XX35萬噸/年乙二醇項目附錄XX35萬噸/年乙二醇項目附錄2015年8月12日目錄附錄一物料衡算一覽表 11.1物料衡算 11.1.1物料衡算的意義 11.1.2物料衡算的任務 11.1.3物料衡算遵循的原則 11.1.4系統物料衡算 21.1.5物耗一覽表 21.2能量衡算 31.2.1能量衡算的目的 31.2.2能量衡算可以解決的問題 31.2.3能量衡算遵循的原則 41.2.4系統能量衡算 41.3合成氣分離工段 51.3.1閃蒸罐 51.3.2甲烷洗滌塔 61.3.3氣提塔 61.3.4脫甲烷塔 71.4酯化再生工段 81.4.1反應精餾塔（T0201） 81.4.2甲醇雙效精餾高壓塔（T0202) 91.4.3甲醇雙效精餾低壓塔（T0203) 101.5羰化偶聯工段 121.5.1羰化偶聯反應器(R0301) 121.5.2閃蒸罐(V0301) 131.5.3甲醇洗滌塔（T0301) 141.5.4草酸二甲酯回收塔（T0302） 151.5.5常壓恒沸精餾塔(T0303) 161.5.6加壓恒沸精餾塔(T0304) 171.6催化加氫工段 191.6.1加氫反應器（R0401) 191.6.2高壓分離罐（V0401） 201.6.3低壓分離罐(V0402) 221.7精制工段 231.7.1粗產品預分離塔（T0501) 231.7.2脫甲醇塔（T0502) 251.7.3萃取塔（T0503) 261.7.4甲苯回收塔（T0504) 271.7.5乙二醇精制塔（T0505） 281.7.6丙二醇精制塔（T0506） 30附錄二能量衡算一覽表 332.1合成氣分離工段能量衡算 332.1.1閃蒸罐（V0101） 332.1.2甲烷洗滌塔（T0101) 332.1.3氣提塔(T0102) 342.1.4甲烷回收塔（T0103) 352.2酯化再生工段能量衡算 362.2.1酯化塔（T0201) 362.2.2甲醇雙效精餾高壓塔（T0202) 362.2.3甲醇雙效精餾低壓塔（T0203) 372.3羰化偶聯工段能量衡算 382.3.1羰化反應器（R0301) 382.3.2閃蒸罐（V0301) 392.3.3甲醇洗滌塔（T0301) 392.3.4草酸二甲酯回收塔（T0302） 402.3.5常壓恒沸精餾塔(T0303) 412.3.6高壓壓恒沸精餾塔(T0304) 412.4催化加氫工段能量衡算 422.4.1加氫反應器（R0401) 422.4.2高壓分離罐（V0401) 432.4.3低壓分離罐（V0402) 432.4.4氫氣壓縮機（C0402) 442.5精制工段能量衡算 452.5.1粗產品預分離塔（T0501) 452.5.2脫甲醇塔（T0502) 452.5.3萃取塔（T0503) 462.5.4甲苯回收塔（T0504) 472.5.5乙二醇精制塔（T0505) 47附錄三設備一覽表 493.1塔設備一覽表 493.2氣液分離器一覽表 523.3儲罐一覽表 533.4壓縮機一覽表 583.5泵一覽表 593.6反應器一覽表 623.7換熱器一覽表 633.8管道一覽表 67附錄四MSDS數據一覽表 774.1乙二醇 774.2碳酸二甲酯 804.3甲醇 844.4合成氣 884.5亞硝酸甲酯 914.6草酸二甲酯 95附錄一物料衡算一覽表1.1物料衡算1.1.1物料衡算的意義物料衡算是確定化工生產過程中物料比例和物料轉變的定量關系的過程，是化工工藝計算中最基本、最重要的內容之一。在化學工程中，設計或改造工藝流程和設備，了解和控制生產操作過程，核算生產過程的經濟效益，確定主副產品的產率，確定原材料消耗定額，確定生產過程的損耗量，便于技術人員對現有的工藝過程進行分析，選擇最有效的工藝路線，確定設備容量、數量和主要尺寸，對設備進行最佳設計以及確定最佳操作條件等都要進行物料核算。毫不夸張的說，一切化學工程的開發和放大都是以物料衡算為基礎的。1.1.2物料衡算的任務通常物料衡算有兩種情況，一是對已有的生產設備或過程利用實測的數據，計算出另一些不能直接測定的物料量，俗稱生產查定，用此計算結果，對生產進行分析，作出判斷，提出改進措施。二是設計一種新的設備或過程，由物料衡算求出進出各設備的物料量、組成等，然后結合能量衡算，確定設備的工藝尺寸及整個工藝過程。1.1.3物料衡算遵循的原則物料衡算的理論基礎是質量守恒定理。它是研究某一體系內進出物料量及組成的變化。進行物料衡算時，必須先確定衡算的體系。對一般體系，均可用如下表示：系統中的積累=輸入-輸出+生成-消耗在穩定狀態下有：輸入=輸出-生成+消耗特別地，當系統沒有化學反應時，則可簡化為：輸入=輸出1.1.4系統物料衡算詳見附錄一，物料衡算一覽表。1.1.5物耗一覽表表1.1項目綜合物耗計算表序號名稱需要量單價（元/噸）總費用（萬元/年）1合成氣108198.36萬Nm3/年0.6元/Nm3649192甲醇3.9萬噸/年23269071.43一氧化氮1424000Nm3/年0.8元/m3113.924氧氣75289584Nm3/年//5氮氣4077832Nm3/年//6甲苯2.75萬噸/年443012182.397催化劑0.02192萬噸/年32179.5643.59總計86930.32表1.2萬噸產品的物耗序號名稱需要量單價（元/噸）費用（萬元/萬噸/年）1合成氣3091.38萬Nm3/萬噸/年0.6元/Nm31854.8285712甲醇0.0866萬噸/萬噸/年2326201.433一氧化氮40685.7Nm3/萬噸/年0.8元/m36004氧氣2151130.97Nm3/萬噸/年//5氮氣116509.48Nm3/萬噸/年//6甲苯0.07864430405.8867催化劑0.0219232179.518.388總計3080.534表1.3萬元產值綜合物耗序號名稱需要量費用（萬噸/萬元/年）1合成氣108198.36萬Nm3/年0.0005391332甲醇3.9萬噸/年0.004963一氧化氮1424000Nm3/年0.0016666674氧氣75289584Nm3/年/5氮氣4077832Nm3/年/6甲苯2.75萬噸/年0.0024637467催化劑0.02192萬噸/年0.054382448總計0.0003251.2能量衡算1.2.1能量衡算的目的對于新設計的生產車間，能量衡算的主要目的是確定設備的熱負荷。根據設備的熱負荷的大小、所處理物料的性質及工藝要求再選擇傳熱面的形式、計算傳熱面積、確定設備的主要工藝尺寸。確定傳熱所需要的加熱劑或冷卻劑的用量及伴有熱效應的溫升情況。對于已投產的生產車間，進行能量衡算是為了更加合理能量利用，以最大限度降低單位產品的能耗。1.2.2能量衡算可以解決的問題在化工設計、化工生產中，通過能量衡算可以解決以下問題：1.確定物料輸送機械（泵、壓縮機等）和其他操作機械（攪拌、過濾、粉碎等）所需要的功率，以便于確定輸送設備的大小、尺寸和型號；2.確定各單元操作過程（蒸發、蒸餾、冷凝、冷卻等）所需要的熱量或冷量，及其傳遞速率；計算換熱設備的工藝尺寸；為其他專業如供汽、供冷、供水專業提供設計條件；3.化學反應常伴有熱效應，導致體系的溫度上升或下降，為此需確定為保持一定反應溫度所需的移出或加入的熱傳遞速率.4.為充分利用余熱，提高能量利用率，降低能耗提供重要依據，使過程的總能耗降低到最低程度；5.最終確定總需求能量和能量的費用，并用來確定這個過程在經濟上的可行性。1.2.3能量衡算遵循的原則根據能量守恒定律，任何均相體系在時間內的能量平衡關系，表述如下：熱量衡算是能量衡算的一種，在能量衡算中占主要地位。熱量衡算的理論依據是熱力學第一定律。能量守恒表達式如下：即輸入=輸出+損失式中：輸入設備熱量的總和；：輸出設備熱量的總和；：損失熱量的總和。對于連續系統：式中Q：設備的熱負荷;W：輸入系統的機械能;∑Hout：離開設備的各物料焓之和;∑Hin：進入設備的各物料焓之和。1.2.4系統能量衡算詳見附錄二，能量衡算一覽表。1.3合成氣分離工段1.3.1閃蒸罐表1.4閃蒸罐進出料流股表流股信息INOUT123TemperatureC-180-180-180Pressurebar343030VaporFrac0.70201MoleFlowkmol/hr6763.7751954.6374809.138MassFlowkg/hr76052.02148717.38527334.637VolumeFlowcum/hr1084.24572.4521161.771EnthalpyGcal/hr-76.988-52.112-24.8MassFlowkg/hrCO61971.85643288.72618683.13H28481.697169.8688311.829N2191.369108.05883.311CH45407.0995150.732256.367MassFracCO0.8150.8890.683H20.1120.0030.304N20.0030.0020.003CH40.0710.1060.0091.3.2甲烷洗滌塔表1.5甲烷洗滌塔進出料流股表流股信息INOUT1234TemperatureC-180-180-170.8-176.3Pressurebar30303029.4VaporFrac1001MoleFlowkmol/hr48093624097.776MassFlowkg/hr27334.63749526.58367641.4279219.793VolumeFlowcum/hr1161.771109.71139.7221106.095EnthalpyGcal/hr-24.8-66.632-84.597-6.834MassFlowkg/hrCO18683.136.04518539.539149.636H28311.8290179.3278132.503N283.3110.00174.5588.754CH4256.36749520.53748848.003928.901MassFracCO0.68300.2740.016H20.30400.0030.882N20.00300.0010.001CH40.00910.7220.1011.3.3氣提塔表1.6氣提塔進出料流股表流股信息INOUT1234TemperatureC-180-170.8-159.2-124Pressurebar303029.430VaporFrac0010MoleFlowkmol/hr1954.6373798.362224.9425528.057MassFlowkg/hr48717.38567641.4271651.224114707.655VolumeFlowcum/hr72.452139.72268.454302.738EnthalpyGcal/hr-52.112-84.597-1.549-130.609MassFlowkg/hrCO43288.72618539.5391097.38160730.953H2169.868179.327349.1880N2108.05874.5587.936174.68CH45150.73248848.003196.71953802.021MassFracCO0.8890.2740.6650.529H20.0030.0030.2110N20.0020.0010.0050.002CH40.1060.7220.1190.4691.3.4脫甲烷塔表1.7脫甲烷塔進出料流股表流股信息INOUT123TemperatureC-124-147.3-182.1Pressurebar302.82.6VaporFrac001MoleFlowkmol/hr5528.0573352.7662175.29MassFlowkg/hr114707.65553790.4360917.224VolumeFlowcum/hr302.738135.7475846.057EnthalpyGcal/hr-130.609-70.871-60.465MassFlowkg/hrCO60730.9536.56560724.388N2174.680.001174.679CH453802.02153783.86418.157MassFracCO0.52900.997N20.00200.003CH40.469101.4酯化再生工段1.4.1反應精餾塔（T0201）1.8反應精餾塔進出料流股表流股信息INOUT1234TemperatureC53.127.1114.233.9Pressurebar5555VaporFrac00.98401MoleFlowkmol/hr6892.46214898.816146.75214400MassFlowkg/hr220870.51437112.748185333.76472649.498VolumeFlowcum/hr291.13972849.091269.10672946.395EnthalpyGcal/hr-387.907-58.027-345.214-114.765MassFlowkg/hrCO0.07172872.083072872.154O2013274.38200NO0.00477502.735027711.751CH3OH220821.61325350.209170349.40822652.936MN37.28618032.98910.726119347.48DMO00.1150.1150DMC0.0019.2629.2620ET11.3996.00717.2980.109N20.132230064.9350230065.067H2O0.0030.03214946.9520MassFracCO00.16700.154O200.0300NO00.17700.059CH3OH10.0580.9190.048MN00.04100.253DMO0000DMC0000ET0000N200.52600.487H2O000.08101.4.2甲醇雙效精餾高壓塔（T0202)表1.9甲醇雙效精餾高壓塔進出料流股表流股信息INOUT12（液相回流）34（氣相采出）TemperatureC114.2123.4130.2123.4Pressurebar7.577.2527VaporFrac0001MoleFlowkmol/hr6146.7523398.433255.9526289.23MassFlowkg/hr185333.76108830.07292759.845201403.988VolumeFlowcum/hr269.155164.463136.50827734.256EnthalpyGcal/hr-345.194-184.683-185.919-295.762MassFlowkg/hrCO0000O20000NO0000CH3OH170349.408108721.93777867.475201203.87MN10.72612.61023.336DMO0.11500.1150DMC9.2620.0019.2610.001MG0000ET17.2985.00413.0419.261,2-BDO0000H20000N20000H2O14946.95290.52114869.952167.52MassFracCO0000O20000NO0000CH3OH0.9190.9990.8390.999MN0000DMO0000DMC0000MG0000ET00001,2-BDO0000H20000N20000H2O0.0810.0010.160.0011.4.3甲醇雙效精餾低壓塔（T0203)表1.10甲醇雙效精餾低壓塔進出料流股表流股信息INOUT1234TemperatureC130.2100.564.299.7Pressurebar7.2521.21811.218VaporFrac00.03800MoleFlowkmol/hr3255.952122986.8092399.873123843.489MassFlowkg/hr92759.8452.28E+0676899.3642.29E+06VolumeFlowcum/hr136.508120496.54103.2972546.999EnthalpyGcal/hr-185.919-8135.075-134.382-8238.079MassFlowkg/hrCO0000O20000NO0000CH3OH77867.475140328.47676890.231141305.951MN0000DMO0.11516.389016.503DMC9.2611330.70501339.974MG0000ET13.041640.3488.643644.8091,2-BDO0000H20000N20000H2O14869.9522.14E+060.492.15E+06MassFracCO0000O20000NO0000CH3OH0.8390.06210.062MN0000DMO0000DMC00.00100.001MG0000ET00001,2-BDO0000H20000N20000H2O0.160.93800.9381.5羰化偶聯工段1.5.1羰化偶聯反應器(R0301)表1.11羰化偶聯反應器進出料流股表流股信息IN-REACREAC-OUTTemperatureC130130Pressurebar55VaporFrac11MoleFlowkmol/hr15999.43515195.29MassFlowkg/hr517254.21517254.21VolumeFlowcum/hr107021.764101547.139EnthalpyGcal/hr-144.607-172.471MassFlowkg/hrCO118619.72172930.518NO27625.0977255.632CH3OH22540.46522540.465MN119016.6918055.149DMO094960.867DMC02059.336ET7.5087.508N2229444.701229444.701H2O0.0330.033MassFracCO0.2290.141NO0.0530.149CH3OH0.0440.044MN0.230.035DMO00.184DMC00.004ET00N20.4440.444H2O001.5.2閃蒸罐(V0301)表1.12閃蒸罐進出料流股表流股信息INOUT123TemperatureC808080Pressurebar51.51.5VaporFrac0.94810MoleFlowkmol/hr15195.2914780.018415.272MassFlowkg/hr517254.21469723.09947531.111VolumeFlowcum/hr84415.114288970.93744.419EnthalpyGcal/hr-188.371-114.118-69.937MassFlowkg/hrCO72930.51872927.2943.224O2000NO77255.63277255.140.492CH3OH22540.46522020.382520.083MN18055.14918014.7640.389DMO94960.86748115.86646845DMC2059.3361945.803113.533ET7.5087.2250.283N2229444.701229436.5968.105H2O0.0330.0330MassFracCO0.1410.1550O2000NO0.1490.1640CH3OH0.0440.0470.011MN0.0350.0380.001DMO0.1840.1020.986DMC0.0040.0040.002ET000N20.4440.4880H2O0001.5.3甲醇洗滌塔（T0301)表1.13甲醇洗滌塔進出料流股表流股信息INOUT1234TemperatureC8064.675.55.2Pressurebar611VaporFrac1001MoleFlowkmol/hr14780.0181022.6771349.05514453.655MassFlowkg/hr469723.09932842.77879608.505422957.655VolumeFlowcum/hr288970.93744.10785.185334021.931EnthalpyGcal/hr-114.118-57.349-125.202-58.27MassFlowkg/hrCO72927.2940072926.694O20000NO77255.140077255.317CH3OH22020.38232706.66629419.92925308.366MN18014.7600.05518014.166DMO48115.86648.11648163.8680.114DMC1945.80337.2361973.839.21MG0000ET7.22550.2950.3527.163H20000N2229436.59600229436.592H2O0.0330.4710.4720.032MassFracCO0.155000.172O20000NO0.164000.183CH3OH0.0470.9960.370.06MN0.038000.043DMO0.1020.0010.6050DMC0.0040.0010.0250MG0000ET00.0020.0010H20000N20.488000.542H2O00001.5.4草酸二甲酯回收塔（T0302）表1.14草酸二甲酯回收塔進出料流股表流股信息INOUT123TemperatureC75.564.6165.2Pressurebar1.06111.068VaporFrac000MoleFlowkmol/hr1349.055941.598407.457MassFlowkg/hr79608.50531492.37948116.126VolumeFlowcum/hr85.18541.57750.023EnthalpyGcal/hr-125.202-54.693-68.878MassFlowkg/hrCO000O2000NO000CH3OH29419.92929419.9120.017MN0.0550.0550DMO48163.86848.16448115.704DMC1973.831973.4250.405MG000ET50.35250.3520H2O0.4720.4720MassFracCO000O2000NO000CH3OH0.370.9340MN000DMO0.6050.0021DMC0.0250.0630MG000ET0.0010.0020H2O0001.5.5常壓恒沸精餾塔(T0303)表1.15常壓恒沸精餾塔進出料流股表流股信息INOUT123TemperatureC93.968.963.5Pressurebar41.21VaporFrac000MoleFlowkmol/hr1533.014918.275614.739MassFlowkg/hr50784.26629497.59521286.671VolumeFlowcum/hr71.04639.91327.646EnthalpyGcal/hr-87.057-51.373-36.781MassFlowkg/hrCO000O2000NO000CH3OH48175.66629361.34718814.319MN19.244019.244DMO48.16448.1640DMC2488.82337.2742451.549MG000ET51.89950.341.558H2O0.4720.4710.001MassFracCO000O2000NO000CH3OH0.9490.9950.884MN000.001DMO0.0010.0020DMC0.0490.0010.115MG000ET0.0010.0020H2O0001.5.6加壓恒沸精餾塔(T0304)表1.16加壓恒沸精餾塔進出料流股表流股信息INOUT123TemperatureC65.7184.4137Pressurebar1310.310VaporFrac000MoleFlowkmol/hr614.73921.568593.17MassFlowkg/hr21286.6711937.59319349.077VolumeFlowcum/hr27.7512.4629.993EnthalpyGcal/hr-36.767-2.976-32.465MassFlowkg/hrCO000O2000NO000CH3OH18814.3192.918811.419MN19.244019.244DMO000DMC2451.5491934.687516.862MG000ET1.5580.0061.5521,2-BDO000H2000N2000H2O0.00100MassFracCO000O2000NO000CH3OH0.8840.0010.972MN0.00100.001DMO000DMC0.1150.9990.027MG000ET0001,2-BDO000H2000N2000H2O0001.6催化加氫工段1.6.1加氫反應器（R0401)表1.17加氫反應器進出料流股表流股信息IN-R401R401-OUTTemperatureC200200Pressurebar2525VaporFrac11MoleFlowkmol/hr49079.7247477.356MassFlowkg/hr216669.584216669.584VolumeFlowcum/hr78040.15475412.612EnthalpyGcal/hr-103.281-127.874MassFlowkg/hrCO258.069258.069NO44.36244.362CH3OH18303.81968868.257MN254.258254.258DMO96623.2681818.505DMC129.043129.043MG4177.9214473.59ET148.712905.4231,2-BDO0.153472.15H295946.07489442.058N2680.358680.358H2O83.0541005.515EG19.50346467.574C3H8O-010.9891850.422MassFracCO0.0010.001NO00CH3OH0.0840.318MN0.0010.001DMO0.4460.008DMC0.0010.001MG0.0190.021ET0.0010.0041,2-BDO00.002H20.4430.413N20.0030.003H2O00.005EG00.214C3H8O-0100.0091.6.2高壓分離罐（V0401）表1.18高壓分離罐進出料流股表流股信息INOUT123TemperatureC404040Pressurebar252020VaporFrac0.94501MoleFlowkmol/hr47477.3562504.07444973.282MassFlowkg/hr216669.584107856.22108813.364VolumeFlowcum/hr47516.477115.01859205.973EnthalpyGcal/hr-220.387-196.611-22.718MassFlowkg/hrCO258.0690.649257.42NO44.3620.04944.313CH3OH68868.25751000.08217868.175MN254.25838.235216.023DMO1818.5051810.8587.647DMC129.043114.32714.717MG4473.594434.61238.979ET905.423757.951147.4721,2-BDO472.15471.9950.155H289442.058089442.057N2680.3581.316679.042H2O1005.515928.85176.664EG46467.57446447.87419.7C3H8O-011850.4221849.4230.999MassFracCO0.00100.002NO000CH3OH0.3180.4730.164MN0.00100.002DMO0.0080.0170DMC0.0010.0010MG0.0210.0410ET0.0040.0070.0011,2-BDO0.0020.0040H20.41300.822N20.00300.006H2O0.0050.0090.001EG0.2140.4310C3H8O-010.0090.01701.6.3低壓分離罐(V0402)表1.19低壓分離罐進出料流股表流股信息INOUT123TemperatureC404040Pressurebar2044VaporFrac010MoleFlowkmol/hr2504.07402504.074MassFlowkg/hr107856.220.001107856.219VolumeFlowcum/hr115.0180.001116.383EnthalpyGcal/hr-196.6110-193.739MassFlowkg/hrCO0.64900.649NO0.04900.049CH3OH51000.0820.00151000.082MN38.235038.235DMO1810.85801810.858DMC114.3270114.327MG4434.61204434.612ET757.9510757.9511,2-BDO471.9950471.995H2000N21.31601.316H2O928.8510928.851EG46447.874046447.874C3H8O-011849.42301849.423MassFracCO00.0050NO00.0010CH3OH0.4730.6330.473MN00.0050DMO0.01700.017DMC0.00100.001MG0.0410.0010.041ET0.0070.0050.0071,2-BDO0.00400.004H200.3340N200.0130H2O0.0090.0020.009EG0.4310.0010.431C3H8O-010.01700.0171.7精制工段1.7.1粗產品預分離塔（T0501)表1.20粗產品預分離塔進出料流股表流股信息INOUT12（側線）345TemperatureC5079.3146.515.115.1Pressurebar40.14VaporFrac00010MoleFlowkmol/hr2504.07463.364779.2571.6611659.792MassFlowkg/hr107856.2195898.68448930.76553.6152973.14VolumeFlowcum/hr116.3835.46349.033398.11965.455EnthalpyGcal/hr-193.739-9.173-82.006-0.077-96.119MassFlowkg/hrCO0.649000.5790.07O200000NO0.049000.0460.003CH3OH51000.08294.231049.81850856.033MN38.2350.00501.24336.987DMO1810.8581654.993155.77800DMC114.3270.53500.194113.597MG4434.6124139.3325.6950.006289.644ET757.9512.43200.307755.2121,2-BDO471.9950471.99500N21.316001.1830.132H2O928.8517.15700.233921.46EG46447.874046447.87400C3H8O-011849.42301849.42300JBEN00000MassFracCO0000.0110NO0000.0010CH3OH0.4730.01600.9290.96MN0000.0230.001DMO0.0170.2810.00300DMC0.001000.0040.002MG0.0410.702000.005ET0.007000.0060.0141,2-BDO0.00400.0100N20000.0220H2O0.0090.00100.0040.017EG0.43100.94900C3H8O-010.01700.038001.7.2脫甲醇塔（T0502)表1.21脫甲醇塔進出料流股表流股信息INOUT1234(側線）TemperatureC15.36398.381.7Pressurebar211.2651.197VaporFrac0000MoleFlowkmol/hr1659.7921587.2356.16216.4MassFlowkg/hr52973.1450879.9711419.394673.775VolumeFlowcum/hr65.47768.1851.5420.909EnthalpyGcal/hr-96.114-88.909-4.086-1.057MassFlowkg/hrCO0.070.0700O20000NO0.0030.00300CH3OH50856.03350829.0910.326.642MN36.98736.98700DMO0000DMC113.5970113.0940.503MG289.6440289.1490.495ET755.21213.687140.715600.81N20.1320.13200H2O921.460876.13545.325MassFracCO0000O20000NO0000CH3OH0.960.99900.04MN0.0010.00100DMO0000DMC0.00200.080.001MG0.00500.2040.001ET0.01400.0990.892N20000H2O0.01700.6170.0671.7.3萃取塔（T0503)表1.22萃取塔進出料流股表流股信息INOUT1234TemperatureC44.7147.2102.244.1Pressurebar1111VaporFrac0000MoleFlowkmol/hr1156.779779.2571185.585750.451MassFlowkg/hr106586.33748930.765108103.9647413.142VolumeFlowcum/hr125.93549.068135.78343.501EnthalpyGcal/hr4.218-82.0052.022-79.808MassFlowkg/hrCO0000O20000NO0000CH3OH0000MN0000DMO0.406155.778155.6910.492MG0.3965.6955.8060.2851,2-BDO0471.995471.3650.63EG046447.8742271.67844176.196C3H8O-0101849.423281.6931567.729JBEN106585.5340104917.7261667.809MassFracCO0000O20000NO0000CH3OH0000MN0000DMO00.0030.0010MG00001,2-BDO00.010.0040EG00.9490.0210.932C3H8O-0100.0380.0030.033JBEN100.9710.0351.7.4甲苯回收塔（T0504)表1.23甲苯回收塔進出料流股表流股信息INOUT123TemperatureC102.2110.445.3Pressurebar10.180.1VaporFrac000MoleFlowkmol/hr1185.58554.8931130.693MassFlowkg/hr108103.963921.253104182.707VolumeFlowcum/hr135.7834.048123.171EnthalpyGcal/hr2.022-5.1124.154MassFlowkg/hrCO000O2000NO000CH3OH000MN000DMO155.691155.2810.41MG5.8065.4060.41,2-BDO471.365471.3650EG2271.6782271.6780C3H8O-01281.693281.6930JBEN104917.726735.829104181.897MassFracCO000O2000NO000CH3OH000MN000DMO0.0010.040MG00.00101,2-BDO0.0040.120EG0.0210.5790C3H8O-010.0030.0720JBEN0.9710.18811.7.5乙二醇精制塔（T0505）表1.24乙二醇精制塔進出料流股表流股信息INOUT1234TemperatureC142.022678132.689232136.80510561.1702537PressurebarVaporFrac0000MoleFlowkmol/hr753.168082691.8618.530728942.7773535MassFlowkg/hr47588.450642950.96751307.479243330VolumeFlowcum/hr47.878389242.25612111.303099213.65066376EnthalpyGcal/hr-77.11417-72.963888-2.0864204-2.581386MassFlowkg/hrCH3OH3.40E-052.10E-408.65E-523.40E-05MN0000DMO4.197893447.21E-102.17E-144.19789343DMC1.15E-058.42E-334.98E-421.15E-05MG0.357404184.31E-141.77E-190.35740418ET3.51E-083.41E-489.36E-613.51E-081,2-BDO0.307538730.302322520.005200241.60E-05H20000N20000H2O64.3290531.10E-241.49E-3364.329053EG43883.473242906.1697928.52439148.7845862C3H8O-011581.669444.49324710.022756841537.15343JBEN1675.177589.09E-201.10E-271675.17758CACL20000DEG378.9385260.0022513378.926893.65E-26MassFracCH3OH7.15E-104.88E-456.61E-551.02E-08MN0000DMO8.82E-051.68E-141.66E-170.00126062DMC2.42E-101.96E-373.81E-453.46E-09MG7.51E-061.00E-181.35E-220.00010732ET7.38E-137.94E-537.16E-641.05E-111,2-BDO6.46E-067.04E-063.98E-064.82E-09H20000N20000H2O0.001351772.57E-291.14E-360.01931803EG0.922145450.9989570.710163780.01465002C3H8O-010.033236410.00103591.74E-050.46160764JBEN0.035201342.12E-248.42E-310.50305633CACL20000DEG0.007962825.24E-080.289814841.10E-291.7.6丙二醇精制塔（T0506）表1.25丙二醇精制塔進出料流股表流股信息INOUT123TemperatureC45.8138.845.5PressurebarVaporFrac000MoleFlowkmol/hr42.77720.98721.791MassFlowkg/hr33301587.8571742.143VolumeFlowcum/hr3.591.7472.017EnthalpyGcal/hr-2.581-2.334-0.184MassFlowkg/hrDMO4.1983.9080.29DMC000MG0.3570.3050.053ET0001,2-BDO000H2000N2000H2O64.3290.00164.328EG48.78548.7330.052C3H8O-011537.1531532.2814.872JBEN1675.1782.6291672.549MassFracDMO0.0010.0020DMC000MG000ET0001,2-BDO000H2000N2000H2O0.01900.037EG0.0150.0310C3H8O-010.4620.9650.003JBEN0.5030.0020.96附錄二能量衡算一覽表2.1合成氣分離工段能量衡算2.1.1閃蒸罐（V0101）表2.1閃蒸罐負荷計算表HeatingDutyHeatduty/Gcal/hr0.0764Q=0.0764Gcal/hr表2.2閃蒸罐焓變計算表流股信息INOUT123TemperatureC-180-180-180Pressurebar343030VaporFrac0.70201MoleFlowkmol/hr6763.7751954.6374809.138MassFlowkg/hr76052.02148717.38527334.637VolumeFlowcum/hr1084.24572.4521161.771EnthalpyGcal/hr-76.988-52.112-24.8∑HGcal/hr-76.988-76.912表2.3閃蒸罐能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-76.9880.07640.0000-76.912-0.00042.1.2甲烷洗滌塔（T0101)表2.4甲烷洗滌塔負荷計算表CondenserReboilerHeatduty/Gcal/hr0.00000.0000Q=0.0000Gcal/hr表2.5甲烷洗滌塔焓變計算表流股信息INOUT1234TemperatureC-180.000-180.000-170.800-176.300Pressurebar30.00030.00030.00029.400VaporFrac1.0000.0000.0001.000MoleFlowkmol/hr4809.1383087.0003798.3624097.776MassFlowkg/hr27334.63749526.58367641.4279219.793VolumeFlowcum/hr1161.771109.710139.7221106.095EnthalpyGcal/hr-24.800-66.632-84.597-6.834表2.6甲烷洗滌塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-91.4320.00000.0000-91.43202.1.3氣提塔(T0102)表2.7氣提塔負荷計算表CondenserReboilerHeatduty/Gcal/hr0.00004.551Q=4.551Gcal/hr表2.8氣提塔焓變計算表流股信息INOUT1234TemperatureC-180.000-170.800-159.200-124.000Pressurebar30.00030.00029.40030.000VaporFrac0.0000.0001.0000.000MoleFlowkmol/hr1954.6373798.362224.9425528.057MassFlowkg/hr48717.38567641.4271651.224114707.655VolumeFlowcum/hr72.452139.72268.454302.738EnthalpyGcal/hr-52.112-84.597-1.549-130.609表2.9氣提塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-136.7094.5510.0000-132.1581.59872E-142.1.4甲烷回收塔（T0103)表2.10甲烷回收塔負荷計算表CondenserReboilerHeatduty/Gcal/hr-2.7592.032Q=-0.727Gcal/hr表2.11甲烷回收塔焓變計算表流股信息INOUT123TemperatureC-124.000-147.300-182.100Pressurebar30.0002.8002.600VaporFrac0.0000.0001.000MoleFlowkmol/hr5528.0573352.7662175.290MassFlowkg/hr114707.65553790.43060917.224VolumeFlowcum/hr302.738135.7475846.057EnthalpyGcal/hr-130.609-70.871-60.465表2.12甲烷回收塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-130.609-0.7270.0000-131.33602.2酯化再生工段能量衡算2.2.1酯化塔（T0201)表2.13酯化塔負荷計算表CondenserReboilerHeatduty/Gcal/hr-46.37532.329Q=-14.046Gcal/hr表2.14酯化塔焓變計算表流股信息INOUT1234TemperatureC53.10027.100114.20033.900Pressurebar5.0005.0005.0005.000VaporFrac0.0000.9840.0001.000MoleFlowkmol/hr6892.46214898.8106146.75214400.000MassFlowkg/hr220870.510437112.748185333.760472649.498VolumeFlowcum/hr291.13972849.091269.10672946.395EnthalpyGcal/hr-387.907-58.027-345.214-114.765表2.15酯化塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-445.934-14.0460.0000-459.9790.0012.2.2甲醇雙效精餾高壓塔（T0202)表2.16甲醇雙效精餾高壓塔負荷計算表CondenserReboilerHeatduty/Gcal/hr048.196Q=48.196Gcal/hr表2.17甲醇雙效精餾高壓塔焓變計算表流股信息INOUT12（液相回流）34（氣相采出）TemperatureC114.200123.400130.200123.400Pressurebar7.5007.0007.2527.000VaporFrac0.0000.0000.0001.000MoleFlowkmol/hr6146.7523398.4303255.9526289.230MassFlowkg/hr185333.760108830.07292759.845201403.988VolumeFlowcum/hr269.155164.463136.50827734.256EnthalpyGcal/hr-345.194-184.683-185.919-295.762∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-529.87748.1960.0000-481.6810表2.18甲醇雙效精餾高壓塔能量平衡表2.2.3甲醇雙效精餾低壓塔（T0203)表2.19甲醇雙效精餾低壓塔負荷計算表CondenserReboilerHeatduty/Gcal/hr-51.4260Q=-51.426Gcal/hr表2.20甲醇雙效精餾低壓塔焓變計算表流股信息INOUT1234TemperatureC130.200100.50064.20099.700Pressurebar7.2521.2181.0001.218VaporFrac0.0000.0380.0000.000MoleFlowkmol/hr3255.952122986.8092399.873123843.489MassFlowkg/hr92759.8452278540.00076899.3642294410.000VolumeFlowcum/hr136.508120496.540103.2972546.999EnthalpyGcal/hr-185.919-8135.075-134.382-8238.079∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-8320.994-51.4260.0000-8372.461-3.52172E-12表2.21甲醇雙效精餾低壓塔能量衡算表2.3羰化偶聯工段能量衡算2.3.1羰化反應器（R0301)表2.22羰化反應器負荷計算表HeatingDutyHeatduty/Gcal/hr-27.864Q=-27.864Gcal/hr表2.23羰化反應器焓變計算表流股信息IN-REACREAC-OUTTemperatureC130.000130.000Pressurebar55VaporFrac1.0001.000MoleFlowkmol/hr15999.43515195.290MassFlowkg/hr517254.210517254.210VolumeFlowcum/hr107021.764101547.139EnthalpyGcal/hr-144.607-172.471表2.24羰化反應器能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr誤差-144.607-27.8640.0000-172.47102.3.2閃蒸罐（V0301)表2.25閃蒸罐負荷計算表HeatingDutyHeatduty/Gcal/hr4.316Q=4.316Gcal/hr表2.26閃蒸罐焓變計算表流股信息INOUT1.0002.0003.000TemperatureC80.00080.00080.000Pressurebar5.0001.5001.500VaporFrac0.9481.0000.000Mole