Isobaric vapor-liquid equilibrium for ternary system of ethanol, ethyl propionate and para-xylene at 101.3 kPa

doi:10.1016/j.cjche.2017.10.020

Abstract

Abstract: Isobaric vapor-liquid equilibrium (VLE) data for the binary system ethyl propionate (2) + para-xylene (3) and ternary system ethanol (1) + ethyl propionate (2) + para-xylene (2) at atmospheric pressure (101.3 kPa) were obtained by a VLE modified othmer still. All the experimental data passed a point to point consistency test of Van Ness method, which verified the data reliability. The Wilson and UNIQUAC activity coefficient models were employed to correlate the binary VLE data to obtain binary interaction parameters. Based on binary interaction parameters, ternary VLE data of ethanol (1) + ethyl propionate (2) + para-xylene (3) were predicted by Wilson and UNIQUAC models, which proved that predicted values are consistent with the experimental data. Furthermore, azeotropic phenomenon between ethanol and ethyl propionate disappears when the mole ratio of para-xylene and binary system of ethanol and ethyl propionate is 1:1. Therefore, this paper convinced that para-xylene is a proper extractive additive that could be used in extractive distillation to separate the binary azeotropic system of ethanol and ethyl propionate.

Key words: Vapor-liquid equilibrium, Azeotrope, Ethanol, Ethyl propionate, Para-xylene

摘要： Isobaric vapor-liquid equilibrium (VLE) data for the binary system ethyl propionate (2) + para-xylene (3) and ternary system ethanol (1) + ethyl propionate (2) + para-xylene (2) at atmospheric pressure (101.3 kPa) were obtained by a VLE modified othmer still. All the experimental data passed a point to point consistency test of Van Ness method, which verified the data reliability. The Wilson and UNIQUAC activity coefficient models were employed to correlate the binary VLE data to obtain binary interaction parameters. Based on binary interaction parameters, ternary VLE data of ethanol (1) + ethyl propionate (2) + para-xylene (3) were predicted by Wilson and UNIQUAC models, which proved that predicted values are consistent with the experimental data. Furthermore, azeotropic phenomenon between ethanol and ethyl propionate disappears when the mole ratio of para-xylene and binary system of ethanol and ethyl propionate is 1:1. Therefore, this paper convinced that para-xylene is a proper extractive additive that could be used in extractive distillation to separate the binary azeotropic system of ethanol and ethyl propionate.

关键词: Vapor-liquid equilibrium, Azeotrope, Ethanol, Ethyl propionate, Para-xylene

Zhongpeng Xing, Yujie Gao, Hui Ding, Xianqin Wang, Lujun Li, Hang Zhou. Isobaric vapor-liquid equilibrium for ternary system of ethanol, ethyl propionate and para-xylene at 101.3 kPa[J]. Chin.J.Chem.Eng., 2018, 26(3): 560-565.

References

[1] D.C. Rennard, P.J. Dauenhauer, S.A. Tupy, L.D. Schmidt, Autothermal catalytic partial oxidation of bio-oil functional groups:esters and acids, Energy Fuels 22(2) (2008) 1318-1327.

[2] S.S. Kanwar, H.K. Verma, R.K. Kaushal, R. Gupta, S.S. Chimni, Y. Kumar, Effect of solvents and kinetic parameters on synthesis of ethyl propionate catalysed by poly (AAc-co-HPMA-cl-MBAm)-matrix-immobilized lipase of Pseudomonas aeruginosa BTS-2, World J. Microbiol. Biotechnol. 21(6-7) (2005) 1037-1044.

[3] S.J. Lin, Y.Z. Sun, Catalytic synthesis of ethyl propionate with p-toluene sulfonic acid, J. Beijing Inst. Petrochem. Technol. 13(1) (2005) 49-52(in Chinese).

[4] J. Ortega, J. Ocon, J. Pena, C.D. Alfonso, M. Paz-Andrade, J. Fernandez, Vapor-liquid equilibrium of the binary mixtures CnH2n +1(OH)(n=2, 3, 4) + propyl ethanoate and + ethyl propanoate, Can. J. Chem. Eng. 65(1987) 982-990.

[5] W.F. Shen, H. Benyounes, V. Gerbaud, Extractive distillation:recent advances in operation strategies, Rev. Chem. Eng. 31(1) (2015) 13-26.

[6] Z.Y. Zhu, Y.S. Ri, M. Li, H. Jia, Y.K. Wang, Extractive distillation for ethanol dehydration using imidazolium-based ionic liquids as solvents, Chem. Eng. Process. 109(2016) 190-198.

[7] Y. Xiao, P. Bai, Z.K. Jiang, Vapour-liquid equilibrium for systems containing ionic liquids, Asian J. Chem. 24(9) (2012) 3775-3780.

[8] H. Ding, Y.J. Gao, J.Q. Li, H. Zhou, S.J. Liu, X. Han, Vapor-liquid equilibria for ternary mixtures of isopropyl alcohol, isopropyl acetate, and DMSO at 101.3 kPa, J. Chem. Eng. Data 61(9) (2017) 3013-3019.

[9] Q.Y. Wang, B.R. Yu, C.J. Xu, Design and control of distillation system for methylal/methanol separation. Part 1:extractive distillation using dmf as an entrainer, Ind. Eng. Chem. Res. 51(3) (2012) 1281-1292.

[10] H. Zhou, H. Ding, J.B. Quan, Extractive distillation of ethanol-ethyl propionate azeotrope with para-xylene, Chem. Ind. Eng. 34(2017) 25-34(in Chinese).

[11] K. Xu, Handbook of Fine Organic Chemical Raw Materials and Intermediates, Chemical Industry Press, Beijing, 199834-36(in Chinese).

[12] M. Corbetta, C. Pirola, F. Galli, F. Manenti, Robust optimization of the heteroextractive distillation column for the purification of water/acetic acid mixtures using p-xylene as entrainer, Comput. Chem. Eng. 95(2016) 161-169.

[13] C. Pirola, F. Galli, F. Manenti, M. Corbetta, C.L. Bianchi, Simulation and related experimental validation of acetic acid/water distillation using p-xylene as entrainer, Ind. Eng. Chem. Res. 53(46) (2014) 18063-18070.

[14] H. Zhang, H. Xu, X. Dai, H. Yu, Q. Ye, Simulation and optimization of extractive distillation for separating methanol and trimethoxysilane, Mod. Chem. Ind. 35(1) (2015) 163-167(in Chinese).

[15] M.D. Sanchez-Russinyol, A. Aucejo, S. Loras, Isobaric vapor-liquid equilibria for binary and ternary mixtures of ethanol, methylcyclohexane, and p-xylene, J. Chem. Eng. Data 49(5) (2004) 1258-1262.

[16] Q.S. Li, F.Y. Xing, Z.G. Lei, B.H. Wang, Q.L. Chang, Isobaric vapor-liquid equilibrium for isopropanol + water +1-ethyl-3-methylimidazolium tetrafluoroborate, J. Chem. Eng. Data 53(1) (2008) 275-279.

[17] J. Hou, S.M. Xu, H. Ding, T. Sun, Isobaric vapor-liquid equilibrium of the mixture of methyl palmitate and methyl stearate at 0.1 kPa, 1 kPa, 5 kPa, and 10 kPa, J. Chem. Eng. Data 57(10) (2012) 2632-2639.

[18] G.W. Tang,H. Ding, J. Hou, S.M. Xu, Isobaric vapor-liquid equilibrium for binary system of ethyl myristate + ethyl palmitate at 0.5, 1.0 and 1.5 kPa, Fluid Phase Equilib. 347(2013) 8-14.

[19] J.M. Smith, H.C. Van Ness, M.M. Abbott, Introduction to Chemical Engineering Thermodynamics, McGraw-Hill Education, Boston, New York, 2005338-369, 430-442, 545-546.

[20] J.M. Prausnitz, R.N. Lichtenthaler, E.G.D. Azevedo, Molecular Thermodynamics of Fluid-Phase Equilibria, Vols. 1-22, Pearson Education, NJ, 199842-45(in Chinese).

[21] T.E. Tan, M. Dou, M.H. Zhou, Principles of Chemical Engineering, 3rd. ed.Vols. 74-75, Chemical Industry Press, Beijing, 2006157-158(in Chinese).

[22] X.D. Zhang, D.P. Hu, Z.C. Zhao, Measurement and prediction of vapor pressure for H₂O + CH₃OH/C₂H₅OH +[BMIM][DBP] ternary working fluids, Chin. J. Chem. Eng. 21(8) (2013) 886-893.

[23] M.T.G. Jongmans, J.I.W. Maassen, A.J. Luijks, B. Schuur, A.B. de Haan, Isobaric lowpressure vapor-liquid equilibrium data for ethyl benzene + styrene + sulfolane and the three constituent binary systems, J. Chem. Eng. Data 56(9) (2011) 3510-3517.

[24] Z.G. Lei, C.Y. Li, B.H. Chen, Behaviour of tributylamine as entrainer for the separation of water and acetic acid with reactive extractive distillation, Chin. J. Chem. Eng. 11(5) (2003) 515-519.

[25] D.B. Kaymak, W.L. Luyben, O.J. Smith, Effect of relative volatility on the quantitative comparison of reactive distillation and conventional multi-unit systems, Ind. Eng. Chem. Res. 43(12) (2004) 3151-3162.

[26] Aspentech, Aspen Property System:Physical Property Systems Methods and Models 11.1., Aspen Technology, Inc., Burlington, 200120-33.

[27] A. Fredenslund, J. Gmehling, P. Rasmussen, Vapor-liquid Equilibria Using UNIFAC:A Group Contribution Method, Elsevier, Amsterdam, 1977.

[28] P.L. Jackson, R.A. Wilsak, Thermodynamic consistency tests based on the GibbsDuhem equation applied to isothermal, binary vapor-liquid equilibrium data:data evaluation and model testing, Fluid Phase Equilib. 103(1995) 155-197.

[29] J.W. Kang, V. Diky, R.D. Chirico, J.W. Magee, C.D. Muzny, A.F. Kazakov, K. Kroenlein, M. Frenkel, Algorithmic framework for quality assessment of phase equilibrium data, J. Chem. Eng. Data 59(7) (2014) 2283-2293.

[30] R.E. Rooks, V. Julka, M.F. Doherty, M.F. Malone, Structure of distillation regions for multicomponent azeotropic mixtures, AIChE J. 44(6) (1998) 1382-1391.

[31] S. Widagdo, W.D. Seider, Azeotropic distillation, AIChE J. 42(1) (1996) 96-130.

[32] X.M. Zhang, Y.X. Liu, C.G. Jian, F. Wei, H.P. Liu, Experimental isobaric vapor-liquid equilibrium for ternary system of sec-butyl alcohol + sec-butyl acetate + N,Ndimethyl formamide at 101.3 kPa, Fluid Phase Equilib. 383(2014) 5-10.

[33] X.M. Zhang, H.P. Liu, Y.X. Liu, C.G. Jian, W. Wang, Experimental isobaric vapor-liquid equilibrium for the binary and ternary systems with methanol, methyl acetate and dimethyl sulfoxide at 101.3 kPa, Fluid Phase Equilib. 408(2016) 52-57.

[34] A. Fredenslund, J. Gmehling, P. Rasmussen, Vapor-liquid Equilibria Using UNIFAC:A Group Contribution Method, Vols. 68-84, Elsevier, Amsterdam, 1977150-155.