Cited by 21 publications

(6 citation statements)

References 10 publications

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“…In comparison to the activity coefficients for n-alkanes in LDPE, the activity coefficients for n-alkanes in ethanol are greater than 1 and also increase with molecular weight. Data from Cori and Delogu (1986) shows that the activity coefficients of n-alkanes in ethanol increase with molecular weight. The regular solution correctly predicts this behavior with activity coefficients of 2.1 for C12 and 4.8 for C22 using Hoy's dispersive solubility parameters.…”

Section: Calculationsmentioning

confidence: 99%

Prediction of solute partition coefficients between polyolefins and alcohols using the regular solution theory and group contribution methods

Baner¹,

Piringer²

1991

Ind. Eng. Chem. Res.

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Section: Calculationsmentioning

confidence: 99%

Prediction of solute partition coefficients between polyolefins and alcohols using the regular solution theory and group contribution methods

Baner¹,

Piringer²

1991

Ind. Eng. Chem. Res.

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“…(b) Ethanol (1) + n -octane (2). ln γ 1 ∞ : this work (expt (●), model (eq ) ()); Cori and Delogu . (red ●); Vrbk et al (black ○).…”

Section: Results and Discussionmentioning

confidence: 91%

Infinite Dilution Activity Coefficients for Systems of C2–C4 n-Alcohols in the Range of T = (303.15 to 343.15) K

Moodley

Raal

2020

J. Chem. Eng. Data

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In this work vapor pressures and activity coefficients at infinite dilution (γ i ∞) were measured using a newly commissioned ebulliometer (a noninvasive phase equilibrium measurement device), that has been modified with the view to improve the precision and measurement time of the apparatus, as well as the effects of superheating. The systems considered were C2–C4 n-alcohols with three different classes of solvents (ester, n-alkane, ketone), namely, (ethanol/propan-1-ol/butan-1-ol) + (ethyl acetate, n-octane, butan-2-one). The temperature range considered was T = (303.15 to 343.15) K, which corresponded to subatmospheric conditions. The γ i ∞ data were correlated empirically for temperature using standard procedures. A portion of the γ i ∞ data measured are available in the literature and compared well with an acceptable correlation for this type of data, for the majority of the systems considered. The data were also compared to extrapolations of γ i ∞ from reliable vapor–liquid equilibrium data. Vapor–liquid equilibrium predictions were also made from the limiting activity coefficients and established that the presence of azeotropes and their temperature dependence were correlated from the measured γ i ∞.

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“…The pure-group energy parameters of ethanol were determined by fitting vapor pressure data of pure ethanol. The GCA–EoS equation was able to reproduce the vapor pressures of this compound with an average deviation of 0.38% in the range of temperatures 290–510 K. The binary interaction parameters between ethanol (CH 3 CH 2 OH) and paraffin groups (CH 3 /CH 2 ) were obtained by fitting experimental vapor–liquid equilibrium data of ethanol–alkanes (pentane, hexane, heptane, octane) at temperatures between 293 and 318 K and pressures between 0.06 and 0.7 bar , and infinite dilution activity coefficients (γ ∞ ) of ethanol + alkanes (pentane, hexane, heptane, octane) at temperatures between 283–354 K and atmospheric pressure …”

Section: Thermodynamic Modeling Sectionmentioning

confidence: 99%

“…The binary interaction parameters between ethanol (CH 3 CH 2 OH) and paraffin groups (CH 2 ) were obtained by fitting experimental vapor–liquid equilibrium data of ethanol–alkanes (pentane, hexane, heptane, octane, isooctane) in the range 293–318 K and 0.06 and 0.7 bar , and infinite dilution activity coefficients (γ ∞ ) of ethanol + alkanes (pentane, hexane, heptane, octane) at temperatures between 283–354 K …”

Section: Thermodynamic Modeling Sectionmentioning

confidence: 99%

Liquid–Liquid Equilibria in Ternary Mixtures of Methyl Oleate + Ethanol + Glycerol at Atmospheric Pressure

Andreatta

2012

Ind. Eng. Chem. Res.

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The knowledge and the ability to describe the phase equilibrium behavior of systems composed of transesterification products are very important in the optimization of biodiesel production and purification process. In this work, liquid−liquid equilibrium data have been measured for the ternary system methyl oleate + ethanol + glycerol, at temperatures between 303 and 333 K. This system has not been explored before. The experimental data measured were compared with analogous ternary systems showing an increasing of the solubility regarding the systems containing methanol. The isothermal experimental data have shown a good linear fit in an Othmer−Tobias plot. The group contribution with association GCA−EoS equation of state and the A-UNIFAC model were applied to represent the phase equilibria of this ternary system. The GCA−EoS model in particular, has shown a good predictive capability.

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Infinite dilution activity coefficients of ethanol-n-alkanes mixtures

Cited by 21 publications

References 10 publications

Prediction of solute partition coefficients between polyolefins and alcohols using the regular solution theory and group contribution methods

Prediction of solute partition coefficients between polyolefins and alcohols using the regular solution theory and group contribution methods

Infinite Dilution Activity Coefficients for Systems of C2–C4 n-Alcohols in the Range of T = (303.15 to 343.15) K

Liquid–Liquid Equilibria in Ternary Mixtures of Methyl Oleate + Ethanol + Glycerol at Atmospheric Pressure

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