Vapour-liquid equilibrium in strongly associated systems. The systems acetic acid-propionic acid and acetic acid-trifluoroacetic acid

1986 ◽  
Vol 51 (1) ◽  
pp. 194-205 ◽  
Author(s):  
Ivona Malijevská ◽  
Marie Sýsová ◽  
Dagmar Vlčková
Keyword(s):  
Acetic Acid ◽  
Propionic Acid ◽  
Trifluoroacetic Acid ◽  
Normal Pressure ◽  
Vapour Phase ◽  
Liquid Equilibrium ◽  
Correct Expression

Vapour-liquid equilibrium was measured in the systems acetic acid-propionic acid and acetic acid-trifluoroacetic acid at normal pressure. Special emphasis has been laid on the correct expression of the P-V-T behaviour in the vapour phase and the analysis of the data obtained.

Vapour-liquid equilibrium in strongly associated systems. The propionic acid-n-heptane system

1985 ◽  
Vol 50 (10) ◽  
pp. 2101-2110 ◽  
Author(s):  
Ivona Malijevská ◽  
Dagmar Vlčková
Keyword(s):  
Propionic Acid ◽  
Normal Pressure ◽  
Vapour Phase ◽  
Liquid Equilibrium ◽  
Correct Expression

Vapour-liquid equilibrium in the propionic acid-n-heptane system was measured at normal pressure. When treating the data, emphasis was laid on the correct expression of volumetric behaviour in the vapour phase and the analysis of the data obtained.

Vapour-liquid equilibrium in the benzene(1)-propionic acid(2)-acetic acid(3) ternary system

1986 ◽  
Vol 51 (12) ◽  
pp. 2665-2674 ◽  
Author(s):  
Ivona Malijevská ◽  
Helena Perničková ◽  
Karel Ledvinka ◽  
Bohuslav Doležal
Keyword(s):  
Acetic Acid ◽  
Ternary System ◽  
Propionic Acid ◽  
Activity Coefficients ◽  
Error Propagation ◽  
Binary Data ◽  
Normal Pressure ◽  
Wilson Equation ◽  
Liquid Equilibrium ◽  
Experimental Values

Results of measurement of vapour-liquid equilibria in the benzene-propionic acid-acetic acid ternary system at normal pressure are presented. The activity coefficients were, within the framework of inaccuracies determined on the basis of the law of error propagation, subjected to a test of consistency and correlated by the Wilson equation. The experimental values of activity coefficients are compared with the values calculated on the basis of the Wilson equation with its constants obtained both from the ternary and from the binary data and with the values estimated by the UNIFAC method.

Vapour-liquid equilibrium in the ternary system cyclohexane-acetic acid-propionic acid

1989 ◽  
Vol 54 (11) ◽  
pp. 2840-2847 ◽  
Author(s):  
Ivona Malijevská ◽  
Alena Maštalková ◽  
Marie Sýsová
Keyword(s):  
Acetic Acid ◽  
Ternary System ◽  
Propionic Acid ◽  
Activity Coefficients ◽  
Error Propagation ◽  
Analytical Techniques ◽  
Liquid Equilibrium ◽  
Consistency Test ◽  
Propagation Law ◽  
Equilibrium Data

Isobaric equilibrium data (P = 101.3 kPa) for the system cyclohexane-acetic acid-propionic acid have been measured by two different analytical techniques. Activity coefficients calculated by simultaneous solving of equations for the chemical and phase equilibria were subjected to a consistency test based on inaccuracies determined from the error propagation law, and were correlated by Wilson’s equation. The activity coefficients measured were compared with those calculated from binary vapour-liquid equilibrium data and with values predicted by the UNIFAC method.

Pycnometric determination of densities and excess volumes of binary mixtures containing at least one associating component

1990 ◽  
Vol 55 (10) ◽  
pp. 2395-2403 ◽  
Author(s):  
Kamila Chýlková ◽  
Ivona Malijevská
Keyword(s):  
Acetic Acid ◽  
Propionic Acid ◽  
Binary Mixtures ◽  
Trifluoroacetic Acid ◽  
Excess Volume ◽  
Excess Volumes ◽  
Molar Excess ◽  
Molar Excess Volumes

Densities at 20 °C and molar excess volumes calculated from them are reported in the work for the mixtures of the substances: propionic acid-n-heptane, propionic acid-benzene, trifluoroacetic acid-benzene, propionic acid-cyclohexane, acetic acid-cyclohexane, acetic acid-trifluoroacetic acid, acetic acid-propionic acid, and propionic acid-trifluoroacetic acid. For the last system mentioned, a strange dependence of excess volume on composition was found which is noted for three local extremes. The dependences of excess volume on composition are correlated by the Redlich-Kister polynomial.

Vapour-phase hetero-association of trifluoroacetic acid with acetic acid

1966 ◽  
pp. 293 ◽  
Author(s):  
Chii Ling ◽  
Sherril D. Christian ◽  
Harold E. Affsprung ◽  
Robert W. Gray
Keyword(s):  
Acetic Acid ◽  
Trifluoroacetic Acid ◽  
Vapour Phase

scholarly journals Carboxylic acid recovery from Fischer–Tropsch aqueous product by fractional freezing

2020 ◽  
Vol 10 (3) ◽  
pp. 149-156
Author(s):  
Nuvaid Ahad ◽  
Arno de Klerk
Keyword(s):  
Acetic Acid ◽  
Liquid Phase ◽  
Carboxylic Acid ◽  
Carboxylic Acids ◽  
Propionic Acid ◽  
Butyric Acid ◽  
Acid Water ◽  
Liquid Equilibrium ◽  
Fischer Tropsch ◽  
Solid Liquid

Abstract About half of the product from iron-based high-temperature Fischer–Tropsch synthesis is an aqueous product containing dissolved oxygenates. Volatile oxygenates can be recovered by distillation, but the bulk of the carboxylic acids remain in the water, which is called acid water. Fractional freezing was explored as a process for producing a more concentrated carboxylic acid solution from which the carboxylic acids could be recovered as petrochemical products, while concomitantly producing a cleaner wastewater. Solid–liquid equilibrium data were collected for aqueous solutions of acetic acid, propionic acid, and butyric acid. A synthetic Fischer–Tropsch acid water mixture (0.70 wt% acetic acid, 0.15 wt% propionic acid, and 0.15 wt% butyric acid) was prepared and the liquid phase concentrations of the acid species at solid–liquid equilibrium were determined. Control experiments with material balance closure on each of the carboxylic acid species were performed at selected conditions. Having more than one carboxylic acid species present in the mixture meaningfully changed the solid–liquid equilibrium versus temperature of the system. The carboxylic acids partitioned between the solid phase and the liquid phase and a practical design would require multiple duty-controlled solid–liquid equilibrium stages, with most of the separation taking place in the temperature range 0 to − 5 °C.

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