广东石油化工学院跬步千里6设计说明书附录

1、70 万吨/年组合工艺清洁生产对二甲苯项目设计2014 年“中国-三井化学杯”第八届大学生化工设计竞赛设计说明题目：70 万吨/年组合工艺清洁生产书对二甲苯附录项目设计环境预评价参赛学校：石油化工学院团队名称：跬步千里团队成员：邓清文、郭 阳、余诗虎、 江衍梁、林晓元指导：陈 辉设计时间：2014.42014.7不积跬步，无以至千里。荀子·劝学170 万吨/年组合工艺清洁生产对二甲苯项目设计2014 年“恒逸-三井化学杯”第八届大学生化工设计竞赛题目：70 万吨/年组合工艺清洁生产对二甲苯项目设计设计说明书附录参赛学校：石油化工学院团队名称：跬步千里团队成员：邓清文、郭阳、余诗虎、江

2、衍梁、林晓元指导：陈 辉、黄燕青、刘宝生、谢颖、梁朝林设计时间：2014.42014.7初步设计说明书附录·跬步千里目录第 1 章 物料衡算11.1 物料衡算的意义11.2 物料衡算遵循的原则11.3 物料衡算11.3.1总物料衡算21.3.21.3.3抽提单元4甲苯歧化与烷基转移与择形歧化组合工艺单元81.3.41.3.51.3.6精馏单元10异构化单元14吸附分离单元18第 2 章 能量衡算222.1 能量衡算的意义222.2 能量衡算的原则222.3 能量衡算222.3.12.3.2抽提单元22组合工艺单元242.3.32.3.42.3.5精馏单元27异构化单元29吸附分离单元

3、32第 3 章 能量集成353.1 概述353.2 换热网络设计结果353.2.1物料流股提取353.2.23.2.3夹点的确定36换热网络设计37第 4 章 塔设备的选型和设计394.1 概述39170 万吨/年组合工艺清洁生产对二甲苯项目设计4.2塔设备选型394.2.14.2.24.2.3依据39原则39塔型选择404.2.4板式塔塔盘选择40非芳烃蒸馏塔（T104）设计414.34.3.14.3.2流体力学数据41塔体工艺设计414.3.34.3.44.3.54.3.64.3.74.3.84.3.9塔板工艺设计43流体力学检验46塔板负荷性能图48设计计算结果50塔附件设计52塔体总高

4、度53塔体重量544.4塔设备一览表56第 5 章 反应器的选型和设计585.1概述58反应器类型58传统歧化反应器设计605.25.35.3.15.3.25.3.35.3.4反应条件60反应器结构的计算61强度计算和校核63反应器高度的确定645.3.55.3.6反应器接管内径的计算64反应器支座的设计655.3.7烃化反应器工艺及强度计算结果665.4择型歧化反应器设计672初步设计说明书附录·跬步千里5.4.15.4.25.4.35.4.4反应条件67反应器结构的计算67强度计算和校核69反应器高度的确定715.4.55.4.6反应器接管内径的计算71反应器支座的设计715.4

5、.7烃化反应器工艺及强度计算结果725.5异构化反应器设计735.5.15.5.25.5.35.5.45.5.55.5.65.5.7反应条件73反应器结构的计算74强度计算和校核76反应器高度的确定77接管内径的计算78反应器反应器支座的设计78烃化反应器工艺及强度计算结果795.6反应器一览表80第 6 章 换热器的选型和设计826.1概述82换热器类型82选型原则83换热器的选型计算856.26.36.46.4.16.4.26.4.3贫溶剂水冷器 E10585分馏塔进料加热器 E10189预分馏塔塔底再沸器 E103936.5换热器一览表97第 7 章 泵的选型和设计1037.1 概述10

6、37.2 泵的类型103370 万吨/年组合工艺清洁生产对二甲苯项目设计7.3 选型依据及原则1037.3.1 依据1037.3.2 原则1047.4 泵的选型计算1057.5 泵一览表110第 8 章 压缩机的选型和设计1158.1概述115压缩机类型1158.28.3选型原则116压缩机选型计算117压缩机一览表1198.48.5第 9 章 储罐的选型和设计120概述120选型原则120对二甲苯罐设计1219.19.29.39.3.19.3.2对二甲苯基本性质121储罐的选型1229.3.3储罐体积计算1229.4苯塔回流罐设计1229.4.1 工艺基本参数1229.4.2 回流罐体积计算

7、122气液分离罐设计123储罐一览表124管道的选型和设计1279.59.6第 10 章10.1 管道选型依据12710.2 设计要求12710.3 管道选型方法12810.3.1 流速的确定1284初步设计说明书附录·跬步千里10.3.2 管径的确定12910.3.3 公称直径及管道壁厚的确定13010.4 管道一览表130阀门设计选型176第 11 章11.1阀176旁路阀和阀17611.211.3放空阀176阀门计算17611.411.5阀门一览表177第 12 章主要物料 MSDS19112.1 概述19112.2 主要物料 MSDS19112.2.112.2.212.2.3

8、苯191邻二甲苯195对二甲苯19812.2.412.2.5甲苯203氢气20712.2.6一氧化碳210570 万吨/年组合工艺清洁生产对二甲苯项目设计第1章 物料衡算1.1 物料衡算的意义在化学工程中，设计或改造工艺流程和设备、了解和生产操作过程、核算生产过程的效益、确定原材料消耗定额、确定生产过程的损耗量、对现有的工艺过程进行分析、选择最有效的工艺路线、对设备进行最佳设计以及确定最佳操作条件等都要进行物料衡算。而且，化学工程的开发与放大都以物料衡算为基础的。物料衡算是质量守恒定律的一种表现形式。凡引入某一设备的物料成分、质量或体积等于操作后所得产物的成分、质量或体积加上物料损失。1.2

9、物料衡算遵循的原则物料衡算的理论基础是质量守恒定理。它是研究某一体系内进出的物料量及组成的变化情况。进行物料衡算时，必须先确定衡算的体系。对一般体系，均可用如下表示：系统中的积累输入输出生成消耗在稳定状态下有：输入输出生成消耗特别地，当系统没有化学反应时，则可简化为：输入输出1.3 物料衡算的步骤（1）确定衡算范围，画出衡算示意图，标明各股物料的方向及组成。（2）定出衡算基准，对连续操作常以时间为基准如：kg/h，件/h，t/h；对间歇操作，常以一批物料（即一个操作循环为基准）。基准选定后，各流股按所选基准进行计算。1.3 物料衡算1初步设计说明书附录·跬步千里本项目利用 C7+重整

10、油和乙烯 C8 芳烃及乙烯甲苯，乙烯厂氢气生产对二甲苯。整个流程分为 5 个单元：抽提单元、甲苯歧化与烷基转移与择形歧化组合工艺单元、精馏单元、异构化单元、吸附分离单元。现对整个流程和 5 个单元进行物料衡算。1.3.1 总物料衡算本工艺项目的系统总物料衡算结果见表 1-3-1-1 和表 1-3-1-2。表 1-3-1-1流入系统物料汇总2ITEMINC7+重整油乙烯甲苯乙烯C8芳烃氢气解吸剂+水环丁砜+水Temperature （ ）431554040177124Pressure（MPa）0.1012.450.1011.030.951.6Vapor Frac000100Mole Flow （

11、kmol/hr）963.133147.376127.125901.317411.2884546.076Mass Flow（kg/hr)10625013587.5135001816.94855108531250Total（kg/hr）721512.44870 万吨/年组合工艺清洁生产对二甲苯项目设计表 1-3-1-2流出系统物料汇总由表 1-3-1-1 和表 1-3-1-2 可系统流入流出总物料平衡3ITEMOUTPX择形歧化苯传统歧化苯抽余油工业氢废水废解吸剂其他烯烃Temperature（ ）4090904343406060195Pressure（MPa）0.1010.150.120.20.

12、3150.30.170.1012.45Vapor Frac000010000MoleFlow（kmol/hr）831.53975.15318.41675.2572278.615148.1490.014740.5687.773Mass Flow（kg/hr)88281.6565870.4851354.5917654.6486551.8382668.9531.329608932.932195.691Total（kg/hr）721512.448初步设计说明书附录·跬步千里1.3.2 抽提单元抽提单元 Aspen 流程图见图 1-3-2-1。抽提单元物料衡算结果见表 1-3-2-1图 1-3

13、-2-1抽提单元 Aspen流程图470 万吨/年组合工艺清洁生产对二甲苯项目设计表 1-3-3-1抽提单元物料衡算结果5ITEMINOUTC7-芳烃和非芳烃环丁砜循环环丁砜抽余油芳烃水Temperature C9087160.243.05220614043Pressure bar6.8120.220.40.18Vapor Frac000000Mole Flow kmol/hr284.41334546.075764393.60175.2565898214.301322147.33Mass Flow kg/hr26948.01531250527986.3647654.6483419902.789

14、2654.20866Volume Flow cum/hr36.26271439.342109510.14411.366930323.1369618EnthalpyGcal/hr-2.60294-461.12011407.247-3.97183380.13531823-10.842Mass Flow kg/hrBENZENE21.2500.2837873320.9661634.82E-05N-HEP-016141.2506140.1624400.00141METHY-01456.87220456.720774.9306e-080.000498TOLUE-0119149.4100.76719615

15、19148.64493.35E-05N-OCT-011104.99201055.303314.333e-096.13E-05CYCL0.00673700.000541463.69e-052.21E-10EB31.3946103.2601e-0631.3946124.41E-11P-XYL-0114.2915301.3551e-0614.29153412.02E-11初步设计说明书附录·跬步千里6M-XYL-0125.405101.3803e-0625.40511041.77E-11O-XYL-013.02196806.4425e-093.021968619.67E-14NONANE0

16、.02808100.0014359007.99E-09N-PRO-010.0011304.0654e-052.0304e-074.73E-07ISOPR-010.01255905.5477e-110.012558852.25E-16N-PROPY0.004653000.0046525301:3:5-010.003888000.0038882801,2,3-TR7.23E-05007.2322e-0501,2,4-TR0.000318000.0003181901-METH-30.024863000.0248627601-MET-010.002181000.002181300N-DEC-014.4

17、6E-0501.5535e-0803.14E-152:2-D-010.00097301.0305e-0504.29E-07N-BUT-011.74E-0604.2705e-101.6466e-074.47E-121-MET-026.44E-07006.4342e-070.00E+001:2:4-015.13E-07005.0093e-070.00E+00NAPH6.53E-10004.4079e-100.00E+00STY0.037923000.037922610SULFO-015.641e-08528593.755.641e-08658.333229070 万吨/年组合工艺清洁生产对二甲苯项

18、目设计由表 1-3-2-1 可知抽提单元物料平衡。7WATER1.408792122656.251.408792120.645013112654.20866Total（kg/hr）558198.0155198.01初步设计说明书附录·跬步千里1.3.3 甲苯歧化与烷基转移与择形歧化组合工艺单元歧化单元 Aspen 流程图见图 1-3-3-1。歧化单元物料衡算结果见表 1-3-3-1。图 1-3-3-1歧化化单元 Aspen流程图表 1-3-3-1歧化单元物料衡算结果8ITEMINOUTE206-INV205-OUTC203-OUTTemperature C97.64060Pressu

19、re bar15.1336.7Vapor Frac0.4080.0031Mole Flow kmol/hr743.517457.019248286.462217Mass Flow kg/hr42119.17541524.2991594.875281Volume Flow cum/hr657.80551.9048922219.827068EnthalpyGcal/hr2.8881.617704120.05366513Mass Flow kg/hrBENZENE67.05973045923.963130N-HEP-01000METHY-01000TOLUE-0141378.505427889.45

20、010N-OCT-0100070 万吨/年组合工艺清洁生产对二甲苯项目设计9CYCL000EB3.4668446241.8553530P-XYL-0115.49378647166.68430M-XYL-012.89451491145.696060O-XYL-012.7211999651.21740270NONANE6.799563916.799563870N-PRO-016.793750526.793750520ISOPR-01000N-PROPY0001:3:5-010001,2,3-TR0001,2,4-TR6.793755.1960248201-METH-30001-MET-016.79

21、3750016.793750010N-DEC-010002:2-D-016.79422266.79422260N-BUT-010001-MET-020001:2:4-01000NAPH000STY000SULFO-01000WATER000H2589.4715345.82125214576.303961CH4057.63591760C2H6000C6H14-16.793755395.441223410CO4.10352360.041035234.06248836CO26.44743570.064474356.38296134N28.207949640.082079498.12587014初步设

22、计说明书附录·跬步千里由表 1-3-3-1 可知，歧化单元物料平衡。1.3.4 精馏单元精馏单元 Aspen 流程图见图 1-3-4-1。精馏单元物料衡算见表 1-3-4-1。图 1-3-4-1精馏单元 Aspen 流程图10C3H800.695267680C3H6-100.66348340C6H12-10.033742001.472704360C10H14E66.011e-171.137988850Total（kg/hr）42119.17542119.174370 万吨/年组合工艺清洁生产对二甲苯项目设计表 1-3-4-1精馏单元物料衡算结果11ITEMINOUTT401-INT5

23、03-IN2M501-INT401-DT402-DE803-INA601-INT601-WTemperature100173.619992.2572183112.427053250.180064173.117895209.956373Pressurebar42.07211.41.013303949.11.51.76Vapor Frac01000000MoleFlowkmol/hr6580.543713367.49802677.46815118.4161983209.6414264027.973016165.65592203.823336Mass Flowkg/hr765366.08535821

24、9.17879171.60351450.9799519361.4502428115.261727355.20926473.9661VolumeFlowcum/hr963.01234356754.9201111.8874461.8121002424.8593998687.6126261004.0275236.7435753EnthalpyGcal/hr-51.85693135.3989619-0.93557290.247723451.3406988628.6767599-25.952745-1.3735188Mass Flowkg/hrBENZENE1357.30603107.1353272.4

25、219e-091354.591452.71458523107.13532700N-HEP-0103.366e-079.8098e-05009.8435e-0500METHY-011.5608e-071.642e-050.002757054.9428e-081.0665e-070.0027734700TOLUE-0119148.6449808.5071417.4677645195.743192719014.797854.0796087.9336e-081.7219e-15N-OCT-018.0016e-070.0898040910.63290646.7172e-107.6282e-0710.72

26、271053.84e-083.2327e-15CYCL16186.792147.2473458127.4932626.6964e-080.001325766.6705545716347.02157.83928617EB14681.7604152245.9665387.355370.00012013208.037891157488.2914618.64290.11098111P-XYL-0149502.794943679.90665723.208430.0001148199.005243882900.685715906.01950.1994543初步设计说明书附录·跬步千里12M-XY

27、L-0131699.3295113306.88112427.09484.8348e-0535.9676245131440.91925956.06140.35813756O-XYL-0152724.89643304.46427646.978024.3259e-060.7529247651657.886652014.93692.76190933NONANE1675.040893198.1427663.72191872.0044e-060.168552673233.620321703.053510.06318937N-PRO-015726.290486.7943857753.12386992.229

28、5e-080.000107820.000798915777.18629.0216284ISOPR-0141110.4362138.368932424.9874416.4831e-080.00067795139.09678541512.640122.0549534N-PROPY57201.90950.055748821274.995351.5795e-092.0072e-060.0556523158293.9467182.9582371:3:5-01118262.14473.81744816608.746118.0149e-111.6538e-080.00153238123495.5541449

29、.152051,2,3-TR9820.734132.699999723113.124938.4515e-156.8303e-145.0669e-1210151.46062785.098471,2,4-TR5888.34147.891458632220.624682.4184e-131.18e-112.8787e-087733.67771383.1798211-METH-3270773.8620.0717882912505.60012.2641e-091.5564e-060.07139495281923.0311356.431571-MET-0160406.85276.793375663325.

30、622825.5756e-111.2481e-081.058e-0562733.42511005.84372N-DEC-017776.553446.2333e-05106.2499554.4304e-112.8371e-096.1737e-057761.71465121.0887332:2-D-01668.974513279.2901037.436527361.9913e-070.00425754275.91576679.6920190.08910735N-BUT-0180.1624529053.12499832.7493e-151.2871e-141.1998e-1979.592599553

31、.69485171-MET-02126.9401090180.6249998.7857e-187.1664e-183.544e-17126.002221181.5628871:2:4-01125.247349016819.3755.9119e-223.4728e-243.8476e-25124.04793216820.5745NAPH0.0612017301083.753.2952e-294.4075e-331.9232e-370.060569541083.75063STY0.000192992.1279e-050.261299158.5817e-151.1362e-090.1062220.1

32、55280151.128e-05SULFO-010000000070 万吨/年组合工艺清洁生产对二甲苯项目设计由表 1-3-4-1 可知精馏单元物料平衡。13WATER0.645013110.0009070700.6450131100.0009070700C10H14-8420.3657751005.0534201.2285e-175.7912e-185.3069e-18417.2871871008.13201Total（kg/hr）1202756.8631202756.866初步设计说明书附录·跬步千里1.3.5 异构化单元吸附分离单元 Aspen 流程图见图 1-3-5-1。异构

33、化单元物料衡算结果见表 1-3-5-1图 1-3-5-1异构化单元 Aspen 流程图1470 万吨/年组合工艺清洁生产对二甲苯项目设计表 1-3-5-1异构化单元物料衡算结果15ITEMINOUTE802-INMAKEC8RECY-H2P803-OUTT804-DTO-T103DIRTY-WC801-OUTTemperature145.0706574080192.701233135.7112971104080Pressurebar7.21.0132510.320.72.83.8332Vapor Frac00101001MoleFlowkmol/hr3256.83452127.12478890

34、1.31743367.499047.0590617410.06211640.73745305901.334885Mass Flowkg/hr346380.301135001816.94772358219.284585.3179991005.7669413.28542322025.62021VolumeFlowcum/hr460.91284915.84033952580.94909513.24616380.2371661.284921710.01338736838.643296EnthalpyGcal/hr2.80180586-0.46554670.3444460611.87921890.141

35、234330.02958676-0.05014490.18930904Mass Flowkg/hrBENZENE105.87438700107.135327428.75658888.844447600N-HEP-019.8434e-07003.366e-073.8555e-072.622e-0700METHY-012.7735e-05001.642e-053.8532e-067.4611e-0600TOLUE-01876.50714165.3477478204.16575300N-OCT-010.10722699000.089804090.004062720.0133602900CYCL0.0

36、591636447.25047.24734580.000206710.0024475200EB157432.7117015.950152245.96657.956962436.48503600P-XYL-01179.9676161375.65043679.90669.4994842276.897821800初步设计说明书附录·跬步千里16M-XYL-01131475.3073578.850113306.88121.5750457178.92733200O-XYL-0151690.6471474.2043304.46421.7845927117.645026300NONANE3153.

37、84362003198.142760.332588892.7024707300N-PRO-016.79445786006.794385771.2076e-050.0001429700ISOPR-01125.04022800138.3689320.000534170.0065757700N-PROPY0.05075521000.055748823.0151e-084.6255e-07001:3:5-010.001379862.7073.81744818.9406e-060.00016577001,2,3-TR02.702.699999721.0206e-082.7037e-07001,2,4-T

38、R5.191463222.707.891458632.0367e-074.3979e-06001-METH-30.06437829000.071788292.4012e-083.9147e-07001-MET-016.79338663006.793375666.2286e-071.1499e-0500N-DEC-015.6388e-05006.2333e-051.0152e-111.6369e-10002:2-D-01303.2901030.008624670.0762917000N-BUT-01000000001-MET-02000000001:2:4-0100000000NAPH00000

39、000STY0.10382186000.106395483.0668e-063.15e-0500SULFO-010000000070 万吨/年组合工艺清洁生产对二甲苯项目设计由表 1-3-5-1 可知，异构化单元物料平衡。17WATER13.3378665000.000907070.051532021.4313e-1113.28542320C10H14-81005.05343001005.053424.3834e-071.369e-0500H2001816.9477200001800.37966CH4000000025.6430306C2H60000000199.597516C6H14-100

40、000000CO00000000CO200000000N200000000C3H800000000C3H6-100000000C6H12-100000000C10H14E61.8173e-060000001.8173e-06Total（kg/hr）361697.2487361697.249初步设计说明书附录·跬步千里1.3.6 吸附分离单元吸附分离单元 Aspen 流程图见图 1-3-6-1。吸附分离单元物料衡算结果见表 1-3-6-1。图 1-3-6-1吸附分离单元Aspen流程图1870 万吨/年组合工艺清洁生产对二甲苯项目设计表 1-3-6-1吸附分离单元物料衡算结果19ITE

41、MINOUTT703-INP710-OUTPXE802-INM703-INT706-WP705-OUTV703-OUTV702-H2OV703-H2OTemperature177178.114156158.366842145.070657196.2206.976703198.609577666066Pressurebar9.54.863.877.22.221.7424.31.51.081.5Vapor Frac0000000000MoleFlowkmol/hr946.8244213564.56332831.5202613256.83452304.4645030.00990128113.6189

42、311.603592710.018856070.06278055Mass Flowkg/hr103277.634387604.07888279.6589346380.30140865.57821.3289619114826.4974170.0075420.339697381.1310097VolumeFlow cum/hr144.720534541.520545120.397389460.91284957.83854150.0019111221.12930990.206235640.000345500.00118619EnthalpyGcal/hr0.780871066.652695550.5

43、96038582.80180586-1.7904055-5.002e-05-0.5124778-0.0063901-0.0012754-0.0042644Mass Flowkg/hrBENZENE1.07135327106.0639740.71793272105.874387004.2491e-090.3534201104.3367e-07N-HEP-019.745e-059.8435e-077.7234e-059.8434e-07007.8814e-122.0217e-0501.4279e-17METHY-010.002745732.7735e-050.002423052.7735e-050

44、04.4476e-090.0003226701.3364e-13TOLUE-018.84557585875.7120098.24131044876.1752057.8165e-1200.000108270.6041571101.1425e-08N-OCT-0110.61548340.1072271110.18535910.107226991.9077e-1400.000714950.4294093204.1379e-15CYCL6.603849030.066705542.032694230.059163642.3946e-095.3683e-184.570791940.0003628508.2

45、075e-14EB0157729.3960157432.7119.5043e-061.74e-160000P-XYL-0189877.1967180.11462388115.0385179.9676162.3034e-087.512e-191593.76713168.39105307.3715e-08初步设计说明书附录·跬步千里20M-XYL-01118.427794131468.01115.777012131475.3071.8426e-056.4537e-162.451203730.199578401.2275e-10O-XYL-0131.025460251678.074827.659017351690.6474.9684e-057.4405e-153.3