Flüssigkeit‐Dampf‐Gleichgewichte in binären Systemen von Kohlenwasserstoffen verschiedenen Typs

Sieg, L.

doi:10.1002/cite.330221503

Cited by 85 publications

(24 citation statements)

References 15 publications

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“…The pressure versus composition of both phases is plotted in Fig. 1 where it is shown that this binary system exhibits an ideal behavior, which is in agreement with other data published in the literature at different conditions [26,27]. Concerning the ternary system measured, {1-pentanol (1) + 2,2,4-trimethylpentane (2) + heptane (3)}, as the Margules equation cannot be extended directly to ternary mixtures, the Wohl's expansion was used.…”

Section: Discussionsupporting

confidence: 87%

Vapour–liquid equilibria of the ternary mixture (1-pentanol+2,2,4-trimethylpentane+heptane) and the binary mixture (2,2,4-trimethylpentane+heptane) at T=313.15K for the characterization of second generation biofuels

Moreau

Segovia

Villamañán

et al. 2015

Fluid Phase Equilibria

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Section: Discussionsupporting

confidence: 87%

Vapour–liquid equilibria of the ternary mixture (1-pentanol+2,2,4-trimethylpentane+heptane) and the binary mixture (2,2,4-trimethylpentane+heptane) at T=313.15K for the characterization of second generation biofuels

Moreau

Segovia

Villamañán

et al. 2015

Fluid Phase Equilibria

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“…a&, replaces aiw,. of mercury are available for the binary systems n-heptane-cyclohexane (36,59). For calculating vapor-liquid equilibria the vapor pressures were calculated from the constants and equations in Table 11.…”

Section: Applicationsmentioning

confidence: 99%

“…The approximate effect of temperature on the systems n-heptane-toluene and cyclohexane-toluene has been estimated based on the system n-heptane-benzene, for which data are available (8,53,59) at several temperatures. With the aid of this temperature effect, coefficients for the binaries n-heptane-toluene and cyclohexane-toluene have been estimated at 90' and 105' C. Although the sign convention is satisfied, the absolute values are not in sufficient agreement with Equation 6.…”

Section: Applicationsmentioning

confidence: 99%

“…51 Binary data for n-heptane-benzene (8, 53, 59), n-hexane-benzene (62), methylcyclopentane-benzene (26), cyclohexane-benzene (28,49,52,67), and n-heptane-cyclohexane (36) form the basis for the coefficients in the eight-component equations. Only 14 points for heptane, 18 points for cyclohexane, and six points for toluene deviate 3% or more from the experimental data.…”

Section: Applicationsmentioning

confidence: 99%

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Multicomponent Vapor-Liquid Equilibria from Binary Data

Black¹

1959

Ind. Eng. Chem.

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A D v m T A m s of calculating vaporliquid equilibria in multicomponent systems from data for the pure components and individual binaries are obvious. The relative simplicity of the experimental determination of binary data as contrasted to multicomponent data is a basic advantage. The main value of the calculation method is lost if the data required for its application become excessive or too difficult to obtain.Several types of binary data conveniently furnish activity coefficients and in some cases provide a double check on the data and their thermodynamic consistency. Such binary data are already available for many systems. They are becoming more and more available from measurements of total pressures, boiling points, azeotropic data, relative volatilities, and complete vapor-liquid equilibria. Their efficient use in calculating multicomponent systems is of prime importance.Several methods have been reported for calculating vapor-liquid equilibria. Usually vapor-liquid equilibria are calculated by liquid phase activity coefficients. The Margules (3, 7.9,22,34,45,47,57,69) and van Laar-type (4, 6 , 74, 79, 63-65, 67, 69) equations have frequently been applied to representation of the activity coefficients as a function of composition. Another method uses equations relating directly to liquid composition and relative volatilities, or vapor compositions (72, 73,23,38, 46,60).The objective of this article is to show further application of the modified van Laar-type equations ( 6 ) to the calculation of multicomponent vapor-liquid equilibria based only on data for the pure components and their binary mixtures. Phase EquilibriaComplete vapor-liquid equilibria in terms of the liquid, x,, the vapor composition, Y,, the total pressure, P, and the temperature, T , provide more than the minimum data required for a check of the thermodynamic consistency. The pressure-temperature relationship a t liquid composition x , and the vapor composition, Y,, at the corresponding x , and T . or P, provides a double check on the consistency of the data. The two are related through the activity coefficient, yt, according toand at, = r t P W r t P P 9 , = Y,x,/x,Y, (2) A method for calculating the imperfection-pressure coefficients, 0, has been described (5). For a nonpolar substance the only basic data needed are critical temperature, T,, critical pressure, P,, and vapor pressure, Po. For a polar substance a minimum of one individual constant is also required. A vapor density a t one or two temperatures can furnish the required individual constants for each polar substance. Except where special "chemical" effects are present, no binary coefficients are required to represent the imperfection-pressure coefficients for the components in the mixtures.The activity coefficients, y's, are functions of temperature and liquid compositions, 2's. While in many systems the qualitative effect of temperature on the activity coefficients is known, exact quantitative values are best derived empirically from data at more than one temperature. For ...

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“…In Table , we listed the experimental data (LLE and VLE) of binary systems available in literature. ,,,,,, Antoine parameters of {water + MEG} systems, obtained from our previous work, are reported in Table . All these data were correlated using the NRTL activity coefficient model with temperature-dependent parameter: C ij 0 and C ij T are the binary parameters of NRTL model.…”

Section: Results: Data Correlation and Prediction By Nrtlmentioning

confidence: 99%

Liquid–Liquid Equilibria of Binary, Ternary, and Quaternary Systems Involving Monoethylene Glycol, Water, Toluene, p-Xylene, Hexane, and Octane

et al. 2017

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To prevent gas hydrate formation and the plugging of the pipe, monoethylene glycol, MEG, is injected into the wellhead. To develop the thermodynamic model for the optimization of MEG injection, liquid−liquid equilibrium, LLE, studies are necessary. In the present work, original data are presented of binary, ternary, and quaternary systems involving MEG, water, hexane, octane, toluene, and p-xylene under atmospheric pressure and in the temperature range between 278.15 and 333.15 K. The NRTL thermodynamic model was used for the solubility prediction of binary, ternary, and quaternary systems. The adjustable parameters of the model were determined through regression of binary mixtures data from literature. Experimental and predicted solubilities are in a quite good agreement, in view of the low solubility data involved in the different systems.

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Flüssigkeit‐Dampf‐Gleichgewichte in binären Systemen von Kohlenwasserstoffen verschiedenen Typs

Abstract: Im Folgenden werden besonders sorgfältige Gleichgewichtsmessungen an 15 binären Systemen von Kohlenwasserstoffen mitgeteilt.

Cited by 85 publications

References 15 publications

Vapour–liquid equilibria of the ternary mixture (1-pentanol+2,2,4-trimethylpentane+heptane) and the binary mixture (2,2,4-trimethylpentane+heptane) at T=313.15K for the characterization of second generation biofuels

Vapour–liquid equilibria of the ternary mixture (1-pentanol+2,2,4-trimethylpentane+heptane) and the binary mixture (2,2,4-trimethylpentane+heptane) at T=313.15K for the characterization of second generation biofuels

Multicomponent Vapor-Liquid Equilibria from Binary Data

Liquid–Liquid Equilibria of Binary, Ternary, and Quaternary Systems Involving Monoethylene Glycol, Water, Toluene, p-Xylene, Hexane, and Octane

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