A Unified Thermodynamics Model for Solid–Liquid Equilibrium, Liquid–Liquid Equilibrium, and Vapor–Liquid Equilibrium of Cyclohexane Oxidation Systems: NRTL Model

This work deals with the study of thermodynamical models for the solid-liquid equilibrium (SLE) and comparing its performance with experimental data. The xylose solubility in the xylose-water and xylose-water-ethanol systems has been measured using a variant of the isothermal method. A total of 12 experiments were performed in a 100 mL glass jacketed crystallizer with helix-type agitator by changing the temperature from 0 to 60°C. The solution was mixed during 72 h with an IKA Labortechnic, RW 20.n agitator at 450 rpm. Later, the experimental and reported results were fitted using the prediction models based on the vapor-liquid-equilibrium (UNIFAC (Universal Functional Activity Coefficient), ASOG (Analytical Solutions of Groups) and GSP (Group Solubility Parameter); semi-empirical models based on the vapor-liquid-equilibrium (VLE) (UNIQUAC (Universal Quasi Chemical), Wilson and NRTL (Non Randon Two Liquid)) on the solid-liquid-equilibrium, and empirical model with fitted parameters (Nývlt, λh, Margules with 1 and 2 parameters). The results showed that the UNIQUAC model with fitted parameters can describe the SLE with reasonable accuracy (1.28 and 3.36% for binary and ternary systems, respectively). The average deviation was the arithmetic mean of the deviations. On the other hand, the other methods resulted in poor agreement with the system’s behavior presenting systematic deviations from the experimental data.

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Investigation of the (Solid−Liquid and Vapor−Liquid) Equilibrium of the System H2O + CH3OH + Na2SO4

Industrial & Engineering Chemistry Research ◽

10.1021/ie0508177 ◽

2006 ◽

Vol 45 (1) ◽

pp. 454-466 ◽

Cited By ~ 2

Author(s):

Álvaro Pérez-Salado Kamps ◽

Mathias Vogt ◽

Michael Jödecke ◽

Gerd Maurer

Keyword(s):

Liquid Equilibrium ◽

Vapor Liquid Equilibrium ◽

Solid Liquid ◽

Vapor Liquid

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PREDICTION OF SOLID-LIQUID EQUILIBRIA FROM VAPOR-LIQUID EQUILIBRIUM DATA USING THE SOLUTION OF GROUPS MODEL

JOURNAL OF CHEMICAL ENGINEERING OF JAPAN ◽

10.1252/jcej.12.81 ◽

1979 ◽

Vol 12 (2) ◽

pp. 81-85 ◽

Cited By ~ 5

Author(s):

YOSHIKI UNNO ◽

DAISUKE HOSHINO ◽

KUNIO NAGAHAMA ◽

MITSUHO HIRATA

Keyword(s):

Liquid Equilibrium ◽

Vapor Liquid Equilibrium ◽

Equilibrium Data ◽

Solid Liquid ◽

Vapor Liquid

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Evaluation of the possibility of separating commercial phenol from the phenolic fraction of coal tar

E3S Web of Conferences ◽

10.1051/e3sconf/202126602011 ◽

2021 ◽

Vol 266 ◽

pp. 02011

Author(s):

Y.O. Schastnyy ◽

N.A. Romanova ◽

R.R. Gizatullin

Keyword(s):

Coal Tar ◽

Component Composition ◽

Technological Scheme ◽

Technological Parameters ◽

Liquid Equilibrium ◽

Phenolic Fraction ◽

Vapor Liquid Equilibrium ◽

Nrtl Model ◽

Azeotropic Mixtures ◽

Vapor Liquid

This article is about the possibility of concentrating commercial coal phenol with a concentration of 99% by the weight method of rectification from the phenolic fraction of coal tar. The sufficiency of phenol is ensured by the kumol method, however, the consumption of phenol increases. Modeling of the vapor-liquid equilibrium of double and triple mixtures of components using the NRTL model showed the presence of the following positive homogeneous azeotropic mixtures: phenol-indane, phenol-indene. Modeling of the vapor-liquid equilibrium of double and triple mixtures of components using the NRTL model showed the presence of the following positive homogeneous azeotropic mixtures: phenol-indane, phenol-indene. The compositions and temperatures of these azeotropes are determined. The authors propose the isolation of phenol from the fraction and its purification from indane and indene by a clear rectification method. The technological scheme consisting of four devices is based on the analysis of the component composition of the initial mixture and the existing azeotropes. Modeling of the technological scheme showed that this scheme provides the release of phenol by 99% of the mass, which meets the requirements for coal phenol. After optimizing the technological parameters of the distillation columns, the estimated extraction costs will amount to 5.64 Gcal per ton of commercial phenol.

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