7.重庆v-star团队作品设计集附录

1、附录 1 物料一览表1.1 反应与预分离工段1.1.1 反应器(R0101)流入物料流出物料Temperature ()44.445Prere (bar)1010Vapor Frac00Mole Flow (kmol/hr)9421.1679394.532Mass Flow (kg/hr)287174.585287174.585Volume Flow(cum/hr)364.767359.452Enlpy (Gcal/hr)-511.231-542.819Mass Flow (kg/hr)O23.85560.048C3H631920.3248026.475C3H8109.724109.724C3

2、H6O1.27931330.839CH4O187796.263187250.447H2O37834.58947922.551H2O219911.246477.87C4H10O26140.6857675.856C3H8O23456.6214320.776Mass FracO200C3H60.1110.028C3H800C3H6O00.109CH4O0.6540.652H2O0.1320.167H2O20.0690.002C4H10O20.0210.027C3H8O20.0120.015Mole Flow (kmol/hr)O20.121.877C3H6758.551190.74C3H82.488

3、2.488C3H6O0.022539.442CH4O5860.9115843.8771.1.2 PO 分离塔(T0101)流入物料 1流入物料 2流出物料 1流出物料 2Temperature ()554579.258.5Prere (bar)1.121.41.1Vapor Frac0001Mole Flow (kmol/hr)875.7919394.5327768.0642502.259Mass Flow (kg/hr)30839.617287174.585219079.58698934.617Volume Flow(cum/hr)40.359359.452284.03762722.145E

4、nlpy (Gcal/hr)-46.204-542.819-470.865-92.182Mass Flow (kg/hr)O20.03760.048060.085C3H640.5548026.47508067.029C3H83.667109.7240113.391C3H6O6219.9231330.8391.59837549.16CH4O24547.526187250.447158694.32853103.645H2O27.91347922.55147909.15841.306H2O20477.87477.870C4H10O207675.8567675.8560C3H8O204320.7764

5、320.7760Mass FracO20000.001C3H60.0010.02800.082C3H80000.001C3H6O0.2020.10900.38CH4O0.7960.6520.7240.537H2O0.0010.1670.2190H2O200.0020.0020C4H10O200.0270.0350C3H8O200.0150.020Mole Flow (kmol/hr)O20.0011.87701.878C3H60.964190.740191.704C3H80.0832.48802.571C3H6O107.092539.4420.028646.507CH4O766.1015843

6、.8774952.6731657.305H2O2100.1392660.106H2O2585.37214.049C4H10O268.13785.172C3H8O245.42556.781丙烯提纯与吸收工段丙烯分离塔(T0201)流入物料流出物料 1流出物料 2流出物料 3Temperature ()25.994.8-9.3-9.3Prere (bar)554.84.8Vapor Frac0010Mole Flow (kmol/hr)1611.851431.1616.324174.364Mass Flow (kg/hr)67488.62859886.512261.3257340.79Volume

7、 Flow(cum/hr)87.35783.49128.90313.083Enlpy (Gcal/hr)-66.237-63.5420.023-0.01Mass Flow (kg/hr)O219.473015.6183.855C3H67478.3050242.9927235.313C3H8108.7814.4442.715101.622C3H6O31313.64631313.64600CH4O28555.02928555.02900H2O13.39313.39300H2O20000C4H10O20000C3H8O20000Mass FracO2000.060.001C3H60.11100.93

8、0.986C3H80.00200.010.014C3H6O0.4640.52300CH4O0.4230.47700H2O0000H2O20000C4H10O20000C3H8O20000Mole Flow(kmol/hr)O20.60900.4880.12C3H6177.71405.774171.939C3H82.4670.1010.0622.305C3H6O539.146539.14600H2O1.5492660.1062659.3622.293H2O2014.04914.0490C4H10O2085.17285.1720C3H8O2056.78156.78101.2.2 丙烯精制塔(T02

9、02)流入物料流出物料 1流出物料 2Temperature ()-8.916.926.7Prere (bar)10.21010.3Vapor Frac000Mole Flow (kmol/hr)174.364171.9232.441Mass Flow (kg/hr)7340.797233.902106.888Volume Flow(cum/hr)13.09713.8640.217Enlpy (Gcal/hr)-0.0080.19-0.058Mass Flow (kg/hr)O23.8553.8550C3H67235.3137219.52415.789C3H8101.62210.52491.0

10、98C3H6O000CH4O000H2O000H2O2000C4H10O2000C3H8O2000Mass FracO20.0010.0010C3H60.9860.9980.148C3H80.0140.0010.852C3H6O000CH4O000H2O000H2O2000C4H10O2000C3H8O2000Mole Flow (kmol/hr)O20.120.120C3H6171.939171.5640.375C3H82.3050.2392.066C3H6O000CH4O891.171891.17100H2O0.7430.74300H2O20000C4H10O20000C3H8O20000

11、1.2.3 丙烯吸收塔(T0203)流入物料 1流入物料 2流出物料 1流出物料 2Temperature ()10-11.41012.8Prere (bar)1.21.61.21.5Vapor Frac0110Mole Flow (kmol/hr)789.77420.9431.862808.854Mass Flow (kg/hr)25143867.69759.58725951.11Volume Flow(cum/hr)30.982284.88336.53432.45Enlpy (Gcal/hr)-45.4270.07-0.006-45.351Mass Flow (kg/hr)O2056.19

12、456.0090.185C3H60791.1620791.162C3H803.65703.657C3H6O0.22115.594015.815CH4O24933.241.093.5724930.759H2O209.5400.007209.532H2O20000C4H10O20000C3H8O20000Mass FracO200.0650.940C3H600.91200.03C3H800.00400C3H6O00.01800.001CH4O0.9920.0010.060.961H2O0.008000.008H2O20000C4H10O20000C3H8O20000Mole Flow (kmol/

13、hr)O201.7561.750.006C3H6018.801018.801C3H800.08300.083C3H6O0.0040.26800.272CH4O000H2O000H2O2000C4H10O2000C3H8O2000甲醇提纯与回流工段渗透汽化分离膜(X0301)流入物料流出物料 1流出物料 2Temperature ()606060Prere (bar)1.41.41.4Vapor Frac000Mole Flow (kmol/hr)9007.2945899.9973107.297Mass Flow (kg/hr)253895.934195048.44258847.492Volum

14、e Flow(cum/hr)320.304255.39463.333Enlpy (Gcal/hr)-548.274-339.583-207.951Mass Flow (kg/hr)O2000C3H6000C3H8000C3H6O1.5991.5990CH4O187228.654180675.6516553.003H2O54191.181896.69152294.489H2O2477.87477.870C4H10O27675.8567675.8560C3H8O24320.7764320.7760Mass FracO2000C3H6000C3H8000C3H6O000CH4O0.7370.9260

15、.111H2O0.2130.010.889H2O20.0020.0020C4H10O20.030.0390C3H8O20.0170.0220Mole Flow (kmol/hr )O2000C3H6000C3H8000CH4O778.1390.0340.111778.061H2O11.6310011.631H2O20000C4H10O20000C3H8O200001.3.2 甲醇提纯塔(T0301)流入物料流出物料 1流出物料 2Temperature ()6066.7105.9Prere (bar)1.41.11.25Vapor Frac000Mole Flow (kmol/hr)3107.

16、297202.9072904.391Mass Flow (kg/hr)58847.4926491.92952355.563Volume Flow(cum/hr)63.3338.75557.43Enlpy (Gcal/hr)-207.951-11.351-193.935Mass Flow (kg/hr)O2000C3H6000C3H8000C3H6O000CH4O6553.0036479.55673.447H2O52294.48912.37352282.116H2O2000C4H10O2000C3H8O2000Mass FracO2000C3H6000C3H8000C3H6O000CH4O0.1

17、110.9980.001H2O0.8890.0020.999H2O2000C4H10O2000C3H8O2000Mole Flow(kmol/hr)O2000C3H6000C3H8000C3H6O0.0280.0280CH4O5843.1975638.685204.512H2O3008.068105.2822902.785H2O214.04914.0490C4H10O285.17285.1720C3H8O256.78156.78101.3.3 甲醇分离塔(T0302)流入物料流出物料 1流出物料 2Temperature ()6066.9145.7Prere (bar)1.41.11.4Vap

18、or Frac000Mole Flow (kmol/hr)1179.9991144.59935.4Mass Flow (kg/hr)39009.68836439.132570.558Volume Flow(cum/hr)51.07949.0993.05Enlpy (Gcal/hr)-67.917-64.181-3.394Mass Flow (kg/hr)O2000C3H6000C3H8000C3H6O0.320.320CH4O36135.1336135.130H2O379.338303.6875.658H2O295.574095.574C4H10O21535.17101535.171C3H8O

19、2864.1550864.155Mass FracO2000C3H6000C3H8000C3H6O000CH4O0.9260.9920H2O0.010.0080.029H2O20.00200.037C4H10O20.03900.597C3H8O20.02200.336Mole Flow (kmol/hr)O2000C3H6000C3H8000C3H6O000CH4O204.512202.222.292H2O2902.7850.6872902.098H2O2000C4H10O2000C3H8O2000副产物提取工段副产物分离塔(T0401)流入物料 1流入物料 2流出物料 1流出物料 2Temp

20、erature ()145.7144.3126.5173.8Prere (bar)1.41.11.11.4Vapor Frac0000Mole Flow (kmol/hr)35.47.53124.04218.89Mass Flow (kg/hr)2570.558405.0941706.331269.323Volume Flow(cum/hr)3.050.4352.0291.459Enlpy (Gcal/hr)-3.394-0.477-2.151-1.716Mass Flow (kg/hr)O20000C3H60000C3H80000C3H6O0000CH4O0000H2O75.658075.6

21、580H2O295.574165.89695.497165.972C4H10O21535.171239.191535.171239.19C3H8O2864.1550.0090.003864.16Mass FracO20000C3H60000C3H80000C3H6O0000CH4O0000H2O0.02900.0440H2O20.0370.410.0560.131C4H10O20.5970.590.90.188C3H8O20.336000.681Mole Flow(kmol/hr)O20000C3H60000C3H6O0.0060.0060CH4O1127.7371127.7370H2O21.

22、05616.8574.2H2O22.8102.81C4H10O217.034017.034C3H8O211.356011.3561.4.2 丙二醇塔(T0402)流入物料流出物料 1流出物料 2Temperature ()173.8144.3195.7Prere (bar)1.41.11.3Vapor Frac000Mole Flow (kmol/hr)18.897.53111.358Mass Flow (kg/hr)1269.323405.094864.229Volume Flow(cum/hr)1.4590.4351.037Enlpy (Gcal/hr)-1.716-0.477-1.233

23、Mass Flow (kg/hr)O2000C3H6000C3H8000C3H6O000CH4O000H2O000H2O2165.972165.8960.077C4H10O2239.19239.190C3H8O2864.160.009864.152Mass FracO2000C3H6000C3H8000C3H6O000CH4O000H2O000H2O20.1310.410C4H10O20.1880.590C3H8O20.68101Mole Flow(kmol/hr)O2000C3H6000C3H80000C3H6O0000CH4O0000H2O4.204.20H2O22.814.8772.80

24、84.879C4H10O217.0342.65417.0342.654C3H8O211.3560011.3561.4.3 丙二醇甲醚分离塔(T0403)流入物料流出物料 1流出物料 2Temperature ()126.5123.2160.6Prere (bar)1.31.11.4Vapor Frac000Mole Flow (kmol/hr)24.04221.2322.809Mass Flow (kg/hr)1706.331610.66495.666Volume Flow(cum/hr)2.0291.9370.075Enlpy (Gcal/hr)-2.151-2.033-0.118Mass

25、Flow (kg/hr)O2000C3H6000C3H8000C3H6O000CH4O000H2O75.65875.6580H2O295.4970.00895.489C4H10O21535.1711534.9970.174C3H8O20.00300.003Mass FracO2000C3H6000C3H8000C3H6O000CH4O000H2O0.0440.0470H2O20.05600.998C4H10O20.90.9530.002C3H8O2000Mole Flow(kmol/hr)O2000C3H6000C3H8000C3H6O000CH4O000H2O000H2O24.8794.87

26、70.002C4H10O22.6542.6540C3H8O211.356011.3561.4.4 丙二醇甲醚精制塔(T0404)流入物料流出物料 1流出物料 2Temperature ()123.2137.6102.4Prere (bar)1.21.31.1Vapor Frac000Mole Flow (kmol/hr)21.23217.054.183Mass Flow (kg/hr)1610.6641534.54576.119Volume Flow(cum/hr)1.9371.9220.083Enlpy (Gcal/hr)-2.033-1.742-0.28Mass Flow (kg/hr)O

27、2000C3H6000C3H8000C3H6O000CH4O000H2O75.6580.49575.162H2O20.0080.0080C4H10O21534.9971534.0410.957C3H8O2000Mass FracO2000C3H6000C3H8000C3H6O000CH4O000H2O0.04700.987H2O2000C3H8000C3H6O000CH4O000H2O4.24.20H2O22.80802.807C4H10O217.03417.0320.002C3H8O2000环氧丙烷提纯工段萃取精馏塔(T0501)流入物料 1流入物料 2流入物料 3流出物料 1流出物料 2T

28、emperature ()44.54053.537.677.6Prere (bar)1.51.251.41.11.4Vapor Frac000.02800Mole Flow (kmol/hr)92.166348.5271431.161632.6241239.23Mass Flow (kg/hr)3954.4096282.66859886.51235307.22734816.362Volume Flow(cum/hr)4.7866.418854.76343.65746.111Enlpy (Gcal/hr)-3.982-23.691-65.138-19.533-73.089Mass Flow (k

29、g/hr)O200000C3H600000C3H8004.4444.4440C3H6O3317.348031313.64634630.9930CH4O12.8698.81428555.02942.37828534.333H2O624.1926273.85413.393629.4116282.029H2O200000C4H10O200000C3H8O200000Mass FracO200000C3H600000C3H800000C3H6O0.83900.5230.9810CH4O0.0030.0010.4770.0010.82H2O0.1580.99900.0180.18H2O200000C4H

30、10O200000C4H10O20.95310.013C3H8O2000Mole Flow(kmol/hr)O2000C3H6000C3H8000C3H6O000CH4O000H2O4.20.0274.172H2O2000C4H10O217.03217.0220.011C3H8O20001.5.2 PO 精制塔(T0502)流入物料流出物料 1流出物料 2Temperature ()37.636.744.5Prere (bar)1.51.11.3Vapor Frac000Mole Flow (kmol/hr)632.624540.45892.166Mass Flow (kg/hr)35307.

31、22731352.8183954.409Volume Flow(cum/hr)43.65938.8924.786Enlpy (Gcal/hr)-19.533-15.557-3.982Mass Flow (kg/hr)O2000C3H6000C3H84.4444.4440C3H6O34630.99331313.6453317.348CH4O42.37829.50912.869H2O629.4115.219624.192H2O2000C4H10O2000C3H8O2000Mass FracO2000C3H6000C3H8000C3H6O0.9810.9990.839CH4O0.0010.0010.

32、003H2O0.01800.158H2O2000C4H10O2000C3H8O200000Mole Flow(kmol/hr)O200000C3H600000C3H8000.1010.1010C3H6O57.1170539.146596.2630CH4O0.4020.275891.1711.323890.525H2O34.648348.2520.74334.938348.706H2O200000C4H10O200000C3H8O200000C3H8O2000Mole Flow(kmol/hr)O2000C3H6000C3H80.1010.1010C3H6O596.263539.14657.11

33、7CH4O1.3230.9210.402H2O34.9380.2934.648H2O2000C4H10O2000C3H8O2000附录 2能量一览表2.1 反应与预分离能量2.1.1反应器(R0101)表 2-1反应器焓变计算表表 2-2反应器负荷计算表表 2-3反应器能量平衡计算表2.1.2 PO 分离塔(T0101)Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)-31.5880030-511.231-542.8190.000003Heating dutyHeat duty(Gcal/hr)-31.588003Q= -31.58

34、8003 Gcal/hrW=0流入物料流出物料Temperature ()44.445Prere(bar)1010Vapor Frac00Mole Flow(kmol/hr)9421.1679394.532Mass Flow(kg/hr)287174.585287174.585Volume Flow(cum/hr)364.767359.452Enlpy(Gcal/hr)-511.231-542.819H(Gcal/hr)Hin =-511.231Hout =-542.819表 2-4PO 分离塔物流焓变计算表表 2-5PO 分离塔负荷计算表表 2-6PO 分离塔能量平衡计算表丙烯提纯与吸收工段

35、丙烯分离塔(T0201)表 2-7 丙烯分离塔物流焓变计算表流入物料流出物料 1流出物料 2流出物料 3Temperature ()25.994.8-9.3-9.3Prere(bar)554.84.8Vapor Frac0010Mole Flow(kmol/hr)1611.851431.1616.324174.364Mass Flow(kg/hr)67488.62859886.512261.3257340.79Volume Flow(cum/hr)87.35783.49128.90313.083Enlpy(Gcal/hr)-66.237-63.5420.023-0.01H(Gcal/hr)Hi

36、n =-66.237Hout =-63.529Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)25.97552420-589.023-563.0470CONDENSERREBOILERHeat duty(Gcal/hr)025.9755242Q= 25.9755242 Gcal/hrW=0流入物料 1流入物料 2流出物料 1流出物料 2Temperature ()554579.258.5Prere(bar)1.121.41.1Vapor Frac0001Mole Flow(kmol/hr)875.7919394.5327768.06

37、42502.259Mass Flow(kg/hr)30839.617287174.585219079.58698934.617Volume Flow(cum/hr)40.359359.452284.03762722.145Enlpy(Gcal/hr)-46.204-542.819-470.865-92.182H(Gcal/hr)Hin =-589.023Hout =-563.047表 2-8丙烯分离塔负荷计算表表 2-9丙烯分离塔能量平衡计算表2.2.2丙烯精制塔(T0202)表 2-10丙烯精制塔物流焓变计算表表 2-11丙烯精制塔负荷计算表表 2-12丙烯精制塔能量平衡计算表Q(Gcal/

38、hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)0.140-0.0080.1320CONDENSERREBOILERHeat duty(Gcal/hr)-4.31419614.45466795Q= 0.14Gcal/hrW=0流入物料流出物料 1流出物料 2Temperature ()-8.916.926.7Prere(bar)10.21010.3Vapor Frac000Mole Flow(kmol/hr)174.364171.9232.441Mass Flow(kg/hr)7340.797233.902106.888Volume Flow(c

39、um/hr)13.09713.8640.217Enlpy(Gcal/hr)-0.0080.19-0.058H(Gcal/hr)Hin =-0.008Hout =0.132Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)2.708563240-66.237-63.5290.00056324CONDENSERREBOILERHeat duty(Gcal/hr)-0.99187173.70044024Q= 2.70856324 Gcal/hrW=02.2.3丙烯吸收塔(T0203)表 2-13 丙烯吸收塔物流焓变计算表表 2-14丙烯吸收

40、塔负荷计算表表 2-15丙烯精制塔能量平衡计算表丙烯提纯与吸收工段甲醇水分离膜(M0301)表 2-16 甲醇水分离膜物流焓变计算表流入物料流出物料 1流出物料 2Temperature ()606060Prere(bar)1.41.41.4Vapor Frac000Mole Flow(kmol/hr)9007.2945899.9973107.297Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)00-45.357-45.3570CONDENSERREBOILERHeat duty(Gcal/hr)00Q= 0Gcal/hrW=0流

41、入物料 1流入物料 2流出物料 1流出物料 2Temperature ()10-11.41012.8Prere(bar)1.21.61.21.5Vapor Frac0110Mole Flow(kmol/hr)789.77420.9431.862808.854Mass Flow(kg/hr)25143867.69759.58725951.11Volume Flow(cum/hr)30.982284.88336.53432.45Enlpy(Gcal/hr)-45.4270.07-0.006-45.351H(Gcal/hr)Hin =-45.357Hout =-45.357表 2-17 甲醇水分离膜

42、负荷计算表表 2-18 甲醇水分离膜能量平衡计算表2.3.2 甲醇提纯塔(T0301)表 2-19 甲醇提纯塔物流焓变计算表表 2-20 甲醇提纯塔负荷计算表CONDENSERREBOILERHeat duty(Gcal/hr)-11.88894214.5544585Q= 2.655643Gcal/hrW=0流入物料流出物料 1流出物料 2Temperature ()6066.7105.9Prere(bar)1.41.11.25Vapor Frac000Mole Flow(kmol/hr)3107.297202.9072904.391Mass Flow(kg/hr)58847.4926491.

43、92952355.563Volume Flow(cum/hr)63.3338.75557.43Enlpy(Gcal/hr)-207.951-11.351-193.935H(Gcal/hr)Hin =-207.951Hout =-205.286Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)0.739513060-548.274-547.5340Heating dutyHeat duty(Gcal/hr)-31.588003Q= -0.73951306Gcal/hrW=0Mass Flow(kg/hr)253895.934195048

44、.44258847.492Volume Flow(cum/hr)320.304255.39463.333Enlpy(Gcal/hr)-548.274-339.583-207.951H(Gcal/hr)Hin =-548.274Hout =-547.534表 2-21 甲醇提纯塔能量平衡计算表2.3.3甲醇分离塔(T0302)表 2-22 甲醇分离塔物流焓变计算表表 2-23 甲醇分离塔负荷计算表表 2-24 甲醇分离塔能量平衡计算表2.4 副产物提取工段表 2-25 副产物提取段物流焓变计算表401405408410411Temperature ()418.871129468.87454343

45、3.743691375.533208410.746531Prere(bar)140000130000140000110000130000Vapor Frac00000Mole Flow(kmol/hr)0.009833320.003155110.000780340.001161870.00473598Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)0.340-67.917-67.5750.002CONDENSERREBOILERHeat duty(Gcal/hr)-14.60110214.9419372Q= 0.34Gcal/hrW

46、=0流入物料流出物料 1流出物料 2Temperature ()6066.9145.7Prere(bar)1.41.11.4Vapor Frac000Mole Flow(kmol/hr)1179.9991144.59935.4Mass Flow(kg/hr)39009.68836439.132570.558Volume Flow(cum/hr)51.07949.0993.05Enlpy(Gcal/hr)-67.917-64.181-3.394H(Gcal/hr)Hin =-67.917Hout =-67.575Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/

47、hr)Errcal/hr)2.6556430-207.951-205.2860表 2-26 副产物提取负荷计算表表 2-27副产物提取段能量平衡计算表2.5 环氧丙烷提纯工段表 2-28环氧丙烷提纯物流焓变计算表表 2-29 环氧丙烷提纯负荷计算表502503504508Temperature ()326.625109313.15350.707402309.894019Prere(bar)140000125000140000110000Vapor Frac0.02810845000Mole Flow(kmol/hr)0.397544780.096813020.344230630.1501271

48、8Mass Flow(kg/hr)16.63514251.745185459.671211738.70911608Volume Flow(cum/hr)0.237434080.001782650.012808510.01080326Enlpy(Gcal/hr)-65.137666-23.690657-73.088568-15.557043H(Gcal/hr)Hin=-88.828316Hout =-88.6456Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)0.0213230-3.394439-3.3730CONDENSERREB

49、OILERHeat duty(Gcal/hr)-2.0462092.067532Q=0.021323Gcal/hrW=0Mass Flow(kg/hr)0.714043930.240063510.026573830.021144160.42626242Volume Flow(cum/hr)0.000847120.000288050.0000207432.3109E-050.00053381Enlpy(Gcal/hr)-3.394439-1.2325481-0.1182629-0.2800098-1.7422659H(Gcal/hr)Hin=-3.394439Hout =-3.373表 2-30

50、 环氧丙烷提纯段能量平衡计算表Q(Gcal/hr)W(Gcal/hr)Hin(Gcal/hr)Hout(Gcal/hr)Errcal/hr)0.18210-88.828316-88.64560CONDENSERREBOILERHeat duty(Gcal/hr)-27.889128.0712Q=0.1821Gcal/hrW=0附录 3 设备选型一览表表 3-1 泵选型一览表泵泵的名称水泵型号介质转速n(r/min)单泵运行参数水泵运行方式电机参数流量Q(L/s)扬程H(m)轴功率P(kw)电机功率 (kw)效率(%)台数方式总轴功率 P(kw)电机总功率 (kw)总台数P0101H2O2 原料

51、泵IS100-80-125双氧水145013.215.190.861.577.141单泵0.871.52P0102甲醇原料泵IS100-80-160甲醇145012.898.331.352.277.911单泵1.352.22P0103原料泵XA80/16甲醇混合物145024.018.732.62378.353并联7.8696P0104物料泵IS200-150-250B甲醇、水、副产物14508016.1515.572281.361单泵15.57222P0105PO 分离塔冷凝回流泵IX180-65-160甲醇、环氧丙烷290011.2134.255.044.574.512串联10.194P0

52、106丙烯分离塔给料泵IX100-80-125A丙烯混合物290022.2517.294.835.577.911单泵4.835.52P0201丙烯分离塔回流泵IX140-32-160A丙烯29001.5429.181.141.538.231单泵1.141.52P0202丙烯精制塔进料加压泵14SA-10JB丙烯混合物29003.63842.922.91452.211单泵2.9142P0203丙烯精制塔回流泵100FYS32丙烯290023.6733.7910.151577.212串联10.15154P0204原料回收泵XA50/13丙烯14509.0205.570.681.171.452串联1

53、.382.24P0301膜分离器泵QXG250-27-30甲醇、水98070.9427303976.921单泵30392P0302甲醇提纯塔给料泵IS1100-80-160A甲醇、水290018.531.547.451176.611单泵7.46112P0303甲醇提纯塔回流泵GDF80-30水290014.5624.153.585.577.821单泵3.585.52P0304甲醇分离塔回流泵80D-12甲醇、副产物29507.00753.955.657.565.561单泵5.657.52P0401副产物分离塔给料泵25FYS-16副产物混合物29000.847317.310.460.5531.

54、251单泵0.460.552P0402副产物分离塔回流泵IX140-32-125A丙二醇甲醚、双氧水29001.227820.380.560.7542.622串联1.141.54P0403丙二醇精制塔回流泵CQF15-8副产物混合物29000.38616.210.210.2442.254串联0.420.488P0404丙二醇精制塔进料泵ISG20-110副产物混合物29000.4053150.371单泵0.372备注： 所选泵 2 台均为一用一备副产物混合物主要是含有双氧水，水，丙二醇和丙二醇甲醚表 3-2塔选型一览表名称类型内径/mm壁厚/mm高度/mm设计压力/MPa设计温度/封头形式材料

55、保温层保护层总质量/kgT0101PO 分离塔F1Z-4A 浮阀380014677800.1590标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板130647P0405加压给料泵ISL32-25-125丙二醇甲醚、双氧水29000.563622.740.40.7550.421单泵0.40.752P0406丙二醇甲醚分离塔回流泵25MS*8-2.2丙二醇甲醚、水14501.80149.471.822.242.891单泵1.822.22P0407加压进料泵ISG20-110丙二醇甲醚、水28000.538115.930.371单泵0.372P0408丙二醇甲醚精制塔回流泵25MS*4-1.1水145

56、01.14528.51.11单泵1.12P0501萃取精馏塔给料泵25MS*4-1.1水14501.91424.131.11单泵1.12P0502泵IS80-65-125A甲醇、水290013.515.582.75474.841单泵2.7542P0503萃取精馏塔回流泵KZ200-50A环氧丙烷、甲醇295036.6470.83232977.071单泵23292P0504PO 精制塔回流泵IX1100-80-160A环氧丙烷290022.8629.648.321179.801单泵8.32112表 3-3 换热器选型一览表型号类型列管材料内径/mm/mm列管规格/mm排列方式管数/根管程数换热面

57、积/m2管程壳程重量/ kgE0101BEM-600-0.345-48.8-2/19-1/3管板式6002000192正三角形430148.820Q345B1628E0102BEM-1000-0.345/4.413-170.5-3/25-1/2热虹吸式再沸器10003000252.5正三角形7491170.5Q345RQ345D9084E0103BEM-400-0.345-61.3-6/19-1管板式4006000192正三角形174161.320Q345B1636T0201丙烯分离塔F1Z-3A 浮阀0.6-15标准椭圆封头Q345R复合硅酸盐卷毡铝合金板32451T0202丙烯精制塔F1Z

58、-3A 浮阀1.235标准椭圆封头Q345R复合硅酸盐卷毡铝合金板46443T0203吸收塔25mm填料70010280300.1520标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板13386T0301甲醇提纯塔F1Z-4A 浮阀280014217500.15110标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板65806T0302甲醇分离塔F1Z-4A 浮阀300014511900.15150标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板84602T0401副产物分离塔50mm 不锈钢填料80010345300.15180标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板14719T0402丙二醇

59、精制塔50mm 不锈钢填料60010211700.15200标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板10875T0403丙二醇甲醚分离塔F1Z-3A 浮阀100010423200.15165标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板19597T0404丙二醇甲醚精制塔50mm 不锈钢填料60010280300.15140标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板12707T0501萃取精馏塔F1Z-4A 浮阀380014541450.1580标准椭圆封头Q235-B复合硅酸盐卷毡铝合金板119944T0502PO 精制塔F1Z-4A 浮阀320014258900.1545标准椭圆

60、封头Q235-B/67496E0104BEM-700-0.345-99.4-3/19-2/6管板式7003000192正三角形574299.4Q235-BQ345D2819E0201BEM-273-0.345/0.552-5.4-1.5/19-1管板式2731500192正三角形6515.420Q345B344E0202BEM-450-1.103/0.552-58.4-6/25-2管板式6003000252.5正三角形41627220Q345B5220E0203BEM-1800-4.413/0.552-72-3/25-2热虹吸式再沸器4506000252.5正三角形126258.4Q345R0