Abstract
Correlation equations for expressing the boiling temperature as direct function of liquid composition have been tested successfully and applied for predicting azeotropic behavior of multicomponent mixtures and the kind of azeotrope (minimum, maximum and saddle type) using modified correlation of Gibbs-Konovalov theorem. Also, the binary and ternary azeotropic point have been detected experimentally using graphical determination on the basis of experimental binary and ternary vapor-liquid equilibrium data.
In this study, isobaric vapor-liquid equilibrium for two ternary systems: “1-Propanol – Hexane – Benzene” and its binaries “1-Propanol – Hexane, Hexane – Benzene and 1-Propanol – Benzene” and the other ternary system is “Toluene – Cyclohexane – iso-Octane (2,2,4-Trimethyl-Pentane)” and its binaries “Toluene – Cyclohexane, Cyclohexane – iso-Octane and Toluene – iso-Octane” have been measured at 101.325 KPa. The measurements were made in recirculating equilibrium still with circulation of both the vapor and liquid phases. The ternary system “1-Propanol – Hexane – Benzene” which contains polar compound (1-Propanol) and the two binary systems “1-Propanol – Hexane and 1-Propanol – Benzene” form a minimum azeotrope, the other ternary system and the other binary systems do not form azeotrope.
All the data passed successfully the test for thermodynamic consistency using McDermott-Ellis test method (McDermott and Ellis, 1965).
The maximum likelihood principle is developed for the determination of correlations parameters from binary and ternary vapor-liquid experimental data which provides a mathematical and computational guarantee of global optimality in parameters estimation for the case where all the measured variables are subject to errors and the non ideality of both vapor and liquid phases for the experimental data for the ternary and binary systems have been accounted.
The agreement between prediction and experimental data is good. The exact value should be determined experimentally by exploring the concentration region indicated by the computed values.
References
Hala, E., Pick, J., Fried, V., and Vilim O., “Vapor-Liquid Equilibrium”, 2nd ed., Pergamon press, London, 1968.
Harold, R. N., “Phase Equilibrium in Process Design”, Wiley-Interscience Publisher, New York, 1970.
Hirata, M., Hoen, S., and Nagahama, K., “Computer Aided Data Book of Vapor-Liquid Equilibria”, Kodansha Limited, Tokyo, 1975.
Hoffman, E. J., “Azeotropic and Extractive Distillation”, Interscience Publisher, New York, 1964.
Malesinski, W., “Azeotropy and other Theoretical Problems of Vapor-Liquid Equilibrium”, Interscience, PWN, New York, 1965.
Marc, J. A., Martin, J. P. and Thamas, F. T., “Thermophysical Properties of Fluid, An introduction to their prediction”, Imperial College Press, first reprint, 1998.
McDermott, C., Ellis, S. R. M., “A Multicomponent Consistency Test”, Chem. Eng. Sci., 20, 293, 1965.
Ohe, S., “Vapor-Liquid Equilibria Data Book”, Elsevier Scientific Publishing Company, Netherlands, 1989.
Walas, S. M., “Phase Equilibria in Chemical Engineering”, Butterworth Publishers, London, 1985.
Copyright: Open Access authors retain the copyrights of their papers, and all open access articles are distributed under the terms of the Creative Commons Attribution License, which permits unrestricted use, distribution and reproduction in any medium, provided that the original work is properly cited. The use of general descriptive names, trade names, trademarks, and so forth in this publication, even if not specifically identified, does not imply that these names are not protected by the relevant laws and regulations. While the advice and information in this journal are believed to be true and accurate on the date of its going to press, neither the authors, the editors, nor the publisher can accept any legal responsibility for any errors or omissions that may be made. The publisher makes no warranty, express or implied, with respect to the material contained herein.