6-1、附录一物料平衡计算书

1、目录12总论111223334556777999111111121214161616算的方法 方程式物2.12.22.3物算的基准工艺流程图3各工段物算 3.1 丙烷脱氢工段3.1.13.1.2丙烷脱氢工段流程图丙烷脱氢工段物算分离精制工段分离精制工段流程图3.2.2 分离精制工段物算羰基羰基羰基工段工段流程图工段物算3.4 异构物分离工段3.4.13.4.2异构物分离工段流程图异构物分离工段物算3.5 醇醛缩合工段3.5.13.5.2醇醛缩合工段流程图醇醛缩合工段物算3.6 加氢精馏工段3.6.13.6.2加氢精馏工段辛烯醛加氢精馏工段4主要设备物算 4.1 反应器4.1.1 丙烷反应器（R

2、-104）4.1.24.1.34.1.4选择性加氢反应器（R-201）1718202122222325羰基反应器（R-302）醇醛缩合反应器（R-501）两相分离器塔设备-202）4.3.14.3.24.3.3丙烯精馏塔（T异构物分离塔（T-402）辛醇预蒸馏塔（T-603）1 总论物算是以质量守恒定律为基础对物料平衡进行计算，在工艺设计中，物算是在工艺流程确定后进行的。其在确定项目生产工艺及流程后，通过对整个生产系统、部分重要的生产单元进行物算计算出主、副产品的产量、原材料的消耗、生产过程中各阶段的消耗量以及产品收率等各项经济技术指标，进而定量地评价初步设计所选择的的工艺路线在技术及经济上的

3、合理性，为后续的热量、其他工艺计算及设备计算打下基础。2 物算的方法2.1方程式对一般的体系而言，物料分布均可表示为：（物料的累积率）=（物料进入率）-（物料流出率）+（反应生成率）-（反应消耗率）特别地，当系统没有化学反应时，则可简化为：（物料的累积率）=（物料进入率）-（物料流出率）在稳定状态下有：（物料进入率）=（物料流出率）物算包括总质量、组分和元素。各种方法的适用情况如下：表 2-1物算的适用范围由于项目过程中存在化学反应故主要采用总质量方法，主要采用总质量的方法，同时列出每种组分的质量流量以便于查找和计算。类别物算形式无化学反应有化学反应总式总质量式适用适用总物质的量式适用不适用组

4、分式组分质量式适用不适用组分物质的量式适用不适用元素原子式元素原子质量式适用适用2.2 物算的基准1、对于间歇式操作的过程，常采用一批原料为基准进行计算。2、对于连续式操作的过程，可以采用时间产品数量或原料量为基准进行计算。物算的结果应列成原材料消耗及消耗量表。3、消耗是指以每年或是指每吨产品或以一定量的产品所消耗的原材料量；而消耗量等时间所消耗的原材料量。4、制剂车间的消耗起算入。及消耗量计算时应把原料、辅料及主要包装材料一物算的主要任务如下：1、保证主要产品丁辛醇质量合格。2、确定对环境有危害的工业三废的含量，并确定处理措施。3、各主要单元过程的物算，并指导工艺设备的尺寸确定。4、汇总全流

5、程物算，数据用于完成物料流程图等后续设计任务。2.3 工艺流程图本项目用丙烷、气为原料，Pta/SAPO-34（硅磷铝系列的分子筛）催化剂、三苯基膦氯化铑催化剂、固体碱Ca/Al2O3 催化剂、Cu-Zn-Al催化剂等等为辅助原料，设计年产 46 万吨丁辛醇，整个工艺流程由丙烷脱氢工段、分离精制工段、羰基工段、异构物分离工段、醇醛缩合工段、加氢精馏工段六个工段组成。图 2-1工艺流程示意图3 各工段物算3.1 丙烷脱氢工段3.1.1 丙烷脱氢工段流程图图 3-1丙烷脱氢工段流程图3.1.2 丙烷脱氢工段物算表 3-1消耗表 3-2相关物理化学常数其余物性数据选用 AspenplusV8.0 中

6、自带的物性数据库和整合的企业数据库。以 AspenPlus8.0 的模拟数据为依据得到的物算的结果详见下表：（注：下列表格中0.001 表示 10-310-6；TRACE 表示痕量级 10-610-9）表 3-3丙烷脱氢工段流股物料模拟结果ItemsInputOutputXSJC3H8H2ORECYCLE1C-H2OF1Temperature/25253021.52525Prere/bar1.51.51.58.51.51.5Vapor Frac110001Mole Flow kmol/hr5105980097.722766.0012339.249Mass Flow kg/hr10.079466

7、14.0514412.224221.09213799.7451457.71Volume Flow cum/hr82.70817093.2519.1389.06318.2638463.52Enlpy MMBtu/hr0.001-105.119-218.698-11.67-209.71815.038Mole Flow kmol/hr名称数值摩尔气体常数R=8.31433J/（molK）标准大气压1atm=101.325Kpa伽常数N=6.0220451023mol-1冰点温度0=275.15K标准状态下气体摩尔体积（275.15K，101.325Kpa）V=22.4138310-3m3/mol消耗

8、吨/年丙烷370000.0Pta/SAPO-34 催化剂（硅磷铝系列的分子筛）23.17表 3-4丙烷脱氢工段物算表3.2 分离精制工段3.2.1 分离精制工段流程图图 3-2分离精制工段流程图Mass-flow kg/hrSummationInput65257.448Output65257.449Rel.diff-1.53239E-08C3H801053094.13344.45E-06108.8393C2H60601.75E-271.94E-065.763574H25004.52E-973.77E-051101.863CH400001.13E-0546.66489C3H60000.12123

9、70.000158933.4191C3H40000.1168820.00046158.44755C2H40002.93E-401.19E-070.234642C2H20005.63E-290.00027946.6664H2O008003.35007476637.350083.2.2 分离精制工段物算表 3-5分离精制工段流股物料模拟结果表 3-6 分离精制工段物算Mass-flow kghrSummationInput51578.665ItemsInputOutputF1H2SIS2FLH2T201-DRECYCLE1C3H6Temperature/252540-146.8-146.8-51.

10、521.58.2Prere/bar1.51211.2101098.57.5Vapor Frac1100.0091101Solid Frac00000000Mole Flowkmol/hr2339.249603421.471091.888.20697.7221007.726Mass Flowkg/hr51457.71120.953612.52364.7292200.9381818.2634221.09242361.123Volume Flowcum/hr38463.52124.8730.8191.0611150.696165.3889.0632721.604EnlpyGcal/hr3.790.0

11、01-2.335-0.414-1.2671.853-2.9413.967Mole Flow kmol/hrC3H8108.8393000.05542402.58E-1094.133414.65049C2H65.763574000.05874405.5777311.75E-270.1270994H21101.8636000.2555671091.89.80784.52E-971.675677CH446.664890020.07277026.5921200C3H6933.4191000.69314306.04E-080.121237990.9291C3H458.44755000.00634306.

12、48E-150.1168821.81E-09C2H40.234642000.00597600.2286642.93E-401.16E-06C2H246.6664000.322245046.000115.63E-290.3440509H2O37.350080347.87E-0603.47E-283.3500741.58E-263.3 羰基工段3.3.1 羰基工段流程图图 3-3羰基工段流程图3.3.2 羰基工段物算表 3-7羰基工段流股物料模拟结果ItemsInputOutputC3H6RECYCLE4SJCHJT301-DRECYCLE3T301-WTemperature/8.233.3251

13、201014020.8Prere /bar7.51019184.81.44.9Vapor Frac1110100Solid Frac0000000Mole Flow kmol/hr1007.72641.5262087.8665154.806673.2081033.276Mass Flow kg/hr42361.121723.61430103.29174423.41542.853.56Volume Flow cum/hr2721.60491.5652748.36966.942760.60668.313107.977Enlpy Gcal/hr3.967-0.479-26.28441.84-1.04

14、142.712-56.548Output51578.665Rel.diff0.000表 3-8羰基工段物算表Mass-flow kg/hrSummationInput248611.444Output248611.374Rel.diff2.81564E-07Mole Flow kmol/hrC3H814.6504922.19871002.9368740.00575348.28498C2H60.1270990.155481000.0916641.32E-050.190884H21.6756771.1708761091.80114.54832.24E-051.175397CH40000000C3H6

15、990.929116.65887002.2156470.0050630.14362C3H41.81E-094.80E-11009.36E-111.79E-121.76E-09C2H41.16E-067.07E-07001.05E-065.78E-118.11E-07C2H20.3440510.47289000.2434467.36E-050.573315H2O1.58E-261.06E-07000.0182040.3435811.44184CO00.863857995032.251139.06E-060.87315C4H8O-105.88E-15002.1672987.353795875.46

16、27C4H8O-209.12E-15000.23560.29762373.4308C18H15P0006651.43E-09664.85330.146656C5H10O200005.27E-060.3488171.547054C8H14O0000000C8H18O0000000C4H10O-10000000C4H10O-20000000O200.005205100.0980962.22E-070.0052963.4 异构物分离工段3.4.1 异构物分离工段流程图图 3-4异构物分离工段流程图3.4.2 异构物分离工段物算表 3-9异构物分离工段流股物料模拟结果ItemsInputOutputT

17、301-WRECYCLE4L4T402-DT403-WC4-1C4-2Temperature/20.833.3-3.583.355.731.931.9Prere bar4.91051.80.20.20.2Vapor Frac0101011Solid Frac0000000Mole Flow kmol/hr1033.27641.52633.904105.3632.557149.927699.999Mass Flow kg/hr72089.561723.6141466.4467355.247258.75410810.7750474.78Volume Flowcum/hr107.97791.5652

18、.9061654.4640.32818849.2688005.96Enlpy Gcal/hr-56.548-0.479-0.611-5.072-0.243-7.389-34.499Mole Flow kmol/hrC3H848.2849822.1987120.875355.2119975.21199700表 3-10异构物分离工段物算表Mass-flow kg/hrSummationInput72089.561Output72089.606Rel.diff-6.24224E-07C2H60.1908840.1554810.0354051.11E-091.11E-0900H21.1753971.

19、1708760.00452109.99E-3100CH40000000C3H630.1436216.6588712.879160.60552020.6055200C3H41.76E-094.80E-117.11E-111.64E-091.64E-0900C2H48.11E-077.07E-071.04E-0702.12E-1700C2H20.5733150.472890.1004491.48E-091.48E-0900H2O1.441841.06E-076.07E-071.4418391.44183900CO0.873150.8638570.00929701.61E-2600C4H8O-187

20、5.46275.88E-153.45E-1324.88496875.4627149.8895699.8244C4H8O-273.43089.12E-154.12E-1373.2188173.43080.0373950.174597C18H15P0.146656001.74E-1460.1466562.69E-651.26E-64C5H10O21.547054004.76E-721.5470542.11E-159.86E-15C8H14O0000000C8H18O0000000C4H10O-10000000C4H10O-20000000O20.0052960.0052059.08E-0502.8

21、8E-25003.5 醇醛缩合工段3.5.1 醇醛缩合工段流程图图 3-5醇醛缩合工段流程图3.5.2 醇醛缩合工段物算表 3-11醇醛缩合工段流股物料模拟结果ItemsInputOutputC4-2C-INH-OUTWATERE502-OUTTemperature/31.925112.725150Prere bar0.2550.56Vapor Frac10000Solid Frac00000Mole Flow kmol/hr699.999500500335.466364.533Mass Flow kg/hr50474.789007.649007.646043.51444431.26Volum

22、e Flow cum/hr88005.9611.91912.8427.99777.196EnlpyGcal/hr-34.499-34.495-33.583-23.145-18.203Mole Flow kmol/hrC3H800000表 3-12醇醛缩合工段物算表3.6 加氢精馏工段3.6.1加氢精馏工段1加氢精馏工段流程图Mass-flow kg/hrSummationInput59482.415Output59482.413Rel.diff3.36234E-08C2H600000H200000CH400000C3H600000C3H400000C2H400000C2H200000H2O05

23、00500335.4669.197541CO00000C4H8O-1699.8244001.58E-0610.49736C4H8O-20.174597001.73E-080.174597C18H15P1.26E-640000C5H10O29.86E-150000C8H14O0001.65E-13344.6635C8H18O00000C4H10O-100000C4H10O-200000O200000图 3-6加氢精馏工段流程图2加氢精馏工段物算表 3-13加氢精馏工段流股物料模拟结果ItemsInputOutputH2-1T402-DC4-1T601-DT602-DS102C4H10O-1Tem

24、perature/15083.331.9123.47682.485.1Prere/bar51.80.250.30.30.3Vapor Frac1111110Solid Frac0000000Mole Flow kmol/hr235105.363149.92726.26557.514.5158.478Mass Flow kg/hr473.7327355.24710810.771559.4194258.7911074.67411746.866Volume Flow cum/hr1657.5921654.46418849.26160.5185502.8951413.38117.684Enlpy Gc

25、al/hr0.204-5.072-7.389-1.131-3.773-0.938-11.826Mole Flow kmol/hrC3H805.21199705.211997000C2H60.00E+001.11E-0901.11E-09000H2235001.453211000CH40000000C3H600.6055200.6055202000C3H40.00E+001.64E-0901.64E-09000表 3-14加氢精馏工段物算表3.6.2 辛烯醛加氢精馏工段1辛烯醛加氢精馏工段流程图Mass-flow kg/hrSummationInput18639.749Output18639.7

26、50Rel.diff-5.36488E-08C2H40000000C2H20.00E+001.48E-0901.48E-09000H2O01.44183901.4418391.13E-073.23E-098.90E-36CO0000000C4H8O-1024.88496149.88951.8647451.5789960.0517473.81E-18C4H8O-2073.218810.03739510.943940.0431850.0013065.79E-25C18H15P0.00E+001.74E-1462.69E-650000C5H10O20.00E+004.76E-722.11E-1500

27、00C8H14O0000000C8H18O0000000C4H10O-10000.31556493.3861969.783443157.7938C4H10O-20004.42802152.491624.6635040.6845962O20000000图 3-7辛烯醛加氢精馏工段流程图2辛烯醛加氢精馏工段物算表 3-15辛烯醛加氢精馏工段流股物料模拟结果ItemsInputOutputE502-OUTH2-2V6T603-DT604-WC8H18OTemperature/.8123.4123.3Prere bar66610.10.1Vapor Frac011101Solid Frac000000

28、Mole Flow kmol/hr364.53372035.32821.1810.069343.942Mass Flow kg/hr44431.2591451.43478.3881014.3588.9644780.99Volume Flow cum/hr77.1964234.211153.847650.1020.014112631.3Enlpy Gcal/hr-18.2030.626-0.01-1.071-0.006-27.422Mole Flow kmol/hrC3H8000000C2H6000000H2072035.093950.892832800CH4000000表 3-16辛烯醛加氢精

29、馏工段物算表4 主要设备物算4.1 反应器4.1.1 丙烷反应器（R-104）表 4-1R-104 流股物料模拟结果ItemsInputOutputR103-OUTR104-OUTTemperature/630630Mass-flow kg/hrSummationInput45882.693Output45882.693Rel.diff0.000C3H6000000C3H4000000C2H4000000C2H2000000H2O9.19754100.1779429.0195991.24E-767.28E-09CO000000C4H8O-110.4973600.04814510.386267.

30、65E-582.82E-05C4H8O-20.174596500.0011470.17344911.29E-652.80E-08C18H15P000000C5H10O2000000C8H14O344.663500.0002120.04120087.73E-152.646962C8H18O000.0065470.60493650.068802341.2949C4H10O-1003.92E-050.0628481.79E-434.45E-05C4H10O-2000000O2000000表 4-2R-104 流股物算表4.1.2 选择性加氢反应器（R-201）表 4-3R-201 流股物料模拟结果I

31、temsputOutputR201-INH2T202-INTemperature/26.72550Prere bar251228Mass-flow kg/hrSummationInput50845.2253Output50845.2253Rel.diff0.000Prere bar1.51.5Vapor Frac11Solid Frac00Mole Flow kmol/hr2209.0982305.25Mass Flow kg/hr50845.2350845.23Volume Flow cum/hr110653115468.5Enlpy Gcal/hr25.16528.215Mole Flow

32、 kmol/hrC3H8196.107108.839C2H65.8225.764H21009.6341101.863CH442.74346.665C3H6854.977933.419C3H453.54558.448C2H40.1770.235C2H242.74446.667H2O3.353.35表 4-4R-201 流股物算表4.1.3 羰基反应器（R-302）表 4-5R-302 流股物料模拟结果ItemsputOutputE302-OUTR302-OUTTemperature/200100Prere bar17.217.2Mass-flow kghrSummationInput46582.

33、215Output46582.215Rel.diff0.000Vapor Frac010Solid Frac000Mole Flow kmol/hr1103.772601105.448Mass Flow kg/hr46461.26120.95346582.22Volume Flow cum/hr98.605124.873113.067Enlpy Gcal/hr0.0370.001-1.413Mole Flow kmol/hrC3H8108.78390108.7839C2H60.12709900.127099H21.67E-30601.675677CH43.50E-1500C3H6932.726

34、0991.0503C3H458.4412100.116882C2H41.16E-0601.16E-06C2H20.34405100.344051H2O3.35007303.350073表 4-6R-302 流股物算表Mass-flow kghrSummationVapor Frac0.6760.122Solid Frac00Mole Flow kmol/hr2140.8421861.29Mass Flow kg/hr248611.4248611.4Volume Flow cum/hr3120.067570.225Enlpy Gcal/hr6.661-12.976Mole Flow kmol/h

35、rC3H849.506151.2276C2H60.2825620.282562H2256.6361115.7237CH400C3H6172.150732.36433C3H41.86E-091.86E-09C2H41.86E-061.86E-06C2H20.8168350.816835H2O1.4360071.803625CO171.947533.12429C4H8O-1758.3506884.9838C4H8O-263.2906873.96402C18H15P665665C5H10O21.1375261.895876C8H14O00C8H18O00C4H10O-100C4H10O-200O20

36、.2872020.1033934.1.4 醇醛缩合反应器（R-501）表 4-7R-501 流股物料模拟结果ItemsputOutputC4-2R501-OUTTemperature/31.9120Prere bar0.25Vapor Frac10Solid Frac00Mole Flow kmol/hr699.999699.999Mass Flow kg/hr50474.7850474.78Volume Flow cum/hr88005.9688.272Enlpy Gcal/hr-34.499-40.072Mole Flow kmol/hrC3H800C2H600H200CH400C3H60

37、0C3H400C2H400C2H200H2O0344.6635CO00C4H8O-1699.824410.49737C4H8O-20.1745970.174597Input248611.374Output248611.374Rel.diff0.000表 4-8R-501 流股物算表4.2 两相分离器本项目中的两相分离器主要为气液分离器（F-601）。该气液分离器的流股物流模拟结果见下表：表 4-9F-601 流股物料模拟结果ItemsputOutputE604-OUTV6T603-INTemperature/404040Prere bar666Vapor Frac0.08810Solid Fr

38、ac000Mole Flow kmol/hr400.5235.328365.192Mass Flow kg/hr45882.6978.38845804.3Volume Flow cum/hr220.31153.84766.464Enlpy Gcal/hr-35.042-0.01-35.033Mole Flow kmol/hrC3H8000Mass-flow kghrSummationInput50474.775Output50474.775Rel.diff0.000C18H15P1.26E-640C5H10O29.86E-150C8H14O0344.6635C8H18O00C4H10O-100

39、C4H10O-200O200表 4-10F-601 流股物算表4.3 塔设备4.3.1 丙烯精馏塔（T-202）表 4-11T-202 流股物料模拟结果ItemsInputOutputMass-flow kg/hrSummationInput45882.6921Output45882.6921Rel.diff0.000C2H6000H235.9867835.093950.892833CH4000C3H6000C3H4000C2H4000C2H2000H2O9.1975410.1779429.019599CO000C4H8O-110.434430.04814510.38629C4H8O-20.1

40、745970.0011470.173449C18H15P000C5H10O2000C8H14O2.6883750.0002122.688163C8H18O341.97510.006547341.9686C4H10O-10.0629323.92E-050.062893C4H10O-2000O2000表 4-12T-202 流股物算表4.3.2 异构物分离塔（T-402）表 4-13T-402 流股物料模拟结果ItemsputOutputMass-flow kghrSummationInput46582.2158Output46582.2154Rel.diff8.94279711e-09T202-

41、INC3H6RECYCLE1Temperature/508.221.5Prere bar287.58.5Vapor Frac010Solid Frac000Mole Flow kmol/hr1105.4481007.72697.722Mass Flow kg/hr46582.2242361.124221.092Volume Flow cum/hr113.0672721.6049.063Enlpy Gcal/hr-1.4133.967-2.941Mole Flow kmol/hrC3H8108.783914.6504994.1334C2H60.1270990.1270991.75E-27H21.6756771.6756774.52E-97CH4000C3H6991.0503990.92910.121237C3H40.1168821.81E-090.116882C2H41.16E-061.16E-062.93E-40C2H20.3440510.3440515.63E-29H2O3.3500731.58E-263.350074T403-INT402-402-DTem