Selecting extracting agents for separation of biazeotropic binary mixtures by extractive distillation

Серафимов, Л. А.; Фролкова, А. К.; Chelyuskina, T. V.

doi:10.1134/s0040579509060062

Cited by 12 publications

(7 citation statements)

References 2 publications

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“…Then, the coefficient of the relative volatility of the pseudo binary mixture will be calculated as follows: (13) where and are the relative total concentration of components 1 and 2 in the liquid phase. Based on the above constructed model for describing the liquidliquid-vapor phase equilibrium in benzene-hep tane-SA systems, we calculated the values of the com positions of the equilibrium vapor over the entire range Table 7.…”

Section: Design Of Relative Volatility Lines Equal To 1 (Line = 1) Inmentioning

confidence: 99%

“…The first group is based on the works of tech nological character on the optimization of operating conditions and apparatus design of extractive distilla tion processes [5][6][7]. The second group includes research works related to the study of phase equilibria, mixing heats, and the interaction mechanisms of the separating agent with the components of separat ing mixtures in order to select the most effective SA [8][9][10][11][12][13][14].…”

Section: Introductionmentioning

confidence: 99%

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Vapor-liquid-liquid phase equilibrium in four-component benzene-heptane-N-methylpyrrolidone-sulfolane system

Иванов

Lotkhov

Tikhonov

et al. 2015

Theor Found Chem Eng

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The liquid-vapor phase equilibrium in four component benzene-heptane-N methylpyrroli done-sulfolane system has been experimentally studied, including in the areas of lamination of the liquid phase. The modeling of liquid-liquid-vapor phase equilibrium in the studied system has been performed using a calculation program compiled based on the nonrandom two liquid (NRTL) equation. A comparative assessment of the effectiveness of N methylpyrrolidone, sulfolane, and their mixture as separating agents in the of extractive distillation of benzene-heptane binary mixture has been performed.

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Section: Design Of Relative Volatility Lines Equal To 1 (Line = 1) Inmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

Vapor-liquid-liquid phase equilibrium in four-component benzene-heptane-N-methylpyrrolidone-sulfolane system

Иванов

Lotkhov

Tikhonov

et al. 2015

Theor Found Chem Eng

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“…Serafimov et al presented basic diagram structures for extractive distil lation systems with the aid of analyzing relative volatil ity α = 1 lines and pseudo ideal lines is for the case in which the mixture to be separated is biazeotropic. [35] Recently, based on the achievement of Serafimov's [30] group in topological theory on ternary system [36][37][38], Rodriguez Donis et al [8] studied how univolatility lines split the composition triangle into regions of cer tain order of volatility of components and defined a general feasibility criterion for extractive distillation under infinite reflux ratio. In this work we consider unidistribution and univolatility line diagrams for the purpose of sketching the volatility order region and thus of assessing the feasible structures which will give possible products and offer information of possible limitation of entrainer feed.…”

Section: Unidistribution and Relative Volatilitymentioning

confidence: 99%

A Review of Ternary Azeotropic Mixtures Advanced Separation Strategies

Shen¹,

Benyounes²,

Song³

2016

Теор. основы хим. технол.

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In most multi component systems, the predominant non ideality occurs which lead to the occur rence of an azeotrope. The ternary systems classification and study are summarized in first part of this review. The next part covers thermodynamic knowledge of residue curve maps, univolatility and unidistribution curves. A feasibility criterion based on thermodynamic properties of ternary diagram is presented, they are considered as powerful tool for the flow sheet development and conceptual design. Separation of azeotropic mixtures and close boiling mixtures require non conventional distillation processes, among which the lead ing processes are pressure swing distillation if the composition of the azeotrope changes significantly with pressure, azeotropic distillation, extractive distillation, reactive distillation, and salt effect distillation. The final section provides an overview of concepts, history, and recent strategies in these non conventional distil lations.

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“…The latter is the ratio of the number of moles of the dissolved compo nent to the mass of the solvent (kg) under equilibrium conditions. The empirical method initially suggested by Buchowski et al [9] is a correlation of solubility using the δh (Buchowski-Ksiazczak) equation: (1) where the solubility x is expressed in terms of mole fractions and is a function of temperature T, T m is the melting point of the solute, and δ and h are two adjust able parameters derived from solubility data.…”

Section: Introductionmentioning

confidence: 99%

“…Phase equilibrium thermodenamics is the theoret ical basis for designing separation processes, including distillation [1,2]. One of the industrial purification methods for the production of high purity materials is crystallization.…”

Section: Introductionmentioning

confidence: 99%