初步設(shè)計(jì)說明書附錄

1、附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)目錄第一章 物料衡算11.11.21.3概述1衡算方法1全廠物料衡算21.3.11.3.21.3.3丁二烯抽提車間物料衡算2MTBE 反應(yīng)精餾車間物料衡算7甲乙酮車間物料衡算13第二章 熱量衡算242.12.22.32.4概述24熱量衡算原則24熱量衡算任務(wù)24各車間熱量衡算252.4.1 丁二烯抽提車間252.4.2 MTBE 反應(yīng)精餾車間322.4.3 甲乙酮車間36第三章 熱集成及節(jié)能技術(shù)513.13.2概述51全廠物流提取513.2.13.2.2丁二烯抽提和MTBE 反應(yīng)精餾車間51甲乙酮車間523.3夾點(diǎn)溫度的確定533.3.1 丁二烯抽提和 M

2、TBE 反應(yīng)精餾車間533.3.2 甲乙酮車間55換熱網(wǎng)絡(luò)設(shè)計(jì)573.4.1 丁二烯抽提和MTBE 反應(yīng)精餾車間573.4.2 甲乙酮車間623.4第四章 設(shè)備選型與典型設(shè)備設(shè)計(jì)674.1 塔設(shè)備的設(shè)計(jì)674.1.1 設(shè)計(jì)規(guī)范674.1.2 設(shè)計(jì)目標(biāo)674.1.3 塔設(shè)備選型原則684.1.4 塔設(shè)備選型結(jié)果764.2反應(yīng)器的設(shè)計(jì)與優(yōu)化1244.2.14.2.24.2.3催化劑的選擇124反應(yīng)器的選擇125反應(yīng)器的設(shè)計(jì)1251附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)4.2.4MTBE預(yù)反應(yīng)器及丁烯水合反應(yīng)器概述1384.3換熱器的選型1424.3.14.3.24.3.34.3.44.3.5選型規(guī)

3、范142概述142選型原則142選型結(jié)果150換熱器總傳熱系數(shù)校核1584.4泵選型1614.4.14.4.24.4.34.4.3選型依據(jù)161泵的分類和適用范圍161選泵原則164選型結(jié)果1684.5壓縮機(jī)選型1734.5.1 選型依據(jù)1734.5.2 壓縮機(jī)的適用范圍和特點(diǎn)1734.5.3 選型原則1744.5.4 選型結(jié)果1754.6 儲(chǔ)罐選型1764.6.14.6.24.6.34.6.4選型依據(jù)176儲(chǔ)罐的分類和適用范圍176儲(chǔ)存原則178選型結(jié)果178第五章 設(shè)備一覽表189第六章 MSDS2016.16.26.3概述201車間所所涉及的化學(xué)品201MSDS 數(shù)據(jù)2012算衡料物章一

4、第附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)第一章 物料衡算1.1概述物料衡算是質(zhì)量守恒定律的一種表現(xiàn)形式。在化學(xué)工程中，確定原材料消耗定額，確定生產(chǎn)過程的損耗量，核算生產(chǎn)過程的效益，對(duì)設(shè)備進(jìn)行最佳設(shè)計(jì)以及確定最佳操作條件等都要進(jìn)行物料衡算。物料衡算是車間工藝設(shè)計(jì)的基礎(chǔ)。本項(xiàng)目為利用總廠混合 C4 原料，經(jīng)過化學(xué)反應(yīng)和分離，得到丁二烯、MTBE 和甲乙酮三種主，同時(shí)副產(chǎn)液化石油氣、氫氣。通過對(duì)全過程或單元過程的物料衡算，計(jì)算出物料的消耗量、主副量、輸出過程物料的損耗量以及三廢產(chǎn)生量；并在此基礎(chǔ)上作熱量衡算，計(jì)算出蒸汽、水、電、煤或其它的消耗定額；同時(shí)根據(jù)衡算所得的各單元設(shè)備物料的物流量及其組成、能

5、量負(fù)荷及其等級(jí)，對(duì)輔助設(shè)備進(jìn)行選型和設(shè)計(jì)，從而對(duì)全過程的設(shè)備費(fèi)用進(jìn)行估價(jià)，并最終確定全廠各項(xiàng)技術(shù)指標(biāo)。1.2 衡算方法系統(tǒng)中物料衡算一般表達(dá)式為：系統(tǒng)中的積累=輸入-輸出+生成-消耗式中，生成或消耗項(xiàng)是由于化學(xué)反應(yīng)而生成或消耗的量；積累量可以是正值，也可以是負(fù)值，當(dāng)系統(tǒng)中積累量不為零時(shí)稱為非穩(wěn)定狀態(tài)過程；積累量為零時(shí)，稱為穩(wěn)定狀態(tài)過程。穩(wěn)定狀態(tài)過程時(shí)，可以簡(jiǎn)化為：輸入=輸出-生成+消耗對(duì)無化學(xué)反應(yīng)的穩(wěn)定過程，又可表示為：輸入=輸出物料衡算包括總質(zhì)量衡算、組分衡算和元素衡算。各種衡算方法的適用情況如下表 1-1 所示：表 1-1 物料衡算式使用范圍1類別物料衡算形式無化學(xué)反應(yīng)有化學(xué)反應(yīng)附錄廈門大

6、學(xué) Noahs Ark 團(tuán)隊(duì)由于系統(tǒng)中存在化學(xué)反應(yīng)，我們主要采用總質(zhì)量衡算的的衡算方法，同時(shí)列出每種物料組分的質(zhì)量流量便于查找和計(jì)算。1.3 全廠物料衡算本廠主要分為丁二烯抽提車間、MTBE 反應(yīng)精餾車間和甲乙酮車間。1.3.1 丁二烯抽提車間物料衡算丁二烯抽提車間是將混合 C4 中丁二烯進(jìn)行抽提精制，得到余 C4 則送往 MTBE 反應(yīng)精餾車間，同時(shí)副產(chǎn)液化石油氣。流程主要包括兩段萃取精餾系統(tǒng)、兩段普通精餾系統(tǒng)，以及溶劑脫氣及再生丁二烯，抽系統(tǒng)。主要設(shè)備有原料閃蒸罐、T101 主洗塔、T102 精餾塔、T103 后洗塔、T104 脫氣塔、T105 第一精餾塔、T106 冷卻塔、T107 炔烴

7、洗滌塔、T108 第二精餾塔。下面對(duì)主要物流設(shè)備進(jìn)行物料衡算。表 1-2 丁二烯抽提車間總物料衡算2項(xiàng)目進(jìn)料出料C4 進(jìn)料新鮮NMPTBC新鮮H2O抽余 C4丁二烯液化石油氣污水Temperature()25.040.025.025.034.018.14413.7Pressure(bar)3.9001.6203.5001.5203.7704.0004.8242.3Vapor(Frac)0.0000.0000.0000.0000.0000.0000.0000.000Mole Flow(kmol/hr)635.2950.6240.12822.761315.208301.46926.62215.49

8、9Mass Flow(kg/hr)3500045.5083.800410.03917624.20816302.5001073.835458.804VolumeFlow(cum/hr)57.9650.0450.0030.41330.37526.0971.6660.543總衡算式總質(zhì)量衡算式適用適用總物質(zhì)的量衡算式適用不適用組分衡算式組分質(zhì)量衡算式適用不適用組分物質(zhì)的量衡算式適用不適用元素原子衡算式元素原子質(zhì)量衡算式適用適用元素原子物質(zhì)的量衡算式適用適用附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-3V102 閃蒸罐物料流股衡算表表 1-4主洗塔 T101 物料流股衡算表3項(xiàng)目進(jìn)料出料C4 進(jìn)料N

9、MP抽余 C4NMP+BDTemperature()42.140.034.0137.8項(xiàng)目進(jìn)料出料預(yù)熱后原料閃蒸后原料高沸點(diǎn)組分Temperature()44.044.044.0Pressure(bar)3.9004.8244.824Vapor(Frac)1.0001.0000.000Mole Flow(kmol/hr)635.295632.1193.176Mass Flow(kg/hr)35000.00034824.729175.271Volume Flow(cum/hr)3944.2333098.7180.302Enthalpy(Gcal/hr)7.6157.5520.023Mass Fl

10、ow(kg/hr)C3H8105.000104.8070.193C4H10-01980.000974.7035.297C4H10 -02210.000209.1420.858C4H8 -014760.0004737.07722.923C4H8 -021680.0001669.66310.337C4H8 -032030.0002018.41311.587C4H8-047805.0007768.81236.188C4H6 -0116590.00016507.90682.094C4H6 -0270.00069.4780.522C4H6 -0370.00069.5400.460C3H4 -0135.0

11、0034.9080.092C4H4560.000556.5613.439C5H12 -01105.000103.7181.282Enthalpy(Gcal/hr)4.175-0.040-0.009-1.553-3.0886.2410.212-0.636合計(jì)(kg/hr)35459.3535459.35附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-5T103 后洗塔物料流股衡算表4項(xiàng)目進(jìn)料出料NMP精餾塔塔頂氣相粗丁二烯塔釜富炔組分Temperature()40.061.073.935.3Pressure(bar)3.8003.8003.6503.800Vapor(Frac)0.0000.000

12、1.0001.000Mole Flow(kmol/hr)392.862572.853317.703497.695Pressure(bar)3.8503.8003.7703.900Vapor(Frac)1.0000.0000.0000.000Mole Flow(kmol/hr)632.1194802.411315.2085119.322Mass Flow(kg/hr)34824.729350000.00017624.208367200.521Volume Flow(cum/hr)3950.298346.89730.375412.214Enthalpy(Gcal/hr)7.552-313.056-

13、3.088-286.467Mass Flow(kg/hr)C3H8104.8070.000104.8070.000C4 H10-01974.7030.000974.7030.000C4 H10-02209.1420.000209.1420.000C4H8-014737.0770.0004733.7423.335C4H8-021669.6630.0001651.32818.335C4H8 -032018.4130.0002013.4434.970C4H8-047768.8120.0007768.6620.150C4H6-0116507.9060.00018.75516489.151C4H6-02

14、69.4780.0000.00869.471C4H6-0369.5400.0000.00069.540C3H4-0134.9080.0000.53334.374C4H4556.5610.0000.000556.561H2O0.00028000.00045.38427954.617C5H9N-010.000322000.0000.000322000.000C5H12-01103.7180.000103.7020.017附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-6T104 脫氣塔物料流股衡算表5項(xiàng)目進(jìn)料出料T102 塔釜含烴溶劑T107 循環(huán)水循環(huán)溶劑富烴溶劑輕炔類Temperature()1

15、12.0114.737.4139.1143.5Pressure(bar)1.6001.6001.5201.5981.620Vapor(Frac)0.0000.0001.0001.0000.000Mole Flow(kmol/hr)5194.48126.85713.62313.0565194.659Mass Flow(kg/hr)379035.759547.976697.458300.000378586.277VolumeFlow(cum/hr)402.2400.610231.383280.049414.824Enthalpy(Gcal/hr)-317.612-1.7850.751-0.732-

16、316.392Mass Flow(kg/hr)Mass Flow(kg/hr)28631.78538731.82516796.54726896.587Volume Flow(cum/hr)28.37845.4302379.7073095.327Enthalpy(Gcal/hr)-25.610-20.0447.70813.273Mass Flow(kg/hr)C3H80.0000.0000.0000.000C4H10-010.0000.0000.0000.000C4H10-020.0000.0000.0000.000C4H8-010.0001.0553.3354.389C4H8-020.0006

17、.83818.33325.170C4H8-030.0001.7154.9706.684C4H8-040.0000.0400.1500.190C4H6-010.00010056.32316306.22726362.551C4H6-020.00049.83767.776117.613C4H6-030.00059.57153.448113.019C3H4-010.00015.71434.08549.799C4H40.000149.81867.326217.143H2O2290.5432093.388197.1610.006C5H9N-0126341.24226297.52143.7210.000C5

18、H12-010.0000.0050.0170.022附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-7第二精餾塔 T108 物料流股衡算表6項(xiàng)目進(jìn)料出料粗丁二烯丁二烯廢水Temperature()63.914.313.7Pressure(bar)7.8002.0002.300Vapor(Frac)0.0000.0000.000Mole Flow(kmol/hr)316.831301.38515.446Mass Flow(kg/hr)16757.84716300.000457.847Volume Flow(cum/hr)29.47925.9030.542Enthalpy(Gcal/hr)6.120

19、6.247-0.632Mass Flow(kg/hr)C4H8-013.2973.2970.000C4H8-0218.32915.9002.429C4H8-034.9674.9130.054C4H8-040.1460.1460.000C4H6-01182.9240.000182.9140.0080.002C4H6-021.6950.0001.6940.0000.000C4H6-0316.0920.00016.0810.0060.005C3H4-010.2900.0000.2900.0000.000C4H4489.2360.010486.2440.9962.005H2O30047.998469.

20、58310.230220.60730286.745C5H9 N-01348297.52178.3820.00278.382348297.520Mass FracC4H6-010.0000.0000.2620.0000.000C4H6-020.0000.0000.0020.0000.000C4H6-030.0000.0000.0230.0000.000C3H4-010.0000.0000.0000.0000.000C4H40.0010.0000.6970.0030.000H2O0.0790.8570.0150.7350.080C5H9N-010.9190.1430.0000.2610.920附錄

21、廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-8萃取劑 NMP 物料衡算表1.3.2MTBE 反應(yīng)精餾車間物料衡算MTBE 反應(yīng)精餾車間主要是將丁二烯抽提車間抽余C4 中異丁烯與甲醇反應(yīng)生產(chǎn)甲基叔丁基醚（反應(yīng)異丁烯轉(zhuǎn)化率可達(dá) 99.5%），醚后 C4 主要含正丁烯，進(jìn)7項(xiàng)目T101 加萃取劑T102 加萃取劑循環(huán)回用NMP新鮮 NMP進(jìn)料Temperature()40.040.0143.540.0Pressure(bar)3.8003.8001.6201.620Vapor(Frac)0.0000.0000.0000.000Mole Flow(kmol/hr)4802.411392.8625194.

22、6590.624Mass Flow(kg/hr)350000.00028631.785378586.27745.508Volume Flow(cum/hr)346.89728.378414.8240.045Enthalpy(Gcal/hr)-313.056-25.610-316.392-0.040Mass Flow kg/hrH2O28000.0002290.54330286.7573.641C5H9N-01322000.00026341.242348297.52041.867合計(jì)378631.785378631.785Mass FracH2O0.0800.0800.0800.080C5H9N

23、-010.9200.9200.9200.920C4H6-0116293.61416238.04355.572C4H6-0267.7761.21966.557C4H6-0353.4476.27047.177C3H4-016.7516.7510.000C4H467.32123.46043.861H2O197.8890.000197.889C5H9N-0143.7210.00043.721C5 H12-010.0170.0000.017C10 H1-010.5720.0000.572附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)入后續(xù)車間進(jìn)行甲乙酮。流程中主要包括 MTBE 混相預(yù)反應(yīng)器 R201、MTBE

24、 反應(yīng)精餾塔 T201、甲醇水洗塔 T202 和甲醇回收塔 T203 等 4 個(gè)主要設(shè)備。表 1-9MTBE 反應(yīng)精餾車間總物料衡算表 1-10預(yù)反應(yīng)器 R201 物料流股衡算表8項(xiàng)目反應(yīng)器進(jìn)口原料反應(yīng)器出口Temperature()40.060.0Pressure(bar)12.5008.500Vapor(Frac)0.0000.000Mole Flow(kmol/hr)458.078324.767Mass Flow(kg/hr)22194.67422194.674Volume Flow(cum/hr)35.78736.226Enthalpy(Gcal/hr)-11.076-12.054Ma

25、ss Flow(kg/hr)C3H8104.817104.817C4H10 -01975.328975.328C4H10 -02209.280209.280C4H8 -014738.1914738.191C4H8 -021654.7481654.748項(xiàng)目進(jìn)料出料抽余 C4新鮮甲醇MTBE醚后 C4污水Temperature()34.025.0133.513.340.0Pressure(bar)3.7701.0007.5003.0002.300Vapor(Frac)0.0000.0000.0001.0000.000Mole Flow(kmol/hr)315.208138.880137.3321

26、76.3952.886Mass Flow(kg/hr)17624.2084435.80012100.009908.00052.008Volume Flow(cum/hr)30.3755.59121.0271287.4820.053Enthalpy(Gcal/hr)-3.088-8.051-9.504-1.025-0.198合計(jì)(kg/hr)22060.00822060.008附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-11萃取精餾塔 T201 物料流股衡算表9項(xiàng)目進(jìn)料出料預(yù)反應(yīng)器出口補(bǔ)充甲醇液MTBE塔頂氣相Temperature()60.040.0133.557.9Pressure(bar

27、)8.5008.0007.5007.000Vapor(Frac)0.0000.0000.0000.000Mole Flow(kmol/hr)324.7674.176137.332187.311Mass Flow(kg/hr)22194.674133.59512100.00010228.269Volume Flow(cum/hr)36.2260.17221.02718.333Enthalpy(Gcal/hr)-12.054-0.240-9.504-2.293Mass Flow(kg/hr)C3H8104.8170.0000.000104.818C4H10 -01975.3280.0180.021

28、975.325C4H10 -02209.2800.0040.001209.282C4H8-014738.1910.1300.0594738.262C4H8-021654.7480.1000.0851654.763C4H8-032016.7860.0980.0642016.819C4H8-04288.9210.0010.02447.614C4H6-0118.7710.0000.00018.772C4H8 -032016.7862016.786C4H8 -047768.679288.921C4H6 -0118.77118.771C4H6 -020.0080.008C4H6-030.0000.000

29、C3H4 -010.5410.541H2O77.15976.992C5H12 -01103.702103.702C5H12 -0219.05511769.575CH4O4507.540236.259C4H10 -030.0690.755附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-12水萃取塔 T202 物料流股衡算表10項(xiàng)目進(jìn)料出料催化精餾塔出料循環(huán)水含水甲醇醚后 C4Temperature()57.940.0100.813.3Pressure(bar)7.0003.0003.3003.000Vapor(Frac)0.0000.0000.0001.000Mole Flow(kmol/hr)1

30、87.311144.321155.236176.395Mass Flow(kg/hr)10228.2692600.0002920.2699908.000Volume Flow(cum/hr)18.3332.6553.2771287.482Enthalpy(Gcal/hr)-2.293-9.918-10.293-1.025Mass Flow(kg/hr)C3H8104.8180.0000.010104.808C4H10-01975.3250.0000.542974.783C4H10-02209.2820.0000.124209.158C4H8-014738.2620.0004.0224734.2

31、40C4H8-021654.7630.0003.0831651.679C4H8-032016.8190.0003.0142013.806C4H8-0447.6140.0000.01647.598C4H6-0118.7720.0000.01418.758C4H6-020.0080.0000.0000.008C4H6-030.0000.0000.0000.000C4H6-020.0080.0000.0000.008C4H6-030.0000.0000.0000.000C3H4-010.5410.0000.0000.542H2O76.9920.9291.34176.580C5H12-01103.70

32、20.0000.261103.441C5H12 -0211769.5750.55712097.30951.900CH4O236.259131.7560.108230.114C4H10 -030.7550.0020.7260.031附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-13甲醇回收塔物料流股衡算表11項(xiàng)目進(jìn)料出料含水甲醇循環(huán)甲醇塔釜出水Temperature()100.839.4107.2Pressure(bar)3.3001.0001.300Vapor(Frac)0.0000.0000.000Mole Flow(kmol/hr)155.2368.029147.207Mass Flow(

33、kg/hr)2920.269268.2692652.000Volume Flow(cum/hr)3.2770.3482.912Enthalpy(Gcal/hr)-10.293-0.454-9.830Mass Flow(kg/hr)C3H80.0100.0100.000C4 H10-010.5420.5420.000C4H10-020.1240.1240.000C4H8-014.0224.0220.000C4H8-023.0833.0830.000C4H8-033.0143.0140.000C4H8-040.0160.0160.000C4H6-010.0140.0140.000C4H6-020.

34、0000.0000.000C4H6-030.0000.0000.000C3H4-010.0080.0080.000H2O2659.7597.8052651.954C5H12-010.0010.0010.000C5 H12-0219.48919.4890.000C3H4-010.5420.0000.0080.534H2O76.5802599.9552659.75916.775C5H12-01103.4410.0000.001103.441C5H12-0251.9000.00019.48932.411CH4O230.1140.045230.1560.003C4H10-030.0310.0000.0

35、310.000附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-14循環(huán)甲醇物料衡算表12項(xiàng)目新鮮甲醇進(jìn)料循環(huán)甲醇進(jìn)預(yù)反應(yīng)器原料甲醇催化精餾塔調(diào)節(jié)用甲醇Temperature()25.030.025.025.0Pressure(bar)1.0001.0001.0001.000Vapor(Frac)0.0000.0000.0000.000Mole Flow(kmol/hr)138.8808.029142.8704.176Mass Flow(kg/hr)4435.800268.2694570.474133.595Volume Flow(cum/hr)5.5910.3435.7610.168Enthal

36、py(Gcal/hr)-8.051-0.461-8.281-0.242Mass Flow(kg/hr)C3H80.0000.0100.0110.000C4H10-010.0000.5420.6250.018C4H10 -020.0000.1240.1370.004C4H8-010.0004.0224.4490.130C4H8-020.0003.0833.4200.100C4H8-030.0003.0143.3430.098C4H8-040.0000.0160.0180.001C4H6-010.0000.0140.0160.000C3H4-010.0000.0080.0080.000H2O18.

37、2647.80531.7830.929C5H12 -010.0000.0010.0010.000C5H12-020.00019.48919.0550.557CH4O4417.536230.1104507.540131.756C4H10 -030.0000.0310.0690.002總計(jì)(kg/hr)4704.0694704.069CH4 O230.156230.1100.046C4 H10-030.0310.0310.000附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)1.3.3甲乙酮車間物料衡算甲乙酮車間主要是利用醚后 C4（主要成分為正丁烯）水合得仲丁醇，后仲丁醇脫氫制得甲乙酮，同時(shí)副產(chǎn)氫氣、少量

38、仲丁醚、粗叔丁醇、重質(zhì)物以及液化石油氣。車間主要設(shè)備分為塔器和反應(yīng)器兩種，共有塔器 13 臺(tái)，正丁烯水合反應(yīng)器一臺(tái)，仲丁醇脫氫反應(yīng)器 4 臺(tái)。表 1-15丁烯提濃及水合工段總物料衡算表 1-16 仲丁醇精制及脫氫（制甲乙酮）工段總物料衡算13項(xiàng)目進(jìn)料出料粗SBAH2O己烷甲 乙酮重質(zhì)物仲丁醚叔丁醇污水工藝水副氫氣Tempe rature ()25.025.040.0102.2165.786.194.040.045.00.000Pressure (bar)7.0007.0002.0002.0006.5002.5001.8001.0003.0002.500Vapor(Frac)0.0000.000

39、0.0000.0000.0001.0000.0000.0000.0001.000Mole Flow(kmol/hr)104.16133.3050.03195.7560.6218.6253.83625.5842.22096.977項(xiàng)目進(jìn)料出料醚后C4新鮮萃取劑NMF+MEKH2O粗 SBA液化石油氣瓦斯氣罐污水馳放氣Temperature()40.052.025.0159.530.097.925.092.5Pressure(bar)2.0005.4001.0007.0006.0001.0001.0001.000Vapor(Frac)1.0000.0000.0000.0000.0001.0000.

40、0001.000Mole Flow(kmol/hr)175.9730.015582.839104.14563.10915.279468.7590.377Mass Flow(kg/hr)9908.0001.331105007707.4083743.150388.3858559.02711.354Volume Flow(cum/hr)2190.6610.001510.56412.1746.268466.64011.88711.353Enthalpy(Gcal/hr)-0.884-0.0011-40.193-7.442-0.972-0.813-31.749-0.015合計(jì)(kg/hr)20409.3

41、3120409.331附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-17萃取精餾塔 T302 物料流股衡算表14項(xiàng)目進(jìn)料出料醚后 C4NMF+MEK液化石油氣含丁烯萃取劑Temperature()75.052.039.7115.1Pressure(bar)5.4005.4005.0005.200Vapor(Frac)1.0000.0000.0000.000Mole Flow(kmol/hr)175.9731349.19340.1951484.971Mass Flow(kg/hr)9908.000119610.0002257.000127261.000Volume Flow(cum/hr)858

42、.174131.2634.055156.306Enthalpy(Gcal/hr)-0.725-98.513-0.700-95.006Mass Flow(kg/hr)C3H8105.3940.000105.3860.008C4H10-01979.8510.622664.651315.823C4H10-02210.2900.005205.8934.402C4H8-014761.42621.3211235.2473547.500C4H8-021659.46916.4723.4701672.471C4H8-032023.74415.07515.9802022.839C4H8-0445.1860.064

43、24.79920.451C4H6-0118.8580.2200.22618.852C4H6-020.0080.0010.0000.008C3H4-010.5360.0150.0130.537C5H12-01103.2380.6420.004103.876C5H9 N-020.00059777.9590.00059777.959C4 H8O-010.00059777.6051.33059776.274Mass Flow (kg/hr)7707.408600.0002.7006905.00051.207460.000149.640467.05140.000237.209Volume Flow(cu

44、m/hr)9.6390.6040.0049.6900.08099.1460.1910.4710.041880.964Enthalpy (Gcal/hr)-8.251-2.272-0.001-5.958-0.0438-0.303-0.272-1.758-0.152-0.0575合計(jì)(kg/hr)8310.3088310.308附錄廈門大學(xué) Noahs Ark 團(tuán)隊(duì)表 1-18丁烯汽提塔 T303 物料流股衡算表表 1-19丁烯水合反應(yīng)器 R302 物料流股衡算表15項(xiàng)目進(jìn)料出料原料水預(yù)反應(yīng)器出口 C4循環(huán)丁烯水合反應(yīng)器水相水合反應(yīng)器有機(jī)相Temperature()25.035.530.0174.

45、9155.0Pressure(bar)1.0004.7006.60070.00064.000項(xiàng)目進(jìn)料出料含丁烯萃取劑循環(huán)萃取劑丁烯Temperature()115.1157.345.6Pressure(bar)5.2004.8004.700Vapor(Frac)0.0000.0001.000Mole Flow(kmol/hr)1484.9711352.223132.748Mass Flow(kg/hr)127261.000119800.0007461.000Volume Flow(cum/hr)156.306150.131676.916Enthalpy(Gcal/hr)-95.006-91.547-0.279Mass Flow(kg/hr)C3H80.0080.0000.008C4H10 -01315.8232.017313.807C4H10-024.4020.0144.388C4H8-013547.50057.3623490.138C4H8-021672.47148.7121623.759C4H8-032022.83945.0401977.799C4