Effect of operating conditions on divinylbenzene production in diethyl benzene dehydrogenation reactor

Document Type: Research note


Iran Polymer and Petrochemical Institute, P. O. Box: 14965-115, Tehran, Iran


DEB dehydrogenation reaction was conducted to produce divinylbenzene (DVB) and ethylvinylbenzene (EVB). The effects of temperature, catalyst weight and time factor on the performance of the dehydrogenation reactor were investigated experimentally. Temperature was varied from 550º C up to 600 º C. Temperature affect the conversion of DEB to DVB significantly. The mole fraction of DEB in the outlet of the reactor is reducing up to 580 º C, but further increase in temperature up to 600 º C does not decrease the mole fraction of DEB in the outlet of the reactor. Catalyst weight was varied from 10 gr up to 40 gr. The results showed that the trends of EVB+DVB production and DEB consumption are identical at various catalyst weights. To obtain optimum time factor for the DEB dehydrogenation process experiments were conducted at various time factors. The results showed that the optimum time factor for DVB as a desired product is 825 gr/hr.mole. . The data and information provided in this research can be used for scale-up and optimization purposes.


Main Subjects

[1]      Toghyani, M., Rahimi, A. and Mirmohammadi, J., “Mathematical modeling and parameteric study of a dehydrogenation decoking process”, Apllied Catalysis, A: General, 489, 226 (2015)

[2]      Finlayson, B. A., “Packed bed reactor analysis by orthogonal collocation”, Chemical Engineering Science, 26, 1081 (1971).

[3]      Barnea, E. and Mednick, R. L., “A generalized approach to fluid dynamics of particulate systems, Part III: General correlation for the pressure drop through fixed beds of spherical particles”, The Chemical Engineering Journal, 15, 215 (1978).

[4]      Suwanprasop, S., Eftaxias, A., Stuber, F., Polaert, I., Julcour-Lebigue, C. and Delmas, H., “Scale-up and modeling of fixed bed reactors for catalytic phenol oxidation over adsorptive active carbon”, Ind. Eng. Chem. Res., 44, 9513 (2005).

[5]      Quan-Sheng, L., Zhi-Xin, Z. and Jing-Lai, Z., “Steady state and dynamic behavior of fixed bed catalytic reactor for fischer-tropsch synthesis”, Journal of Natural Gas Chemistry, 8 (2), 137 (1999).

[6]      Megiris, C. E. and Butt, J. B., “Effects of poisoning on the dynamics of fixed bed reactors: Cyclic and temperature-increased operational policies”, Chemical Engineering Science, 43 (8), 2239 (1988).

[7]      Schuurman, Y., “Aspects of kinetic modeling of fixed bed reactors”, Catalysis Today, 138, 15 (2008).

[8]      Ibrahim, H. G., Al-Meshragi, M., Alshuiref, A. A., Alagta, A. R. and Edali, M. A., “Radial heat transport in packed beds-II: Mathematical modeling of heat transfer through packed beds at elevated pressure”, International Journal of Engineering and Applied Sciences, 4 (2), 24 (2013).

[9]      Kolios, G., Frauhammer, J. and Eigenberger, G., “Auto thermal fixed bed reactor concepts”, Chemical Engineering Science, 55, 5945 (2000).

[10]  Jesus, J. M., Santana, P. L. and Silva, F. V., “Different approaches in concentration-temperature cascade control of a fixed bed reactor for the phthalic anhydride synthesis”, Chemical Engineering Transactions, 32, 1387 (2013).

[11]  Budman, H. and Silveston, P. L., “Control of periodically operated reactors”, Chemical Engineering Science, 63, 4942 (2008).

[12]  Sorensen, J. P., “Experimental investigation of the optimal control of a fixed bed reactor”, Chemical Engineering Science, 32, 763 (1977).

[13]  Clement, K., Jorgensen, S. B. and Sorensen, J. P., “Fixed bed reactor Kalman filtering and optimal control-II”, Chemical Engineering Science, 35, 1231 (1980).

[14]  Reddy, R. K. and Joshi, J. B., “CFD modeling of pressure drop and drag coefficient in fixed beds: Wall effects”, Particuology, 8, 37 (2010).

[15]  Lin, D. Q., Shi, W., Tong, H. F.,Van de Sandt, E. J. A. X, Boer, P., Ferreira, G. N. M. and Yao, S. J., “Evaluation and characterization of axial distribution in expanded bed: Liquid mixing and local effective axial dispersion”, Journal of Chromatography, A, 1393, 65 (2015).

[16]  Farsi, M., Mazinani, S. and Jahanmiri, A., “Steady state operability characteristics of an adiabatic  fixed bed reactor for methanol dehydration”, Iran J. Chem. Eng., 30 (4), 45 (2011).

[17]  Sorensen, M. D. P., “Deactivation models by fitting the progression of temperature profiles-coking model for the MTG process in adiabatic reactors”, Chemical Engineering Science, 106, 126 (2014).

[18]  Qihong, Z., Minheng, C. and Weikang, Y., “Studies of adiabatic fixed bed reactors: (I) Ignition of reactors”, Journal of Chemical Industry and Engineering (China), 2 (2), (1987).

[19]  Schoneberger, J. C., Arellano-Garcia, H., Thielert, H., Korkel, S. and Wozny, G., “Optimal experimental design of a catalytic fixed bed reactor”, 18th European Symposium on Computer Aided Process Engineering-ESCAPE 18, (2008).

[20]  Smeds, S., Sami, T. and Murzin, Y. D., “Gas phase hydrogenation of ethylbenzene over Ni: Comparison of different fixed bed reactors”, Applied Catalysis, A: General, 201, 55 (2000).

[21]  Chen, S., Sun, A., Qin, Z. and Wang, J., “Reaction coupling of diethylbenzene dehydrogenation with water-gas shift over alumina-supported iron oxide catalysts”, Catalysis Communications, 4, 441  (2003).

[22]  Hong, D. Y., Jhung, S. H., Vislovskiy, V. P., Chang, J. S., Yoo, J. S., Park, S. E. and Park, Y. H., “Dehydrogenation of alkylaromatics over supported vanadium oxide catalyst with carbon dioxide as soft oxidant”, Applied Chemistry, 8 (2), 572 (2004).

[23]  Kamiguchi, S., Kondo, K., Kodomari, M. and Chihara, T., “Catalytic ring-attachement isomerization and dealkylation of diethylbenzene over halide clusters of group 5 and group 6 transition metals”, Journal of Catalysis, 223, 54 (2004).

[24]   Forni, L. and Valerio, A., “Kinetics of diethylbenzene catalytic dehydrogenation”, Ind. Eng. Chem. Process Des. Develop., 10 (4), 552 (1971).

[25]  Kotelnikov, G. R., Bespalov, V. P., Sidnev, V. B. and Kachalov, D. V., “Production and operation of dehydrogenation catalysts”, Catalysis in Industry, 1 (1), 66 (2009).

[26]  Kaeding, W. W., Klosek, J. K. and Young, L. B., “Process for preparation of para-divinylbenzene”, US Patent, 4982030, (1991).

[27]  Yu, B., Xu, T., Cong, H., Peng, Q. and Usman M., “Preparation of porous poly(styrene-divinylbenzene) microspheres and their modification with diazoresin for mix-mode HPLC separations”, Materials, 440 (10), 1 (2017).

[28]  Ji, X., Griesing, F., Yan, R., Sun, B., Pauer, W., Zhu, M., Sun, Y.  and Moritz H. U., “One-pot preparation of poly(styrene-co-divinylbenzene)/silver nanoparticles composite microspheres with tunable porosity and their catalytic degradation of methylene blue in aqueous solution”, RSC Advances, 7, 50176 (2017).

[29]  Salek, P., Horak, D. and Hromadkova, J., “Novel prepation of monodisperse poly(styrene-co-divinylbenzene) microspheres by controlled dispersion polymerization”, Polymer Science, Series B, 60 (1), 9 (2018).