The Coupling Process Design Of Methanol Aromatization And Short Chain Olefin Alkylation Of 100000 Tons/year

Aromatics are very important basic raw materials in the chemical industry.At present,most of the production of industrial aromatics mainly comes from the petroleum based route,which is obtained by the way of cracking gasoline hydrogenation and catalytic reforming.It is highly dependent on petroleum resources.According to the fossil energy structure of"relatively rich in coal,poor in oil and little in gas",the development of aromatization technology using coal-based methanol as raw material can not only effectively expand the source of aromatics,reduce the dependence on oil resources,but also help to alleviate the energy dilemma facing China.Based on the research results of the State Key Laboratory for the effective utilization of chemical resources of Beijing University of Chemical Technology for many years,this paper carried out the coupling process design of 100000 tons aromatics/year methanol aromatization and short chain olefin alkylation.First of all,based on the analysis of the existing research results,the paper constructs the methanol aromatization short chain olefin alkylation coupling process,which is mainly composed of methanol feed unit,aromatization unit,three-phase(gas,oil and water)separation unit,benzene and short chain olefin alkylation unit,and the corresponding separation unit,etc.,draws the process flow chart and carries out the material and heat balance Yes.Secondly,based on the mathematical model of one-dimensional quasi homogeneous fixed bed reactor,a five stage adiabatic bed methanol aromatization reactor with inner diameter of 2.16m,catalyst filling height of 12.68m and wall thickness of 20mm was optimized.Thirdly,the design of methanol feed system and three-phase separator is completed on the basis of overall process calculation.Among them,the methanol feed system is composed of one kettle reboiler and two shell and tube heat exchangers.The tube bundle diameter of the kettle reboiler is 707mm and the shell diameter is 1850mm.The two shell and tube heat exchangers are BEM 1600-0.6-811.9-6/25-1 and BEM 1200-1-385.1-4.5/25-1 respectively.Finally,based on the optimization analysis data of Aspen process simulation software,the structure design and operation flexibility analysis of dealkylation tower,debenzylation and xylene tower,debenzylation tower and debenzylation tower are completed.Among them,the diameter of dealkylation tower is 1.0m,and the effective height is 6.4m;the diameter of dealkylation and xylene tower is 2.2M,and the effective height is 8.0m;the diameter of dealkylation tower is 1.2m,and the effective height is 11.6m;the diameter of dealkylation tower is 1.8m,and the effective height is 10.4m.