宁波工程学院-甬碳调.pptx

单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,2014/8/16,#,YTD,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,2014/8/16,#,YTD,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,2014/8/16,#,YTD,年处理,100,万吨甲醇制对二甲苯项目,Production of P-xylene by processing methanol(1000kt/a),甬碳调团队,宁波工程学院,2014“,恒逸,-,三井化学杯”,第,八届全国大学生化工设计竞,赛,团队成员：张 烽 张海林 张中原 陈炜珊 林,强,指导老师：史玉立 邓利娟,1,项目背景,Background,设备设计,Equipment,Design,工艺介,绍,Process,Introduction,经济分析,Economic,Analysis,厂区布置,Plant,Arrangement,项目总,结,Summary,年处理,100,万吨甲醇制对二甲苯项目,2,Production of P-xylene by processing methanol(1000kt/a),1,2,3,4,5,6,项目背景,市场分析,Market Analysis,原料来源及工艺方案,Raw Materials&Process Scheme,项目概况,Project Introduction,3,3,对二甲苯（,PX,）,重要的有机化工原料,精对苯二甲酸（,PTA,）,世界上,90%,以上用来生产聚酯（,PET,）,聚酯（,PET,）,涤纶、纤维、聚酯瓶、聚酯膜、塑料合金等,4,市场分析,原料来源及工艺方案,Raw Materials&Process Scheme,项目概况,Project Introduction,项目背景,Market Analysis,世界,PTA,产能及,PX,需求量对比图,Comparison between the PTA production and the PX demand,自给能力不足,5,国内,PX,的需求,Domestic demand of PX,国内,PX,的自给率,Domestic self-support of PX,市场分析,Market Analysis,项目背景,市场分析,Market Analysis,我国,PX,的价格走势,Domestic price trends of PX,价格持续走高,6,项目概况,Project Introduction,7,项目背景,市场分析,Market Analysis,Process Scheme,工艺方案,7,甲苯歧化和烷基,转移,工艺,C,8,芳烃异构化工艺,甲苯甲醇甲基化工艺,煤制,PX工艺,PX,生产,方,法,对二甲苯,甲醇,煤,原料利用率不高,C,8,损失量大,生产成本高,原料来源丰富,转化率高,8,项目背景,Process Scheme,工艺方案,全,球煤炭产量第一,36.3,亿吨,全,球化纤产量第一,0.8,亿吨,1,2,3,4,YTD,背景,总结,十二五,规划,十三五,规划,多煤贫油少气,HSE,管理体系,工艺合理,绿色生产,煤制甲醇合成,PX,项目背景,9,10,芳构化工段,芳烃分离工段,提纯工段,异构化,工段,烷基化工段,工艺介绍,10,设备设计,Equipment Design,换热网络,Heat Exchanger Network,工艺流程,Process Flowsheet,自动控制,Automatic Control,11,工艺流程,Process Flowsheet,工艺介绍,PX,生产工艺流程框图,Process flow chart of PX,芳构化,Aromatization,脱,水,反,应,器,二,甲,醚,分,离,塔,甲醇,二甲醚,工艺介绍,工艺流程,Process Flowsheet,-,氧化,铝,催,化剂,250,0,.4MPa,12,二甲醚,芳构化产物,工艺介绍,Process Flowsheet,13,工艺流程,MoHAlZSM-5,380,1.4MPa,芳构化,Aromatization,芳,构,化,反,应,器,芳烃低碳烃分离,Arene&Alkane Separation,工艺介绍,工艺流程,Process Flowsheet,14,芳构化,Aromatization,C,1,-,C,9,C,6,-,C,9,C,1,-,C,5,气液,分,离,器,氢,气，甲烷,芳烃低碳烃分离,Arene&Alkane Separation,气体,C,1,-,C,5,分隔壁精馏塔,C,4,-,C,5,二甲醚,C,1,-,C,3,工艺介绍,工艺流程,Process Flowsheet,15,0,3.1MPa,芳构化,Aromatization,精馏塔,液体,C,6,-,C,9,C,6,-,C,7,C,8,-,C,9,异构化,Isomerization,异构化反应器,C,8,-,C,9,氢气,粗对二甲苯,工艺介绍,工艺流程,Process Flowsheet,16,SKI-200,型,420,1.0MPa,芳构化,Aromatization,芳烃低碳烃分离,Arene&Alkane Separation,烷基化,Alkylation,甲醇,甲苯,C,6,-,C,8,烷基化反应器,载气,工艺介绍,工艺流程,Process Flowsheet,17,Zn-HZSM-5,460,0.1MPa,芳构化,Aromatization,异构化,Isomerization,芳烃低碳烃分离,Arene&Alkane Separation,C,6,-C,8,苯,粗对二甲苯,工艺介绍,工艺流程,Process Flowsheet,18,脱苯塔,0,0.1MPa,芳构化,Aromatization,烷基化,Alkylation,异构化,Isomerization,芳烃低碳烃分离,Arene&Alkane Separation,提纯,Purification,烷基化粗,对二甲苯,异构化粗,对二甲苯,PX,吸附分离器,工艺介绍,工艺流程,Process Flowsheet,19,抽提液塔,抽余液塔,芳构化,Aromatization,烷基化,Alkylation,异构化,Isomerization,芳烃低碳烃分离,Arene&Alkane Separation,采用废热回收技术对甲醇芳构化反应器反应热进行回收，,以,产,生,过热,蒸,汽,回收热量,1.6,10,7,kJ/h,年,产,过热,蒸,汽,7,万吨,20,余热回收,工艺介绍,节能降耗,Energy-saving,21,工艺介绍,分隔壁精馏塔,节能降耗,Energy-saving,塔设备,冷凝器,1,kW,冷凝器,2,kW,再沸器,1,kW,再沸器,2,kW,总计,kW,节能,%,传统双塔精馏,3514.4,3291.5,3825.7,4334.4,14966,0,分隔壁塔,5854.2,0,0,5488.2,11342.4,24.2,分隔壁塔的节能效果,Energy-saving effect of the divided-wall distillation column,对于三元混合物分离，采用传统的简单塔分离流程需要,2,个精馏塔，分隔壁精馏塔则能单塔实现分离,脱苯塔操作参数表,Operating parameters of debenzolization tower,脱苯塔,塔顶温度,89.3,塔底温度,100.9,相差,11.6,节能,64.07%,可行,22,节能降耗,Energy-saving,热泵精馏塔,工艺介绍,二甲醚分离塔的回流比,0.28,减压塔的进料位置,16,回流比,23,塔板数,进料位置,工艺介绍,工艺优化,Process Flowsheet,工艺介绍,设备选型,Equipment Selection,工艺设计,Process Flowsheet,自动控制,Automatic Control,节能降耗,Conserve Energy,优化前换热网络,优化后换热网络,换热网络优化后的能量,24,Item,Heating,（,kJ/h,）,Colding,（,kJ/h,）,Before Matching,6.362,10,8,6.326,10,8,After Matching,2.596,10,8,2.275,10,8,Energy Saving,3.766,10,8,4.051,10,8,Percentage of Energy Saving,59.20%,64.03%,热公用工程,64.03%,冷公用工程,59.20%,总费用,1998.8,万元,异构化工段进料,烷基化工段进料,冷却水,异构化工段出料,流化,床,反,应器,T0102,塔底馏出液,加热炉,加热炉,25,实际换热网络,工艺介绍,换热网络,Heat Exchanger Network,26,5,储罐选型,Tank,Design,4,泵选型,Pump,Design,1,塔设备设计,Distillation Tower,Design,换热器设计,Heat Exchanger,Design,2,反应器设计,Reactor,Design,3,工艺介绍节能降耗,Conserve Energy,工艺设计,Process Design,设备设计,Equipment Design,自动控制,Automatic Control,27,机械校核,Mechanical checking,采集数据，分析任务,Collect Data&Task,Analysis,对比选型,Contrast Selection,结构设计,Mechanical,Design,设备设计,Equipment Design,工艺介绍,Aspen Plus,KG-TOWER,SW6-98,GB150-2011,钢制压力容器,Aspen Exchanger Design Rating智能选泵,Cup-TOWER,机械设计手册,化工工艺,设计手册,33,28,项目,结果,操作压力,/MPa,1.6,操作温度,/,260,气体流速,/m/s,0.47,列管长度,/m,7,列管数,/,根,6055,反应器直径,/mm,3400,反应器总高度,/m,11.8,工艺介绍,设备设计,Equipment Design,脱水反应器,脱水反应器设计参数表,Design parameters of dehydrogen reactor,项目,结果,设计压力,(MPa),1.6,设计温度,(),170,实际塔板数（块）,40,塔径（,m,）,3,塔高（,m,）,28.62,二甲醚分离塔,工艺介绍,设备设计,Equipment Design,29,二甲醚分离塔设计参数表,Design parameters of dimethyl-ether separation tower,30,分散控制,Decentralized Control,集中管理,Centralized Management,DCS,节能降耗,Conserve Energy,工艺设计,Process Design,自动控制,Automatic Control,设备设计,Equipments Design,工艺介绍,工艺介绍,自动控制,Automatic Control,压缩机防喘振控制,换热器控制,精馏塔控制,自动控制Automatic Control,反应器控制,进料控制,温度控制,压力控制,工艺介绍,环境影响评价,Environmental Impact Assessment,三废处理,Waste treatment,环境风险评估,Environmental Risk Assessment,环境现状,Present environment status,施工期环境评价,Environment impact,during,construction,period,生产期环境评价,Environment impact,during production period,环境保护,Environment Protection,工艺介绍,33,34,进入焚烧炉,少量,C,1,-C,5,、氢气组成,芳烃分离工段,废气,环境保护,Environment Protection,工艺介绍,运返生产厂家,回收利用,失效催化剂,反应器,废渣,三效蒸发器,碱性液体,芳构化工段,废液,35,环境保护,Environment Protection,工艺介绍,节约蒸,汽,63%,易爆除静电,泄露防蔓延,危险易疏散,易燃防火焰,罐区防火堤 消防泡沫站,管壁阻燃层,尾气烧作烟,罐薄避雷针,罐厚接地线,地面防火花,入区除静电,隔墙加围堰,装卸用软管,温压液位线,报警看得见,风向标在上 指示牌在前,上风口处走 防护措施全,36,安全生产,Safe,Production,工艺介绍,银川,厂区及车间布置,37,厂区布置,Plant Arrangement,车间布置,Workshop Arrangement,厂址选择,Plant Location,地理优越,.,煤矿资源丰富,.,水资源丰富,交通便利,.,两大运输网络发达,.,规划煤化工产品长输管道,政策支持,.,十二五规划提倡煤化工,.,财税政策，提供保障资金,园区配套,.,基地列为全国重点扶持项目,.,公用工程配套完善,38,厂址选择,Plant Location,厂区及车间布置,厂区及车间布置,厂区布置,车间布置,Workshop Arrangement,厂址选择,Plant Location,Plant Arrangement,39,辅助生产区,Supplementary Manufacturing Areas,行政区,Administrative Areas,储运区,Storage Areas,生产区,Apparatuses Areas,发展用地,Development Areas,来自总厂甲醇,管廊,消防站,人流线,物流线,物流线,39,40,厂区布置,Plant Arrangement,厂区及车间布置,芳构化车间布置图,厂区及车间布置,厂区布置,Plant Arrangement,车间布置,厂址选择,Plant Location,Workshop Arrangement,41,异构化车间布置图,厂区及车间布置,车间布置,Workshop Arrangement,42,烷基化车间布置图,厂区及车间布置,车间布置,Workshop Arrangement,43,经济分析,成本估算,Cost Estimation,财务评价,Financial Evaluation,投资估算,Investment Estimation,不确定性分析,Uncertainty Analysis,44,总投资,10.9,亿元,Total investment,固定资产,8.3,亿元,Capital asserts,流动资,金,1.5,亿元,Current assets,建设期利息,1.1,亿元,Interest,i,ncurred,d,uring construction,13.7,%,流 动 资 产,1,0.5,%,建 设 期 利 息,71.3,%,固 定 资产,固定成本,Fixed Cost,可变成本,Variable Costs,3.64,亿元,经济分析,财务评价,Financial Evaluation,投资估算,Investment Estimation,不确定性分析,Uncertainty Analysis,成本估算,Cost Estimation,23.2,亿元,45,总成本,26.84,亿元,Total Cost:,2.684 billion yuan,经营成本,23.4,亿元,Operating,C,osts,:2.34 billion yuan,经济分析,成本估算,Cost Estimation,投资估算,Investment Estimation,财务评价,Financial Evaluation,不确定性分析,Uncertainty Analysis,46,47.6,亿元,投资,利税率,资本金,利润率,静态,分析,投资,利润率,投资,回收期,5.,6,年,38.5,%,38.88,%,32.7,%,47,26%,38%,25%,经济分析,财务评价,Financial Evaluation,47,内部收益率,IRR,净现值,NPV,动态投资,回收期,PBT,动态分析,Dynamic Analysis,5.1,年,26%,14%,9.7,亿元,48,经济分析,财务评价,Financial Evaluation,经济分析,盈亏平衡点BEP,亏损区,盈利区,盈亏,平,衡点：,6.9,万吨,设,计,产能,：,25,万吨,生产能力,利用率：,27.6,%,盈亏平衡分析图,49,成本估算,Cost Estimation,投资估算,Investment Estimation,不确定性分析,Uncertainty Analysis,财务评价,Financial Evaluation,对,净现值影响：销售价格经营成本建设期投资敏感性分析图,经济分析,不确定性分析,Uncertainty Analysis,50,经济分析,经济总结,Economic Summary,3,整合全国过剩的甲醇资源，确保原料甲醇的供应,Integrate The Methyl alcohol Resources In Ningxia to Guarantee,The Supplication of That,.,2,与园区内下游,PTA,企业,签订协议供货,，,充分保证销路,Sign an Agreement With Other Companies Producing PTA to Guarantee,The Market Fully,1,PX,价格在受市场影响的同时受总厂的调控波动较小,The Price of PX Is Affected by The Markets,But That Is Not So Related,With The General Factory,.,51,热泵精馏技术,Heat,pump distillation,technology,废,热回收装置,waste heat recovery unit,以煤制甲醇为原料,From coal to methanol as raw materials,产品原料创新,Innovation of Product Structure,分隔壁精馏塔,divided wall column,过程节能降耗创新,Innovation of Energy Saving,Process,环境保护技术创新,Innovation of Environmental Technology,项目总结,Summary,项目总结,52,分离技术创新,Innovation of Separation Technology,Risk system,环境风险评价,Environmental Risk assessment,经济评价,Economicassessment,53,项目总结,总结,Summary,解决措施,加强舆论引导,开展科普活动,邀请群众参观,甬碳调团队,YTD Group,Ningbo University of Technology,宁波工程学院,54,请评委老师点评及指导！,Thanks,