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Volume 66, Issue 6

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Extractive distillation modeling of the ternary system 2-methoxy-2-methylpropane-methanol-butan-1-ol

Zuzana Labovská
  • Institute of Chemical and Environmental Engineering, Faculty of Chemical and Food Technology, Slovak University of Technology, Radlinského 9, 812 37, Bratislava, Slovakia
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 / Pavol Steltenpohl
  • Institute of Chemical and Environmental Engineering, Faculty of Chemical and Food Technology, Slovak University of Technology, Radlinského 9, 812 37, Bratislava, Slovakia
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 / Elena Graczová
  • Institute of Chemical and Environmental Engineering, Faculty of Chemical and Food Technology, Slovak University of Technology, Radlinského 9, 812 37, Bratislava, Slovakia
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Published Online: 2012-04-11 | DOI: https://doi.org/10.2478/s11696-012-0138-2

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Abstract

Influence of model complexity on the separation equipment performance was investigated. As an example, separation of azeotrope formed by 2-methoxy-2-methylpropane and methanol was considered using butan-1-ol as an extractive solvent. Non-equilibrium model of a column for extractive distillation accounting for the mass and heat transfer rates was composed according to the rigorous Maxwell-Stefan theory. An empirical AICHE correlation was adopted for the calculation of binary mass transfer coefficients at column trays. Results of the column steady-state operation were compared with those obtained assuming different equilibrium models. Effect of the quality of the vapor-liquid equilibrium (VLE) description on the results of the separation simulation considering real behavior of either liquid or both equilibrium phases was tested. Real behavior of the liquid phase was computed according to the NRTL equation taking into account binary and, in some cases, also ternary equilibrium data. In case of real behavior of the vapor phase, the equation of state in the form of virial expansion was employed. Qualitative agreement was found comparing the simulation results calculated by equilibrium and non-equilibrium models of the extractive distillation column while using the same description of ternary VLE.

Keywords: distillation column; equilibrium model; non-equilibrium model; relative volatility; separation efficiency; ternary contribution

  • [1] AICHE (1958). Bubble tray design manual. New York, NY, USA: AIChE. Google Scholar

  • [2] Arce, A., Martínez-Ageitos, J., Rodil, E., & Soto, A. (2000). Phase equilibria involved in extractive distillation of 2-methoxy-2-methylpropane+methanol using 1-butanol as entrainer. Fluid Phase Equilibria, 171, 207–218. DOI: 10.1016/s0378-3812(00)00364-2. http://dx.doi.org/10.1016/S0378-3812(00)00364-2CrossrefGoogle Scholar

  • [3] Arce, A., Martínez-Ageitos, J., Rodil, E., & Soto, A. (2001). Thermophysical properties for 1-butanol+ethanol+2-methoxy-2-methylbutane ternary system. Fluid Phase Equilibria, 187–188, 155–169. DOI: 10.1016/s0378-3812(01)00529-5. http://dx.doi.org/10.1016/S0378-3812(01)00529-5CrossrefGoogle Scholar

  • [4] Arce, A., Martínez-Ageitos, J., & Soto, A. (1996). VLE measurements of ninary mixtures of methanol, ethanol, 2-methoxy-2-methylpropane, and 2-methoxy-2-methylbutane at 101.32 kPa. Journal of Chemical and Engineering Data, 41, 718–723. DOI: 10.1021/je950323o. http://dx.doi.org/10.1021/je950323oCrossrefGoogle Scholar

  • [5] Arce, A., Rodil, E., & Soto, A. (1999). Extractive distillation of 2-methoxy-2-methylpropane + ethanol using 1-butanol as entrainer: Equilibria and simulation. The Canadian Journal of Chemical Engineering, 77, 1135–1140. DOI: 10.1002/cjce.5450770608. http://dx.doi.org/10.1002/cjce.5450770608CrossrefGoogle Scholar

  • [6] Chauvel, A., & Lefebvre, G. (1989). Petrochemical processes: Synthesis-gas derivatives and major hydrocarbons (Vol. 1, Chapter 3, pp. 212–214). Paris, France: éditions Technip. Google Scholar

  • [7] Chen, F. R., Huss, R. S., Malone, M. F., & Doherty, M. F. (2000). Simulation of kinetic effects in reactive distillation. Computers and Chemical Engineering, 24, 2457–2472. DOI: 10.1016/s0098-1354(00)00609-8 http://dx.doi.org/10.1016/S0098-1354(00)00609-8CrossrefGoogle Scholar

  • [8] Doherty, M. F., & Malone, M. F. (2001). Conceptual design of distillation systems (Chapter 5, pp. 183–256). New York, NY, USA: McGraw-Hill. Google Scholar

  • [9] Gentry, J. C., Kumar, S., & Wright-Wytcherley, R. (2004). Use extractive distillation to simplify petrochemical processes. Hydrocarbon Processing, 83(6), 62. Google Scholar

  • [10] Gmehling, J., Menke, J., Krafczyk, J., & Fischer, K. (2004). Azeotropic data (2nd ed., pp. 216–217). Weinheim, Germany: Wiley-VCH. Google Scholar

  • [11] Gmehling, J., & Onken, U, (2003). Vapor-liquid equilibrium data collection (Vol. I, 1c, pp. 625–630). Frankfurt/Main, Germany: DECHEMA. Google Scholar

  • [12] Graczová, E., Steltenpohl, P., & Bafrncová, S. (2005). Extractive distillation: Prediction of the vapour-liquid equilibrium data of multi-component systems. In J. Klemeš (Ed.), Chemical Engineering Transactions (Vol. 7, pp. 339–344). Milano, Italy: AIDIC. Google Scholar

  • [13] Graczová, E., Steltenpohl, P., Chlebovec, M., & Labovsky, J. (2009). Improvement of accuracy of the multicomponent vapor-liquid equilibria prediction for the purpose of separation process modelling. In J. Klemeš (Ed.), Chemical Engineering Transactions (Vol. 18, pp. 207–212). Milano, Italy: AIDIC. DOI: 10.3303/cet0918032. CrossrefGoogle Scholar

  • [14] Hömmerich, U., & Rautenbach, R. (1998). DDesign and optimization of combined pervaporation/distillation processes for the production of MTBE. Journal of Membrane Science, 146, 53–64. DOI: 10.1016/s0376-7388(98)00085-4. http://dx.doi.org/10.1016/S0376-7388(98)00085-4CrossrefGoogle Scholar

  • [15] Krishna, R., & Wesselingh, J. A. (1997). The Maxwell-Stefan approach to mass transfer. Chemical Engineering Science, 52, 861–911. DOI: 10.1016/s0009-2509(96)00458-7. http://dx.doi.org/10.1016/S0009-2509(96)00458-7Web of ScienceCrossrefGoogle Scholar

  • [16] Krishnamurthy, R., & Taylor, R. (1985a). A nonequilibrium stage model of multicomponent separation processes. Part I: Model description and method of solution. AIChE Journal, 31, 449–456. DOI: 10.1002/aic.690310312. http://dx.doi.org/10.1002/aic.690310312CrossrefGoogle Scholar

  • [17] Krishnamurthy, R., & Taylor, R. (1985b). A nonequilibrium stage model of multicomponent separation processes. Part II: Comparison with experiment. AIChE Journal, 31, 456–465. DOI: 10.1002/aic.690310313. http://dx.doi.org/10.1002/aic.690310313CrossrefGoogle Scholar

  • [18] Peters, M., Glasser, D., Hildebrandt, D., & Kauchali, S. (2011). Membrane process design using residue curve maps (Chapter 8, pp. 151–167). Hoboken, NJ, USA: Wiley. http://dx.doi.org/10.1002/9780470910030Google Scholar

  • [19] Poling, B. E., Prausnitz, J. M., & O’Connell, J. P. (2001). The properties of gases and liquids (5th ed.). New York, NY, USA: McGraw-Hill. Google Scholar

  • [20] Renon, H., & Prausnitz, J. M. (1968). Local compositions in thermodynamic excess functions for liquid mixtures. AICHE Journal, 14, 135–144. DOI: 10.1002/aic.690140124. http://dx.doi.org/10.1002/aic.690140124CrossrefGoogle Scholar

  • [21] Rodriguez-Donis, I., Gerbaud, V., & Joulia, X. (2009). Thermodynamic insights on the feasibility of homogeneous batch extractive distillation, 1. Azeotropic mixtures with a heavy entrainer. Industrial & Engineering Chemistry Research, 48, 3544–3559. DOI: 10.1021/ie801060n. http://dx.doi.org/10.1021/ie801060nCrossrefWeb of ScienceGoogle Scholar

  • [22] Steltenpohl, P., & Graczová, E. (2010). Application of extended NRTL equation for ternary liquid-liquid and vapor-liquid-liquid equilibria description. Chemical Papers, 64, 310–317. DOI: 10.2478/s11696-010-0006-x. http://dx.doi.org/10.2478/s11696-010-0006-xWeb of ScienceCrossrefGoogle Scholar

  • [23] Steltenpohl, P., Chlebovec, M., & Graczová, E. (2005). Simulation of toluene extractive distillation from a mixture with heptane. Chemical Papers, 59, 421–427. Google Scholar

  • [24] Steltenpohl, P., Graczová, E., & Chlebovec, M. (2009). Extractive distillation of C7 hydrocarbon mixture in the presence of furfural. In J. Klemeš (Ed.), Chemical Engineering Transactions (Vol. 18, pp. 201–206). Milano, Italy: AIDIC. DOI: 10.3303/cet0918031. CrossrefGoogle Scholar

  • [25] Streicher, C., Asselineau, L., & Forestičre, A. (1995). Separation of alcohol/ether/hydrocarbon mixtures in industrial etherification processes for gasoline production. Pure and Applied Chemistry, 67, 985–992. DOI: 10.1351/pac199567060985. http://dx.doi.org/10.1351/pac199567060985CrossrefGoogle Scholar

  • [26] Surový, J., Dojčanský, J., & Bafrncová, S. (1982). Some information on calculating the liquid-liquid equilibrium of ternary systems. Collection of Czechoslovak Chemical Communications, 47, 1420–1432. http://dx.doi.org/10.1135/cccc19821420Google Scholar

  • [27] Švandová, Z., Kotora, M., Markoš J., & Jelemenský, Ľ. (2006). Dynamic behaviour of a CSTR with reactive distillation. Chemical Engineering Journal, 119, 113–120. DOI: 10.1016/j.cej.2006.03.032. http://dx.doi.org/10.1016/j.cej.2006.03.032CrossrefGoogle Scholar

  • [28] Švandová, Z., Markoš, J., & Jelemenský, Ľ. (2006). Multiple steady states in a CSTR with total condenser: Comparison of equilibrium and nonequilibrium models. Chemical Papers, 60, 432–440. DOI: 10.2478/s11696-006-0079-8. http://dx.doi.org/10.2478/s11696-006-0079-8CrossrefGoogle Scholar

  • [29] Taylor, R., & Krishna, R. (1993). Multicomponent mass transfer. New York, NY, USA: Wiley. Google Scholar

  • [30] Tsonopoulos, C. (1974). An empirical correlation of second virial coefficients. AIChE Journal, 20, 263–272. DOI: 10.1002/aic.690200209. http://dx.doi.org/10.1002/aic.690200209CrossrefGoogle Scholar

About the article

Published Online: 2012-04-11

Published in Print: 2012-06-01

Citation Information: Chemical Papers, Volume 66, Issue 6, Pages 556–565, ISSN (Online) 1336-9075, DOI: https://doi.org/10.2478/s11696-012-0138-2.

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© 2012 Institute of Chemistry, Slovak Academy of Sciences.

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