附录一 物料衡算一览表

中北大学 天津石化1.0104Nm3/h废气脱硫装置项目物料平衡计算书2017“东华科技陕鼓杯”第十一届全国大学生化工设计竞赛知行NUC队 中北大学物料平衡计算书团队成员：亓 天 夏智文 刘 东 李林洪 张娇娇指导老师：李同川 程 原 王艳红 马忠平 杨朝明废气脱硫装置项目天津石化1.0104Nm3/h 知行NUC队 41目录1. 概述32. 物料衡算原理33. 物料衡算44. 系统物料衡算44.1酸性气燃烧工段物料衡算44.2 克劳斯反应工段164.3 尾气处理工段物料衡算254.4液流脱气工段物料衡算351. 概述本项目旨为中国石油化工股份有限公司天津石化设计一座年处理废气分厂，该项目以总厂产生的含硫废气为原料，通过酸性气燃烧、克劳斯反应、尾气处理和液流脱气四个工段，硫资源利用程度大大增加，最终得到质量分数为 99.3%的优质硫，以及副产中压蒸汽。设计过程中利用Aspen Plus对全流程进行模拟，并在此基础上完成物料衡算、能量衡算，Aspen Plus模拟流程如图1-1所示。图1-1 全流程模拟图2. 物料衡算原理系统的物料衡算以质量守恒为理论基础，研究某一系统内进出物料量及组成的变化，即：系统累计的质量输入系统的质量输出系统的质量反应生成的质量反应消耗的质量假设系统无泄漏，有： 当系统无化学反应时，有： 在稳定状态下，有： ， 其中，-进入系统的物料流率； -流出系统的物料流率； -反应产生物料流率； -反应消耗物料流率。3. 物料衡算通过对系统整体以及部分主要单元的详细物料衡算，得到主、副产品的产量，原料的消耗量， “三废”的排放量以及最后产品的质量指标等关键经济技术指标，对所选工艺路线、设计流程进行定量评述，为后阶段的设计提供依据。4. 系统物料衡算4.1酸性气燃烧工段物料衡算酸性气燃烧工段流程模拟图如下图所示：图4-1酸性气燃烧工段模拟图表4-1 酸性气燃烧工段物料衡算表inoutStream No.PG0101PG0102PG0310PG0109BW0101BW0102W0103MS0101MS0102PL0101PL0102PG0122Stream Name酸性水提气溶剂再生酸气再生酸气富氧空气锅炉给水一锅炉给水二酸性废水中压蒸汽一中压蒸汽二液硫一液硫二燃烧后酸性气Temperature C3030117.08342820020029.99999286257.5922405257.9357679170170170Pressure bar112.01325145.0132545.01325145.0132545.013251.313251.313251.31325Molar Vapor Fraction0.9039446440.8014247220.646887179100011001Mole Flows kmol/hr190.515886255.634699.999961198218.6136773508.2352314544.815290169.06280101508.2352314544.815290117.7758575324.02267582448.6340571Mass Flows kg/hr6030.7661697853.901975201126245915698151244.939771915698154209.0665915387.3802610067.25765Volume Flow cum/hr4309.655665127.909693102.94949775471.46529110.5610230511.321149111.302534354430.3121561461.73498620.3648490210.49372830912523.13901Enthalpy Flow Gcal/hr-2.638626967-5.461553349-0.5954881990.004196578-33.08115419-35.46215907-4.756992856-28.6065775-30.66364210.058970034-0.020365932-21.1994155Mass Flows kg/hrH2004.85E-060000001.52E-083.08E-090.019529071O2000.0016236615596.3002700000000N2000.0503800031224.825975000001.56E-054.67E-051309.463879CO001.72E-070000005.82E-093.05E-080.847473689CO2108.2457264286.592287721.134342050000.005394216000.0005408260.000583382345.6671326H2S5389.3056716447.25349517.992002580001.602961273000.0688231260.0142666031189.054106COS061.4303103400000.000238269003.94E-050.000212214247.7212043SO2000.0002834460000003.21E-050.008689179799.1774813H2O430.33223341034.019385161.95185490915698151243.2458349156981518.6095788649.467212036169.864127NH3102.88253870.00E+000.00E+000.00E+000.00E+0000.08533826400000CH4024.606496700004.43E-06003.11E-0600S000000000000S200000000034.701819740.022015570.038967685S80000000004155.6857385297.8672345.158301406MDEA000000000000MDEA+000000000000H3O+7.37E-092.06E-080.0027292930002.80E-08002.80E-082.27E-080.089370699HS-1.24E-083.38E-080.003471950004.60E-08004.87E-083.92E-080.154571283HCO3-6.42E-103.88E-090.0023493120004.52E-09004.71E-113.82E-100.00150628S-1.85E-209.16E-201.14E-110001.25E-19004.99E-161.46E-155.76E-09CO3-5.61E-173.25E-165.36E-100003.91E-16001.19E-183.52E-171.39E-104.1.1 分液罐物料衡算表4-2 分液罐物料衡算表inoutStream No.PG0101PG0102W0103PG0103PG0104Stream Name酸性水提气溶剂再生酸气酸性废水干酸性水提气干溶剂再生酸气Temperature C303029.999992863030Pressure bar11111Molar Vapor Fraction0.9039446440.801424722011Mole Flows kmol/hr190.515886255.6346969.06280101172.2158147204.8719603Mass Flows kg/hr6030.7661697853.9019751244.9397715700.8899946938.83838Volume Flow cum/hr4309.655665127.9096931.3025343544309.3104935126.952326Enthalpy Flow Gcal/hr-2.638626967-5.461553349-4.756992856-1.378332063-1.964855405Mass Flows kg/hrH200000.00E+00O200000N200000.00E+00CO00000.00E+00CO2108.2457264286.59228770.005394216108.2449728286.5876471H2S5389.3056716447.2534951.6029612735388.8819316446.074274COS061.430310340.00023826906.14E+01SO200000.00E+00H2O430.33223341034.0193851243.245834100.9658898120.1398948NH3102.88253870.00E+000.085338264102.79720050CH4024.60649674.43E-0602.46E+01S00000S200000S800000MDEA00000MDEA+00000H3O+7.37E-092.06E-082.80E-0800.00E+00HS-1.24E-083.38E-084.60E-0800.00E+00HCO3-6.42E-103.88E-094.52E-0900.00E+00S-1.85E-209.16E-201.25E-1900.00E+00CO3-5.61E-173.25E-163.91E-1600.00E+004.1.2 一级燃烧炉物料衡算表4-3 一级燃烧炉物料衡算表inoutStream No.PG0113PG0114Stream Name一级燃烧炉入口一级燃烧炉出口Temperature C183.2742731250Pressure bar1.333251.32325Molar Vapor Fraction11Mole Flows kmol/hr474.5332456515.5673606Mass Flows kg/hr15569.3179115570.86957Volume Flow cum/hr13480.3061249347.32515Enthalpy Flow Gcal/hr-3.306595278-1.846153751Mass Flows kg/hrH24.85E-06162.9156242O22238.5217320N2489.9807702574.5683563CO1.72E-071.72E-07CO2415.9686564415.9686564H2S11852.951784762.909178COS61.4300720761.43007207SO20.000283446119.6245325H2O383.06091792838.04178NH3102.79720050.00E+00CH424.6064922624.60649226S00S206610.80488S800MDEA00MDEA+00H3O+0.00E+000.00E+00HS-0.00E+000.00E+00HCO3-0.00E+000.00E+00S-0.00E+000.00E+00CO3-0.00E+000.00E+004.1.3 一级余热锅炉物料衡算表4-4 一级余热锅炉物料衡算表inoutStream No.PG0114BW0101PLG0101MP0101Stream Name一级燃烧炉出口锅炉给水一一级余热锅炉出口中压蒸汽一Temperature C1250200350257.592Pressure bar1.3232545.01331.3232545.0133Molar Vapor Fraction1011Mole Flows kmol/hr515.567508.235515.567508.235Mass Flows kg/hr15570.9915615570.99156Volume Flow cum/hr49347.310.56120133430.312Enthalpy Flow Gcal/hr-1.84615-33.0812-6.32073-28.6066Mass Flows kg/hrH2162.91600.1234743560O20000N2574.5680574.56835630CO1.72E-0700.2121863110CO2415.9690415.96865640H2S4762.9107392.0038340COS61.4301060.974977550SO2119.62503.8485370170H2O2838.0491562903.1551339156NH30000CH424.6065024.606492260S0000S26610.8034.743394860S8004160.6645340MDEA0000MDEA+0000H3O+0000HS-0000HCO3-0000S-0000CO3-00004.1.4 一级物冷凝器料衡算表4-5 一级硫冷凝器物料衡算表inoutStream No.PLG0102PL0101PG0115Stream Name一级余热锅炉出口液硫一一级硫冷凝器出口Temperature C350170170Pressure bar1.323251.313251.31325Molar Vapor Fraction101Mole Flows kmol/hr427.4417.7759409.664Mass Flows kg/hr15570.94209.0711361.8Volume Flow cum/hr16710.90.36484911448.8Enthalpy Flow Gcal/hr-9.554260.05897-10.7662Mass Flows kg/hrH27.93E-063.60E-121.09E-05O2000N20.03690023.71E-090.0505702CO1.36E-051.38E-121.87E-05CO20.02671451.28E-070.0366111H2S0.4747331.64E-050.650571COS0.003915969.35E-090.00536666SO20.0002471637.63E-090.000338723H2O0.1864480.004421310.253868NH3000CH40.001580297.40E-100.00216572S000S20.002231310.008244543.66E-06S80.2672080.9873180.000438205MDEA000MDEA+000H3O+06.66E-121.34E-05HS-01.16E-112.32E-05HCO3-01.12E-142.24E-08S-01.19E-192.38E-13CO3-02.83E-225.68E-164.1.5 二级燃烧炉物料衡算表4-6 二级燃烧炉物料衡算表inoutStream No.PG0117PG0118Stream Name二级燃烧炉入口二级燃烧炉出口Temperature C165.5121250Pressure bar11.30325Molar Vapor Fraction11Mole Flows kmol/hr540.832542.336Mass Flows kg/hr15454.515454.6Volume Flow cum/hr19686.652707.4Enthalpy Flow Gcal/hr-10.6498-12.5421Mass Flows kg/hrH20.12347466.9207O23357.780N21309.461309.46CO0.212186116.278CO2415.968345.669H2S7391.941548.74COS60.97490.148106SO23.84852200.14H2O2884.555431.51NH301.12E-15CH424.60650S00S20.04157524430.79S84.97884.9788MDEA00MDEA+00H3O+00HS-00HCO3-00S-00CO3-004.1.6 二级余热锅炉物料衡算4-7 二级余热锅炉物料衡算表inoutStream No.BW0102PG0118MP0102PLG0105Stream Name锅炉给水二二级燃烧炉出口中压蒸汽二二级余热锅炉出口Temperature C2001250257.936350Pressure bar45.01331.3032545.01331.31325Molar Vapor Fraction0111Mole Flows kmol/hr544.815542.336544.815472.657Mass Flows kg/hr981515454.6981515454.6Volume Flow cum/hr11.321152707.4461.73518609.5Enthalpy Flow Gcal/hr-35.4622-12.5421-30.6636-19.8711Mass Flows kg/hrH2066.920700.0195291O20000N201309.4601309.46CO0116.27800.847474CO20345.6690345.669H2S01548.7401189.23COS00.1481060247.721SO202200.140799.186H2O98155431.5198156219.42NH301.12E-1500CH40000S0000S204430.79040.061S804.978805303.03MDEA0000MDEA+0000H3O+0000HS-0000HCO3-0000S-0000CO3-00004.2 克劳斯反应工段克劳斯反应工段模拟流程图如下图所示：图4-2 克劳斯反应工段模拟流程图表4-8 克劳斯反应工段物料衡算表inoutStream No.BW0102PG0118MP0102PLG0105Stream Name锅炉给水二二级燃烧炉出口中压蒸汽二二级余热锅炉出口Temperature C2001250257.936350Pressure bar45.01331.3032545.01331.31325Molar Vapor Fraction0111Mole Flows kmol/hr544.815542.336544.815472.657Mass Flows kg/hr981515454.6981515454.6Volume Flow cum/hr11.321152707.4461.73518609.5Enthalpy Flow Gcal/hr-35.4622-12.5421-30.6636-19.8711Mass Flows kg/hrH2066.920700.0195291O20000N201309.4601309.46CO0116.27800.847474CO20345.6690345.669H2S01548.7401189.23COS00.1481060247.721SO202200.140799.186H2O98155431.5198156219.42NH301.12E-1500CH40000S0000S204430.79040.061S804.978805303.03MDEA0000MDEA+0000H3O+0000HS-0000HCO3-0000S-0000CO3-00004.2.1 一级克劳斯反应器物料衡算表 4-9 一级克劳斯反应器物料衡算表inoutStream No.PG0201PG0203Stream Name一级克劳斯反应器入口一级克劳斯反应器出口Temperature C170330.804Pressure bar1.313251.25325Molar Vapor Fraction11Mole Flows kmol/hr448.633440.891Mass Flows kg/hr10067.210067.2Volume Flow cum/hr12523.117631.6Enthalpy Flow Gcal/hr-21.1997-20.9113Mass Flows kg/hrH20.01952910.0068853O200N21309.461309.46CO0.8474715.47E-05CO2345.668451.597H2S1189.21421.979COS247.721104.939SO2799.1760.777969H2O6169.946575.6NH300CH400S00S20.03896754.39149S85.158271198.49MDEA00MDEA+00H3O+00HS-00HCO3-00S-00CO3-004.2.2 二级克劳斯反应器物料衡算表 4-10 二级克劳斯反应器物料衡算表inoutStream No.PG0205PG0207Stream Name二级克劳斯反应器入口二级克劳斯反应器出口Temperature C160.032260Pressure bar1.233251.20325Molar Vapor Fraction11Mole Flows kmol/hr435.291435.309Mass Flows kg/hr8851.538851.53Volume Flow cum/hr12645.215993.9Enthalpy Flow Gcal/hr-21.6614-21.2987Mass Flows kg/hrH20.00688530.0089146O200N21309.461309.46CO5.47E-055.47E-05CO2451.597460.13H2S421.977430.491COS104.93993.291SO20.7779672.60081H2O6559.916555.39NH300CH400S00S20.01041050.0861082S82.841130.0605804MDEA00MDEA+00H3O+00HS-00HCO3-00S-00CO3-004.2.3选择性氧化反应器物料衡算表4-11 选择性氧化反应器物料衡算inoutStream No.PG0212PG0209PG0217PL0204PL0205Stream Name选择性氧化反应器进料预热空气进料选择性氧化反应器气体出料选择性氧化反应器液体出料一选择性氧化反应器液体出料二Temperature C200210210210210Pressure bar21.173251.163251.163251.17325Molar Vapor Fraction11100Mole Flows kmol/hr40435.309468.3530.1286071.44218Mass Flows kg/hr1155.618851.539620.7731.664354.701Volume Flow cum/hr787.4411485116122.10.002721070.0305146Enthalpy Flow Gcal/hr0.0492182-21.4815-22.23110.000821990.00912714Mass Flows kg/hrH200.00891460.00891461.01E-111.16E-10O2281.589037.5087.31E-088.67E-07N2874.0211309.462183.485.90E-076.36E-06CO05.47E-055.47E-051.48E-141.70E-13CO20460.13528.4714.05E-064.04E-05H2S0430.4915.74E-152.79E-223.11E-21COS093.2919.06E-204.21E-284.96E-06SO202.6008136.93061.48E-061.19E-06H2O06555.396781.710.09931491.13548NH300000CH400000S00000S200.08610820.006857280.004110650.0751403S800.060580452.648531.5606353.491MDEA00000MDEA+00000H3O+00000HS-00000HCO3-00000S-00000CO3-000004.2.4 三级硫冷凝器物料衡算表4-12 三级硫冷凝器物料衡算表inoutStream No.PG0203PG0204PL0201Stream Name一级克劳斯反应器出料气三级硫冷凝器出料气三级硫冷凝器出料液硫Temperature C330.804160160Pressure bar1.253251.253251.25325Molar Vapor Fraction110Mole Flows kmol/hr440.891435.2915.60017Mass Flows kg/hr10067.28851.531215.72Volume Flow cum/hr17631.612441.40.114341Enthalpy Flow Gcal/hr-20.9113-21.6614-0.0245637Mass Flows kg/hrH20.00688530.00688532.23E-10O2000N21309.461309.469.54E-06CO5.47E-055.47E-054.03E-13CO2451.597451.5920.000178989H2S421.979421.8690.00122236COS104.939104.9392.03E-05SO20.7779690.7779672.11E-06H2O6575.66559.8515.6902NH3000CH4000S000S24.391490.01041054.38108S81198.492.841131195.65MDEA000MDEA+000H3O+00.06237613.33E-09HS-00.1052665.62E-09HCO3-00.0058793.14E-10S-04.42E-092.36E-16CO3-01.12E-095.98E-174.2.5 四级硫冷凝器物料衡算表4-13 四级硫冷凝器物料衡算表inoutStream No.PG0207PG0208Stream Name二级克劳斯反应器出料气四级硫冷凝器出料气Temperature C260140Pressure bar1.203251.20325Molar Vapor Fraction11Mole Flows kmol/hr435.309435.309Mass Flows kg/hr8851.538851.53Volume Flow cum/hr15993.912353.6Enthalpy Flow Gcal/hr-21.2987-21.7338Mass Flows kg/hrH20.00891460.0089146O200N21309.461309.46CO5.47E-055.47E-05CO2460.13460.13H2S430.491430.491COS93.29193.291SO22.600812.60081H2O6555.396555.39NH300CH400S00S20.08610820.0861082S80.06058040.0605804MDEA00MDEA+00H3O+00HS-00HCO3-00S-00CO3-004.2.6 五级硫冷凝器物料衡算表4-14 五级硫冷凝器物料衡算表inoutStream No.PG0217PG0218PL0203Stream Name选择性氧化反应器出料气克劳斯尾气三级硫冷凝器出料液硫Temperature C210120120Pressure bar1.163251.143251.14325Molar Vapor Fraction110Mole Flows kmol/hr468.353467.9680.382553Mass Flows kg/hr9620.779565.0655.7048Volume Flow cum/hr16122.113301.50.00763645Enthalpy Flow Gcal/hr-22.2311-22.5706-0.0109458Mass Flows kg/hrH20.00891460.00891461.17E-11O237.50837.5081.32E-07N22183.482183.486.68E-07CO5.47E-055.47E-051.71E-14CO2528.471528.3811.61E-05H2S5.74E-1500COS9.06E-2000SO236.930636.93061.03E-05H2O6781.716778.433.2033NH3000CH4000S000S20.006857282.00E-050.00683723S852.64850.1538952.4946MDEA000MDEA+000H3O+00.03904721.17E-10HS-000HCO3-00.1252493.75E-10S-000CO3-01.26E-073.78E-164.3 尾气处理工段物料衡算尾气处理工段流程模拟图如下图所示：图4-3 尾气处理工段模拟流程图表4-15 尾气处理工段物料衡算表inoutStream No.PG0302PG0218BW0401PG0310PL0318LP0402PL0319PG0313PG0318PG0316Stream Name氢气进料克劳斯尾气蒸汽发生器给水焚烧炉空气进料MDEA溶液补充低压蒸汽急冷塔排水排放废气MDEA溶液排出再生酸气Temperature C301201002579.3267192.17378.881490079.3268117.083Pressure bar11.1432513.013312.1132513.01331.1432512.113252.01325Molar Vapor Fraction1101014.76E-0910.2497781Mole Flows kmol/hr1.8467.96960.11568.9230116.154760.1156372.473111.6990.10076110Mass Flows kg/hr3.6285895651083257.788296.27610836710.253203.577.72079201.139Volume Flow cum/hr45.392213301.51.12964221.0910.3045931