高品质庚烯的工艺流程优化设计PPT课件.ppt

Click to edit Master text styles,Second level,Third level,Fourth level,Fifth level,.,*,Click to edit Master title style,高品质庚烯的工艺流程优化设计,设计：李宁 陈燕舞,指 导：李 秀 喜,Contents,项目背景,1,项目设计任务,2,设计方案,3,反应过程设计,4,分离过程设计与优化,5,过程模拟与优化,6,流程经济分析,7,2,.,1.,项目背景,庚烯的应用,用作高密度聚乙烯,HDPE,和线型低密度聚乙烯,LLDPE,生产的共聚单体,脂肪醇的中间体：庚烯,-,直链庚醇（增塑剂中间体）,-,邻苯二甲酸酯增塑剂,汽油添加剂（解决新标准汽油的辛烷值问题）,制备高级脂肪酸：聚,烯烃,(PAO),，优质合成润滑油,3,.,1.,项目背景,庚烯的制备方法,萃取分离法,（,）,正构烷烃热裂解法,（,）,脂肪醇脱氢法,（,）,低分子烯烃共聚法：,Dimersol,法和,Lewis,酸法,4,.,2.,项目设计任务,产量规模,27000,吨,/,年,产品纯度要求,99.8,产品要求,5,.,3.,设计方案选择,反应,原料,产品性质与市场,选用,Dimersol,法制备庚烯,（,1,）成分,（,2,）性质：易燃易爆，分离困难,（,3,）价格,（,1,）性质,（,2,）价格,6,.,选用原料,成分,工业丙烯：丙烯,95.23,丙烷,4.77,工业丁烯：已丁烷,18.38,正丁烷,21.83,异丁烯,5.67,正丁烯,55.73,正己烯,0.09,价格,丙烯,9000,元,/,吨,丁烯,6000,元,/,吨,高纯庚烯,13000,元,/,吨,高纯己烯,11000,元,/,吨,高纯辛烯,9000,元,/,吨,高纯癸烯,7000,元,/,吨,液化石油气,5500,元,/,吨,7,.,4.,反应过程设计,2,3,1,反应器的设计,确定反应物的组成,反应条件的选择,压力,温度,反应方式,8,.,4.,反应过程设计,反应器设计,图,1,丙烯与丁烯合成,1,庚烯生产装置,9,.,（,1,）确定反应物的组成,当进料丙烯丁烯含量比,(mol),为,4:1,时庚烯的选择性最大。但是综合考虑经济性与反应率，我们选择进料中丙烯丁烯的含量比（,mol,）为,2:3,，转化为工业丙烯与工业丁烯的摩尔比值约为,2:5,。,丙烯：丁烯,（,mol,）,1:1,1:2,3:2,7:3,4:1,2:3,3:7,反应选择性,0.0519,0.0713,0.0555,0.0616,0.0730,0.0709,0.0589,表,2,丙烯与丁烯不同配比下的反应选择性,10,.,（,2,）反应条件,连续式工艺,反应器条件,进料压力,8.5bar,进料温度,25,反应器温度,45,11,.,5.,分离过程设计与优化,12,.,（,1,）分离工艺的设计,庚烯合成的,BFD,13,.,（,1,）分离工艺的设计,1-,庚烯合成的,CFD,流程图,14,.,（,2,）换热工艺的设计,节能策略：将分离塔,T2,、分离塔,T3,的产品庚烯和己烯（均为,103,）作为反应器出口换热器的热流体对反应后的总物流进行预热，使其进料温度保持在,70,左右，采用双管程进料的换热器。,15,.,（,3,）工艺的过程模拟及优化,建立整体的合成模型,Aspen,模拟流程图,16,.,（,4,）反应转化率与选择性,主要反应选择性表,17,.,（,4,）反应转化率与选择性,本设计采用的原料和反应后产物的摩尔比与摩尔流量,18,.,6.,过程模拟和优化,分离塔,T1,的设计与优化,分离塔,T2,的设计与优化,分离塔,T3,的设计与优化,分离塔,T4,的设计与优化,19,.,（,1,）分离塔,T1,的设计与优化,目的：将,C4,及更轻组分与重组分分离。,关键组 分：己烯与正丁烷（,0.5,）,优化分离要求：己烯的回收率,0.99,塔釜正丁烷含量低于,0.001,灵敏度分析确定理论塔板数和最佳进料板,理论塔板数,23,进料位置,11,塔顶压力（,bar,）,6,塔底压力（,bar,）,8,塔顶温度（）,48.49,塔底温度（）,182.59,冷凝器负荷,（,MMkcal/hr,）,-0.9296635,再沸器负荷,（,MMkcal/hr,）,1.55832676,蒸出率,0.67,回流比,3.5,Aspen,模拟塔,T1,结果,20,.,（,1,）分离塔,T1,的设计与优化,T1,的理论塔板数及回流比,VARY 1,塔顶热量（,MMKCAL/H,）,塔釜热量（,MMKCAL/H,）,总的热量,9,-0.92967,1.55836586,2.488036,10,-0.9296539,1.55834487,2.487999,11,-0.9296635,1.55832676,2.487990,12,-0.9297172,1.55829341,2.488011,13,-0.929885,1.55820606,2.488091,14,-0.9303657,1.55795775,2.488323,15,-0.9316799,1.5572728,2.488953,21,.,（,2,）分离塔,T2,的设计与优化,目的：将己烯与其他重组分分离。,关键组分：己烯与庚烯,优化分离要求：塔顶庚烯含量,0.05%,塔顶己烯含量,99.9,22,.,（,2,）分离塔,T2,的设计与优化,Aspen,模拟塔,T2,结果,理论塔板数,50,进料位置,25,塔顶温度（）,122,6,塔底温度（）,212,9,冷凝器负荷（,MMkcal/hr,）,-0.9296635,再沸器负荷（,MMkcal/hr,）,0.81229758,蒸出率,0.67,回流比,3.5,23,.,（,2,）分离塔,T2,的设计与优化,T2,的理论塔板数及回流比,VARY 1,塔顶热量（,MMKCAL/H,）,塔釜热量（,MMKCAL/H,）,总的热量,(MMKCAL/H),19,-0.7365898,0.81238544,1.548975,20,-0.7365419,0.8123507,1.548893,21,-0.7365135,0.81233039,1.548844,22,-0.7364931,0.81231549,1.548809,23,-0.73648,0.81230587,1.548786,24,-0.7364726,0.8123004,1.548773,25,-0.7364689,0.81229758,1.548766,26,-0.7364707,0.81229872,1.548769,27,-0.7364893,0.81231213,1.548801,28,-0.7365887,0.81238412,1.548973,29,-0.7367975,0.81253551,1.549333,30,-0.7370485,0.81271462,1.549763,31,-0.7373614,0.81293382,1.550295,24,.,（,3,）分离塔,T3,的设计与优化,目的：将庚烯与催化剂及重组分分离。,关键组分：庚烯与辛烯,优化分离要求：庚烯产品纯度达到,0.999,塔釜庚辛烯含量小于,0.05,25,.,（,3,）分离塔,T3,的设计与优化,Aspen,模拟塔,T3,结果,理论塔板数,55,进料位置,30,塔顶温度（）,157,4,塔底温度（）,258,7,冷凝器负荷（,MMkcal/hr,）,-0.8825683,再沸器负荷（,MMkcal/hr,）,0.82448397,蒸出率,0.66,回流比,2,86,26,.,（,3,）分离塔,T3,的设计与优化,T3,的理论塔板数及回流比,VARY 1,塔顶热量（,MMKCAL/H,）,塔釜热量（,MMKCAL/H,）,总的热量,26,-0.8827832,0.82467827,1.707461,27,-0.882686,0.82459024,1.707276,28,-0.8826169,0.82452772,1.707145,29,-0.8825763,0.82449099,1.707067,30,-0.8825683,0.82448397,1.707052,31,-0.8826195,0.82452967,1.707149,32,-0.8827666,0.82466314,1.70743,33,-0.8832925,0.82513863,1.708431,34,-0.8866168,0.82814342,1.71476,35,-0.8992519,0.83960126,1.738853,36,-0.9169118,0.855661,1.772573,27,.,（,4,）分离塔,T4,的设计与优化,目的：将重组分中的辛烯与癸烯分离。,关键组分：辛烯与癸烯,优化分离要求：辛烯产品纯度大于,99.7%,塔顶,C11,含量小于,0.05%,。,28,.,（,4,）分离塔,T4,的设计与优化,Aspen,模拟塔,T4,结果,理论塔板数,23,进料位置,14,塔顶温度（）,193,0,塔底温度（）,273,8,冷凝器负荷（,MMkcal/hr,）,-0.1878422,再沸器负荷（,MMkcal/hr,）,0.147406,蒸出率,0.55,回流比,1,68,29,.,（,4,）分离塔,T4,的设计与优化,T4,的理论塔板数及回流比,VARY 1,塔顶热量（,MMKCAL/H,）,塔釜热量（,MMKCAL/H,）,总的热量,9,-0.1881759,0.14760079,0.335777,10,-0.1879735,0.14748275,0.335456,11,-0.1878916,0.14743493,0.335327,12,-0.1878591,0.14741595,0.335275,13,-0.1878465,0.14740856,0.335255,14,-0.1878422,0.147406,0.335248,15,-0.1878473,0.14740897,0.335256,16,-0.1883718,0.14771473,0.336087,30,.,（,5,）最终物流组分组成结果,最终各物流组分组成结果,1,2,3,4,5,6,7,8,9,10,Temperature C,25,45,48.81,180.96,123.19,212.78,157.44,258.61,193.03,273.64,Pressure bar,8,8,6,8,5,7,5,7,5.5,6,C3H8,0.01339613,0.01823058,0.02680968,1.5455e-09,6.2795e-09,1.2431e-30,0,0,0,0,C3H6-2,0.26725463,0,0,0,0,0,0,0,0,0,C4H10-2,0.13222423,0.17994181,0.26461866,3.505e-06,1.424e-05,4.883e-22,0,0,0,0,C4H10-1,0.14478519,0.19703583,0.28974534,2.8097e-05,0.00011415,2.7376e-19,0,0,0,0,C4H8-5,0.04078973,0.05551009,0.08163144,2.2255e-06,9.042e-06,1.2852e-21,0,0,0,0,C4H8-1,0.40088194,0.22385888,0.32919926,1.0594e-05,4.3044e-05,9.1006e-21,0,0,0,0,C6H12-3,0.00066813,0.08456082,0.00799206,0.24726945,0.99969003,0.00161785,0.00243668,3.8131e-10,6.9525e-10,2.1109e-15,C7H14-7,0,0.1600291,3.5521e-06,0.50008338,0.00012947,0.66330921,0.999029,0.00394789,0.00719744,1.0377e-06,C8H16-16,0,0.04446263,1.6021e-10,0.13894572,1.4069e-11,0.18430896,0.00053431,0.54740967,0.99277686,0.00647076,C11H22-2,0,0.03637024,7.8834e-22,0.11365703,2.7205e-30,0.15076398,2.3302e-23,0.44864243,2.5697e-05,0.9935282,分离出的庚烯达到,99.9wt%,，符合设计要求,31,.,7.,流程的经济技术分析,项目建设投资估算,建设投资估算表（单位：万元人民币）,工程费用,建筑工程费,950,设备及器具购置费,6870,安装工程费,500,预备费,基本预备费,932,涨价预备费,400,工程建设其它费用,土地使用费、管理费与临时设施费等,1000,建设期利息,532,合计,11184,32,.,7.,流程的经济技术分析,损益和利润分配,损益和利润分配表（单位：万元人民币）,项目,合计,建设期,生产经营期,1,2,3,4,5,6,生产负荷,75%,100%,100%,100%,100%,产品销售收入,516264,81516,108688,108688,108688,108688,销售税金及附加,25813,4076,5434,5434,5434,5434,总成本费用,460778,72786,96848,96848,96848,96848,利润总额,29673,4654,6406,6406,6406,6406,税后利润,25222,3956,5475,5475,5475,5475,可分配利润,21974,3362,4653,4653,4653,4653,累计未分配利润,21974,3362,8015,12668,17321,21974,静态法投资回收期约为,3.02,年 项目的投资利润率为,57%,，,33,.,致谢,本设计在化学与化工学院李秀喜老师的指导下完成，在设计过程中得到各位同学的大力帮助，在此表示衷心感谢！,34,.,Thank You!,