石脑油催化裂解结构化反应器反应特性的CFD模拟
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摘要
以石脑油为原料,采用催化裂解六集总动力学模型,建立描述结构化反应器内催化裂解的反应器数学模型,并利用CFD软件对结构化反应器内的石脑油催化裂解性能进行数值模拟。通过改变孔道直径、反应器长度以及反应器内温度、气体入口速率考察反应器结构尺寸和反应条件对目标产物乙烯、丙烯的收率及石脑油转化率的影响。结果表明,反应器孔道直径的增加,目标产物收率减小,反应器长度20 mm时反应完全,升高反应温度和增大入口速率均有利于目标产物的生成。在入口温度680℃和入口速率0.4 m·s-1条件下,石脑油转化率92%,乙烯收率19.3%,丙烯收率23.1%。而在相同反应条件下的固定床反应器中乙烯收率10.3%,丙烯收率13.3%,石脑油转化率80.0%。
Mathematic model for naphtha catalytic cracking in monolith reactor is established using six lumped kinetics by CFD simulations. Effects of reactor size and reaction conditions on yield of ethylene,propylene and naphtha conversion are investigated by changing channel diameter,reactor length,reaction temperature and gas inlet velocity. The results show that increase in channel diameter leads to decrease of products yield. Reaction completes at channel length around of 20 mm. Increasing in reaction temperature and entrance velocity are beneficial to production of target products. The monolith reactor can achieve a propylene yield up to 23. 1% and ethylene yield to 19. 3% with a naphtha conversion being 92% at680 ℃ and 0. 4 m·s-1; this is in contrast to a typical fixed reactor under the same reaction conditions,in which case the ethylene yield is 10. 3%,the propylene yield is 13. 3%,and the conversion rate of naphtha was 80. 0%.
Mathematic model for naphtha catalytic cracking in monolith reactor is established using six lumped kinetics by CFD simulations. Effects of reactor size and reaction conditions on yield of ethylene,propylene and naphtha conversion are investigated by changing channel diameter,reactor length,reaction temperature and gas inlet velocity. The results show that increase in channel diameter leads to decrease of products yield. Reaction completes at channel length around of 20 mm. Increasing in reaction temperature and entrance velocity are beneficial to production of target products. The monolith reactor can achieve a propylene yield up to 23. 1% and ethylene yield to 19. 3% with a naphtha conversion being 92% at680 ℃ and 0. 4 m·s-1; this is in contrast to a typical fixed reactor under the same reaction conditions,in which case the ethylene yield is 10. 3%,the propylene yield is 13. 3%,and the conversion rate of naphtha was 80. 0%.
引文
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[3]王建明.催化裂解生产低碳烯烃技术和工业应用的进展[J].化工进展,2011,30(5):911-917.Wang Jianming.Progress in the production of low carbon olefin by catalytic cracking[J].Chemical Industry and Engineering Progress,2011,30(5):911-917.
[4]魏晓丽,毛安国,张久顺,等.石脑油催化裂解反应特性及影响因素分析[J].石油炼制与化工,2013,44(7):1-7.Wei Xiaoli,Mao Anguo,Zhang Jiushun,et al.Study on reaction characteristics and influence factors of naphtha catalytic cracking[J].Petroleum Processing and Petrochemicals,2013,44(7):1-7.
[5]刘剑,孙淑坤,张永军,等.石脑油催化裂解制低碳烯烃技术进展及其技术经济分析[J].化学进展,2011,29(11):33-37.Liu Jian,Sun Shukun,Zhang Yongjun,et al.Advance in catalytic cracking of naphtha to light olefins and techno-economic analysis[J].Chemical Industry,2011,29(11):33-37.
[6]龙军,邵潜,贺振富,等.规整结构催化剂及反应器研究进展[J].化工进展,2004,23(9):925-932.Long Jun,Shao Qian,He Zhenfu,et al.Monolithic catalysts and monolithic reactors[J].Chemical Industry and Engineering Progress,2004,23(9):925-932.
[7]Wei J,Kuo J C W.A lumping analysis in monomolecular reaction systems[J].Industrial&Engineering Chemistry Fundamentals,1969,8(1):233-243.
[8]Guo W,Xiao W,Luo M.Comparison among monolithic and randomly packed reactors for the methanol-to-propylene process[J].Chemical Engineering Journal,2012,207-208:734-745.
[9]Chen J,Yang H,Wang N,et al.Mathematical modeling of monolith catalysts and reactors for gas phase reactions[J].Applied Catalysis A General,2008,345(1):1-11.
[10]Liu H,Zhao J,Li C,et al.Conceptual design and CFD sim-ulation of a novel metal-based monolith reactor with enhanced mass transfer[J].Catalysis Today,2005,1505(3):401-406.
[11]吴小军.石脑油催化裂解制乙烯丙烯反应动力学研究[D].上海:华东理工大学,2011.Wu Xiaojun.kinetic model study on naphtha catalytic cracking for ethylene and propylene production[D].Shanghai:East China University of Science and Technology,2011.
[12]Hayes R E,Kolaczkowski S T.Mass and heat transfer effects in catalytic monolith reactors[J].Chemical Engineering Science,1994,49(21):3587-3599.
[13]Irani M,Alizadehdakhel A,Pour A N,et al.CFD modeling of hydrogen production using steam reforming of methane in monolith reactors:surface or volume-base reaction model?[J].International Journal of Hydrogen Energy,2011,36(24):15602-15610.