51附录一物料平衡计算书

1、青岛年产 40 万吨丙烯VPRO 团队青岛年产 40 万吨丙烯项目物料衡算计算书设计团队：V-Pro指导：，团队：利，波，杰，贾1VPRO 团队青岛年产 40 万吨丙烯目录物料平衡计算11.1 总论11.2 物料衡算的意义11.3 物料衡算遵循的原则11.4 物料衡算21.4.1物料衡算任务21.4.2丙烷脱氢反应工段物料衡算31.4.3深冷和膜分离氢烃分离工段物料衡算71.4.4脱乙烷和丙炔加氢反应工段物料衡算131.4.5丙烷-丙烯分离工段物料衡算181.4.6 总流程物料衡算212物料平衡计算1.1 总论本项目使用总厂的丙烷为主要原料，通过丙烷脱氢最终制得纯度为99.6%的丙烯，年产量为

2、40万吨。在已确定化学生产工艺和流程后，由定性阶段转向定量阶段，通过对整个生产系统、生产车间，以及部分重要的生产单元进行物料衡算计算出主、副的产量，原材料的消耗定额、“三废”排放量及组成，以及收率等各项技术指标，从而定 量地评述初步设计所选择的工艺路线、生产及工艺流程在上是否合理。1.2 物料衡算的意义在化学工程中，设计或改造工艺流程和，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

3、表现形式。凡引入某一的物料成分、质量或体积比等于操作后所得产物的成分、质量或体积加上物料损失。1.3 物料衡算遵循的原则（1）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)（2）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)1物料平衡计算书（3）在状态下有：(物料进入率)=(物料流出率)（4）物料衡算总质量衡算、组分衡算和元素衡算。各种衡算的适用情1-1 所示：1.4 物料衡算1.4.1 物料衡算任务从原料入厂到输出，其工艺路线可分为如下3 个步骤：丙烷脱氢反应工段、深冷分离和膜分离氢烃分离工

4、段、丙烷-丙烯分离分离工段。对于本厂，工艺采取年开工333天（8000小时）的连续操作，其中一年内的四五周（约30天）用于固定的停车检修及紧急情况处理。物料衡算的主要任务在于：（1）确定丙烯的实际产量以及质量指标；（2）确定氢气、丙烷、丙烯的循环量以及损失率等指标；（3）确定工艺中的“三废”排放量等公共指标；（4）各主要单元过程的物料衡算，并指导工艺的确定；2物料平衡计算书（5）汇总全流程物料衡算，数据用于完成物料流程图等后续设计任务1.4.2 丙烷脱氢反应工段物料衡算下图是由 Aspen Plus模拟得出丙烷脱氢反应单元物料流股衡算图。图 1-1丙烷脱氢反应单元物料流股衡算图3物料平衡计算书

5、表 1-2丙烷脱氢反应单元物料衡算表4物料平衡计算书进料0101010201030104010501060107010801090110出料0111进料0112进料0113进料01140115进料0316Temperat ure C2532.4600527.6600550.7600564.5600573.8567.22525252557.8Pressure bar9.8422222222222229.712VaporFrc0111111111111111Mole Flow kmol/hr1236.911771.9411771.9412280.5412280.5412629.4812629.48

6、12881.9912881.9913068.5610907.331283.3041893.36412001236.96158.374Mass Flow kg/hr54330.3209025.5209025.5209026.3209026.3209026.3209026.3209026.3209026.3209026.3209026.356395.9683463.112419.05654330.312417.03Volume Flow cum/hr113.78149099.5427597.7409079.3446067.5432830.3458739.2448869.8467908.746045

7、5.6381307.715411.6122731.614889.012618.39384819.53Enthalpy MMBtu/hr-133.911-413.667-4.174-4.17458.66458.664101.778101.778132.975132.97590.063-116.238-186.6270.002-116.3465.542MassFlow kg/hrC3H852915.82188174.4188174.4165749.2165749.2150362.1150362.1139227.5139227.5131000.3136285.152366.5382890.22052

8、915.821.794H2014833.4714833.4715858.6215858.6216561.9516561.9517070.8517070.8517446.8312750.6002419.056012414.415物料平衡计算书CH400.1030.1030.7190.7191.5381.5382.4792.4793.4981254.15800000.103C3H6210.4034804.0144804.01426203.1526203.1540884.6840884.6851507.8551507.8559356.2853928.794024.242568.6680210.403

9、0.7C2H456.10856.10956.10957.18557.18558.61858.61860.26260.26262.043627.07900056.1080.001C2H6150.348150.37150.37150.37150.37150.37150.37150.371150.371150.372627.079000150.3480.022C3H4997.6131007.021007.021007.0221007.0221007.0221007.0221007.0221007.0221007.0223553.4475.1824.2250997.6130H2O00000000000

10、00000Mass FracC3H80.9740.90.90.7930.7930.7190.7190.6660.6660.6270.6520.9290.99300.9740H200.0710.0710.0760.0760.0790.0790.0820.0820.0830.06100101CH400000000000.00600000C3H60.0040.0230.0230.1250.1250.1960.1960.2460.2460.2840.2580.0710.00700.0040C2H40.0010000000000.0030000.0010C2H60.0030.0010.0010.0010

11、.0010.0010.0010.0010.0010.0010.0030000.0030C3H40.0180.0050.0050.0050.0050.0050.0050.0050.0050.0050.0170000.0180H2O0000000000000000MoleFlow kmol/hrC3H812004267.3294267.3293758.7833758.7833409.8413409.8413157.3353157.3352970.7623090.611187.5431879.745012000.0416物料平衡计算书H207358.317358.317866.8497866.849

12、8215.748215.748468.1888468.1888654.6976325.08100120006158.31CH400.0060.0060.0450.0450.0960.0960.1550.1550.21878.17600000.006C3H65114.162114.162622.689622.689971.579971.5791224.0271224.0271410.5371281.55895.63213.514050.017C2H42222.0382.0382.0892.0892.1482.1482.21222.35300020C2H655.0015.0015.0015.001

13、5.0015.0015.0015.0015.00120.85400050.001C3H424.925.13525.13525.13525.13525.13525.13525.13525.13525.13588.6930.1290.105024.90H2O0000000000000000Mole FracC3H80.970.3620.3620.3060.3060.270.270.2450.2450.2270.2830.9250.99300.970H200.6250.6250.6410.6410.6510.6510.6570.6570.6620.5800101CH400000000000.0070

14、0000C3H60.0040.010.010.0510.0510.0770.0770.0950.0950.1080.1170.0750.00700.0040C2H40.0020000000000.0020000.0020C2H60.0040000000000.0020000.0040C3H40.020.0020.0020.0020.0020.0020.0020.0020.0020.0020.0080000.020H2O0000000000000000由上表可以看出，单元进、出物料的总体质量保持平衡。1.4.3 深冷和膜分离氢烃分离工段物料衡算1.4.3.1废热锅炉单元物料衡算图 1-2 废热锅

15、炉单元物料流股衡算图表 1-3废热锅炉单元物料衡算表7物料平衡计算书8物料平衡计算书物料说明进料 0111进料 0201出料 0202出料 0203Temperature C567.220350.7300Pressurebar21651652Vapor Frac1011Mole Flowkmol/hr10907.334229.7434229.74310907.33Mass Flowkg/hr209026.37620076200209026.3Volume Flow cum/hr381307.778.707771.802259991.1EnthalpyMMBtu/hr90.063-1158.54

16、-956.356-112.123Mass Flowkg/hr质量流率C3H8136285.100136285.1H212750.60012750.6CH41254.158001254.158C3H653928.790053928.79C2H4627.07900627.079C2H6627.07900627.079C3H43553.447003553.447H2O076200762000Mass Frac质量分数C3H80.652000.652H20.061000.061CH40.006000.006C3H60.258000.258C2H40.003000.003C2H60.003000.003

17、1.4.3.2 深冷分离单元物料衡算9物料平衡计算书C3H40.017000.017H2O0110Mole Flowkmol/hr流率C3H83090.61003090.61H26325.081006325.081CH478.1760078.176C3H61281.558001281.558C2H422.3530022.353C2H620.8540020.854C3H488.6930088.693H2O04229.7434229.7430Mole Frac分数C3H80.283000.283H20.58000.58CH40.007000.007C3H60.117000.117C2H40.002

18、000.002C2H60.002000.002C3H40.008000.008H2O0110图 1-3深冷分离单元物料流股衡算图10物料平衡计算书表 1-4深冷分离单元物料衡算表11物料平衡计算书物料说明进料 0205出料 0206出料 0207Temperature C40-95-95Pressurebar111111Vapor Frac101Mole Flowkmol/hr10907.334497.6986409.627Mass Flowkg/hr209026.3193771.515254.84Volume Flow cum/hr25349.01294.9048683.533Enthalp

19、yMMBtu/hr-267.38-386.456-26.988Mass Flowkg/hr质量流率C3H8136285.1135457.7827.441H212750.634.75412715.85CH41254.158205.3531048.805C3H653928.7953455.05473.734C2H4627.079514.685112.394C2H6627.079570.46456.615C3H43553.4473533.45119.996H2O000Mass Frac质量分数C3H80.6520.6990.054H20.06100.834CH40.0060.0010.069C3H6

20、0.2580.2760.031C2H40.0030.0030.007C2H60.0030.0030.004C3H40.0170.0180.001H2O000Mole Flowkmol/hr流率C3H83090.613071.84618.764H26325.08117.246307.841CH478.17612.865.376C3H61281.5581270.311.258C2H422.35318.3464.006C2H620.85418.9711.883C3H488.69388.1930.499H2O000Mole Frac分数C3H80.2830.6830.003H20.580.0040.9

21、84由上表可以看出，单元进、出物料的总体质量保持平衡。1.4.3.3 氢气膜分离单元物料衡算图 1-4 氢气膜分离单元物料流股衡算图表 1-5氢气膜分离单元物料衡算表12物料平衡计算书物料说明进料 0207出料 0208出料 0209Temperature C404040Pressurebar303030Vapor Frac111Mole Flowkmol/hr6409.6276249.874159.753Mass Flowkg/hr15254.83412601.5232653.311Volume Flow cum/hr5647.4135506.408133.816EnthalpyMMBtu/

22、hr-3.3162.725-6.095Mass Flowkg/hrC3H8827.4411.82825.621H212715.8512598.864116.986CH41048.8050.1051048.7C3H6473.7340.711473.023C2H4112.3940.001112.393CH40.0070.0030.01C3H60.1170.2820.002C2H40.0020.0040.001C2H60.0020.0040C3H40.0080.020H2O000由上表可以看出，单元进、出物料的总体质量保持平衡。1.4.4 脱乙烷和丙炔加氢反应工段物料衡算1.4.4.1 脱乙烷塔单元

23、物料衡算13物料平衡计算书C2H656.6150.02256.593C3H419.996019.996H2O000Mass FracC3H80.05400.311H20.83410.044CH40.06900.395C3H60.03100.178C2H40.00700.042C2H60.00400.021C3H40.00100.008H2O000Mole Flowkmol/hrC3H818.7640.04118.723H26307.8416249.80958.032CH465.3760.00765.369C3H611.2580.01711.241C2H44.00604.006C2H61.883

24、0.0011.882C3H40.49900.499H2O000Mole FracC3H80.00300.117H20.98410.363CH40.0100.409C3H60.00200.07C2H40.00100.025C2H6000.012C3H4000.003H2O000404040图 1-5脱乙烷塔单元物料流股衡算图表 1-6脱乙烷塔单元物料衡算表14物料平衡计算书物料说明进料 0206出料 0301出料 0302Temperature C-9536.5-32.8Pressurebar1113.619.5Vapor Frac001Mole Flowkmol/hr4497.6984419.

25、55378.145Mass Flowkg/hr193771.5191985.11786.417Volume Flow cum/hr294.904421.826152.664EnthalpyMMBtu/hr-386.456-325.81-1.927Mass Flowkg/hr质量流率C3H8135457.7135294.4163.291H234.754034.754CH4205.3530205.353C3H653455.0553161.2293.852C2H4514.6850514.685C2H6570.4640.001570.463C3H43533.4513529.4334.018H2O000

26、Mass Frac质量分数由上表可以看出，单元进、出物料的总体质量保持平衡。1.4.4.2 丙炔加氢反应精馏塔单元物料衡算15物料平衡计算书C3H80.6990.7050.091H2000.019CH40.00100.115C3H60.2760.2770.164C2H40.00300.288C2H60.00300.319C3H40.0180.0180.002H2O000Mole Flowkmol/hr流率C3H83071.8463068.1433.703H217.24017.24CH412.8012.8C3H61270.31263.3176.983C2H418.346018.346C2H618

27、.971018.971C3H488.19388.0930.1H2O000Mole Frac分数C3H80.6830.6940.047H20.00400.221CH40.00300.164C3H60.2820.2860.089C2H40.00400.235C2H60.00400.243C3H40.020.020.001H2O000图 1-6丙炔加氢反应精馏塔单元物料流股衡算图16物料平衡计算书表 1-7丙炔-丙二烯加氢反应精馏塔单元物料衡算表17物料平衡计算书物料说明进料 0304进料0305进料0311进料0312出料0306出料0307出料0313出料0314Temperature C383

28、8404051.764.351.764.3Pressure bar252528.8928.892023.452023.45Vapor Frac00110000Mole Flow kmol/hr2209.7772209.77745.7545.751263.095946.6821263.095946.682Mass Flow kg/hr95992.5395992.5392.24592.24554353.2141731.5654353.2141731.56Volume Flow cum/hr208.807208.80741.83341.833130.653110.49130.653110.49Ent

29、halpy MMBtu/hr-162.624-162.6240.020.02-61.084-102.657-61.084-102.657Mass Flow kg/hr质量流率C3H867647.2167647.210.0130.01326282.3241445.1726282.3241445.17H20092.22692.2260000CH4000.0010.0010.00100.0010C3H626580.626580.60.0050.00528068.3284.2828068.3284.28C2H400000000C2H600000.00100.0010C3H41764.7171764.7

30、17002.592.1122.592.112H2O00000000Mass Frac质量分数C3H80.7050.705000.4840.9930.4840.993H200110000CH400000000C3H60.2770.277000.5160.0070.5160.007C2H400000000C2H600000000C3H40.0180.018000000H2O00000000Mole Flow由上表可以看出，单元进、出物料的总体质量保持平衡。1.4.5 丙烷-丙烯分离工段物料衡算1.4.5.1丙烷-丙烯精馏塔单元物料衡算图 1-7丙炔-丙烯精馏塔单元物料流股衡算图18物料平衡计算书k

31、mol/hr流率C3H81534.0711534.07100596.018939.874596.018939.874H20045.7545.750000CH400000000C3H6631.659631.65900667.0126.756667.0126.756C2H400000000C2H600000000C3H444.04744.047000.0650.0530.0650.053H2O00000000Mole Frac分数C3H80.6940.694000.4720.9930.4720.993H200110000CH400000000C3H60.2860.286000.5280.0070.

32、5280.007C2H400000000C2H600000000C3H40.020.02000000H2O00000000表 1-8丙炔-丙烯精馏塔单元物料衡算表19物料平衡计算书物料说明进料 0319出料 0401出料 0402Temperature C51.756.546.9Pressurebar2020.2719.5Vapor Frac000Mole Flowkmol/hr2526.191283.3041242.885Mass Flowkg/hr108706.456395.9552310.47Volume Flow cum/hr261.307140.604120.679EnthalpyM

33、MBtu/hr-122.167-130.3688.206Mass Flowkg/hr质量流率C3H852564.6452366.42198.226H2000CH40.00200.002C3H656136.64024.35352112.24C2H4000C2H60.00100.001C3H45.185.180H2O000Mass Frac质量分数C3H80.4840.9290.004H2000CH4000C3H60.5160.0710.996C2H4000C2H6000C3H4000H2O000Mole Flowkmol/hr流率C3H81192.0361187.5414.495H2000CH4000C3H61334.02495.6341238.39C2H4000C2H6000C3H40.1290.1290H2O000Mole Frac分数C3H80.4720.9250.004H2000CH4000由上表可以看出，单元进、出物料的总体质量保持平衡。20物料平衡计算书C3H60.5280.0750.996C2H4000C2H600