年产35万吨乙二醇项目初步设计附录

XX35万吨/年乙二醇项目附录XX35万吨/年乙二醇项目附录2015年8月12日目录附录一物料衡算一览表 11.1物料衡算 11.1.1物料衡算的意义 11.1.2物料衡算的任务 11.1.3物料衡算遵循的原则 11.1.4系统物料衡算 21.1.5物耗一览表 21.2能量衡算 31.2.1能量衡算的目的 31.2.2能量衡算可以解决的问题 31.2.3能量衡算遵循的原则 41.2.4系统能量衡算 41.3合成气分离工段 51.3.1闪蒸罐 51.3.2甲烷洗涤塔 61.3.3气提塔 61.3.4脱甲烷塔 71.4酯化再生工段 81.4.1反应精馏塔（T0201） 81.4.2甲醇双效精馏高压塔（T0202) 91.4.3甲醇双效精馏低压塔（T0203) 101.5羰化偶联工段 121.5.1羰化偶联反应器(R0301) 121.5.2闪蒸罐(V0301) 131.5.3甲醇洗涤塔（T0301) 141.5.4草酸二甲酯回收塔（T0302） 151.5.5常压恒沸精馏塔(T0303) 161.5.6加压恒沸精馏塔(T0304) 171.6催化加氢工段 191.6.1加氢反应器（R0401) 191.6.2高压分离罐（V0401） 201.6.3低压分离罐(V0402) 221.7精制工段 231.7.1粗产品预分离塔（T0501) 231.7.2脱甲醇塔（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附录二能量衡算一览表 332.1合成气分离工段能量衡算 332.1.1闪蒸罐（V0101） 332.1.2甲烷洗涤塔（T0101) 332.1.3气提塔(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甲醇双效精馏高压塔（T0202) 362.2.3甲醇双效精馏低压塔（T0203) 372.3羰化偶联工段能量衡算 382.3.1羰化反应器（R0301) 382.3.2闪蒸罐（V0301) 392.3.3甲醇洗涤塔（T0301) 392.3.4草酸二甲酯回收塔（T0302） 402.3.5常压恒沸精馏塔(T0303) 412.3.6高压压恒沸精馏塔(T0304) 412.4催化加氢工段能量衡算 422.4.1加氢反应器（R0401) 422.4.2高压分离罐（V0401) 432.4.3低压分离罐（V0402) 432.4.4氢气压缩机（C0402) 442.5精制工段能量衡算 452.5.1粗产品预分离塔（T0501) 452.5.2脱甲醇塔（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附录三设备一览表 493.1塔设备一览表 493.2气液分离器一览表 523.3储罐一览表 533.4压缩机一览表 583.5泵一览表 593.6反应器一览表 623.7换热器一览表 633.8管道一览表 67附录四MSDS数据一览表 774.1乙二醇 774.2碳酸二甲酯 804.3甲醇 844.4合成气 884.5亚硝酸甲酯 914.6草酸二甲酯 95附录一物料衡算一览表1.1物料衡算1.1.1物料衡算的意义物料衡算是确定化工生产过程中物料比例和物料转变的定量关系的过程，是化工工艺计算中最基本、最重要的内容之一。在化学工程中，设计或改造工艺流程和设备，了解和控制生产操作过程，核算生产过程的经济效益，确定主副产品的产率，确定原材料消耗定额，确定生产过程的损耗量，便于技术人员对现有的工艺过程进行分析，选择最有效的工艺路线，确定设备容量、数量和主要尺寸，对设备进行最佳设计以及确定最佳操作条件等都要进行物料核算。毫不夸张的说，一切化学工程的开发和放大都是以物料衡算为基础的。1.1.2物料衡算的任务通常物料衡算有两种情况，一是对已有的生产设备或过程利用实测的数据，计算出另一些不能直接测定的物料量，俗称生产查定，用此计算结果，对生产进行分析，作出判断，提出改进措施。二是设计一种新的设备或过程，由物料衡算求出进出各设备的物料量、组成等，然后结合能量衡算，确定设备的工艺尺寸及整个工艺过程。1.1.3物料衡算遵循的原则物料衡算的理论基础是质量守恒定理。它是研究某一体系内进出物料量及组成的变化。进行物料衡算时，必须先确定衡算的体系。对一般体系，均可用如下表示：系统中的积累=输入-输出+生成-消耗在稳定状态下有：输入=输出-生成+消耗特别地，当系统没有化学反应时，则可简化为：输入=输出1.1.4系统物料衡算详见附录一，物料衡算一览表。1.1.5物耗一览表表1.1项目综合物耗计算表序号名称需要量单价（元/吨）总费用（万元/年）1合成气108198.36万Nm3/年0.6元/Nm3649192甲醇3.9万吨/年23269071.43一氧化氮1424000Nm3/年0.8元/m3113.924氧气75289584Nm3/年//5氮气4077832Nm3/年//6甲苯2.75万吨/年443012182.397催化剂0.02192万吨/年32179.5643.59总计86930.32表1.2万吨产品的物耗序号名称需要量单价（元/吨）费用（万元/万吨/年）1合成气3091.38万Nm3/万吨/年0.6元/Nm31854.8285712甲醇0.0866万吨/万吨/年2326201.433一氧化氮40685.7Nm3/万吨/年0.8元/m36004氧气2151130.97Nm3/万吨/年//5氮气116509.48Nm3/万吨/年//6甲苯0.07864430405.8867催化剂0.0219232179.518.388总计3080.534表1.3万元产值综合物耗序号名称需要量费用（万吨/万元/年）1合成气108198.36万Nm3/年0.0005391332甲醇3.9万吨/年0.004963一氧化氮1424000Nm3/年0.0016666674氧气75289584Nm3/年/5氮气4077832Nm3/年/6甲苯2.75万吨/年0.0024637467催化剂0.02192万吨/年0.054382448总计0.0003251.2能量衡算1.2.1能量衡算的目的对于新设计的生产车间，能量衡算的主要目的是确定设备的热负荷。根据设备的热负荷的大小、所处理物料的性质及工艺要求再选择传热面的形式、计算传热面积、确定设备的主要工艺尺寸。确定传热所需要的加热剂或冷却剂的用量及伴有热效应的温升情况。对于已投产的生产车间，进行能量衡算是为了更加合理能量利用，以最大限度降低单位产品的能耗。1.2.2能量衡算可以解决的问题在化工设计、化工生产中，通过能量衡算可以解决以下问题：1.确定物料输送机械（泵、压缩机等）和其他操作机械（搅拌、过滤、粉碎等）所需要的功率，以便于确定输送设备的大小、尺寸和型号；2.确定各单元操作过程（蒸发、蒸馏、冷凝、冷却等）所需要的热量或冷量，及其传递速率；计算换热设备的工艺尺寸；为其他专业如供汽、供冷、供水专业提供设计条件；3.化学反应常伴有热效应，导致体系的温度上升或下降，为此需确定为保持一定反应温度所需的移出或加入的热传递速率.4.为充分利用余热，提高能量利用率，降低能耗提供重要依据，使过程的总能耗降低到最低程度；5.最终确定总需求能量和能量的费用，并用来确定这个过程在经济上的可行性。1.2.3能量衡算遵循的原则根据能量守恒定律，任何均相体系在时间内的能量平衡关系，表述如下：热量衡算是能量衡算的一种，在能量衡算中占主要地位。热量衡算的理论依据是热力学第一定律。能量守恒表达式如下：即输入=输出+损失式中：输入设备热量的总和；：输出设备热量的总和；：损失热量的总和。对于连续系统：式中Q：设备的热负荷;W：输入系统的机械能;∑Hout：离开设备的各物料焓之和;∑Hin：进入设备的各物料焓之和。1.2.4系统能量衡算详见附录二，能量衡算一览表。1.3合成气分离工段1.3.1闪蒸罐表1.4闪蒸罐进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甲烷洗涤塔表1.5甲烷洗涤塔进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气提塔表1.6气提塔进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脱甲烷塔表1.7脱甲烷塔进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反应精馏塔（T0201）1.8反应精馏塔进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甲醇双效精馏高压塔（T0202)表1.9甲醇双效精馏高压塔进出料流股表流股信息INOUT12（液相回流）34（气相采出）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甲醇双效精馏低压塔（T0203)表1.10甲醇双效精馏低压塔进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羰化偶联工段1.5.1羰化偶联反应器(R0301)表1.11羰化偶联反应器进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闪蒸罐(V0301)表1.12闪蒸罐进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甲醇洗涤塔（T0301)表1.13甲醇洗涤塔进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草酸二甲酯回收塔进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常压恒沸精馏塔(T0303)表1.15常压恒沸精馏塔进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加压恒沸精馏塔(T0304)表1.16加压恒沸精馏塔进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催化加氢工段1.6.1加氢反应器（R0401)表1.17加氢反应器进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高压分离罐（V0401）表1.18高压分离罐进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低压分离罐(V0402)表1.19低压分离罐进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粗产品预分离塔（T0501)表1.20粗产品预分离塔进出料流股表流股信息INOUT12（侧线）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脱甲醇塔（T0502)表1.21脱甲醇塔进出料流股表流股信息INOUT1234(侧线）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萃取塔进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甲苯回收塔进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乙二醇精制塔进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丙二醇精制塔进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附录二能量衡算一览表2.1合成气分离工段能量衡算2.1.1闪蒸罐（V0101）表2.1闪蒸罐负荷计算表HeatingDutyHeatduty/Gcal/hr0.0764Q=0.0764Gcal/hr表2.2闪蒸罐焓变计算表流股信息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闪蒸罐能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr误差-76.9880.07640.0000-76.912-0.00042.1.2甲烷洗涤塔（T0101)表2.4甲烷洗涤塔负荷计算表CondenserReboilerHeatduty/Gcal/hr0.00000.0000Q=0.0000Gcal/hr表2.5甲烷洗涤塔焓变计算表流股信息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甲烷洗涤塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr误差-91.4320.00000.0000-91.43202.1.3气提塔(T0102)表2.7气提塔负荷计算表CondenserReboilerHeatduty/Gcal/hr0.00004.551Q=4.551Gcal/hr表2.8气提塔焓变计算表流股信息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气提塔能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr误差-136.7094.5510.0000-132.1581.59872E-142.1.4甲烷回收塔（T0103)表2.10甲烷回收塔负荷计算表CondenserReboilerHeatduty/Gcal/hr-2.7592.032Q=-0.727Gcal/hr表2.11甲烷回收塔焓变计算表流股信息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误差-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酯化塔负荷计算表CondenserReboilerHeatduty/Gcal/hr-46.37532.329Q=-14.046Gcal/hr表2.14酯化塔焓变计算表流股信息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误差-445.934-14.0460.0000-459.9790.0012.2.2甲醇双效精馏高压塔（T0202)表2.16甲醇双效精馏高压塔负荷计算表CondenserReboilerHeatduty/Gcal/hr048.196Q=48.196Gcal/hr表2.17甲醇双效精馏高压塔焓变计算表流股信息INOUT12（液相回流）34（气相采出）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误差-529.87748.1960.0000-481.6810表2.18甲醇双效精馏高压塔能量平衡表2.2.3甲醇双效精馏低压塔（T0203)表2.19甲醇双效精馏低压塔负荷计算表CondenserReboilerHeatduty/Gcal/hr-51.4260Q=-51.426Gcal/hr表2.20甲醇双效精馏低压塔焓变计算表流股信息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误差-8320.994-51.4260.0000-8372.461-3.52172E-12表2.21甲醇双效精馏低压塔能量衡算表2.3羰化偶联工段能量衡算2.3.1羰化反应器（R0301)表2.22羰化反应器负荷计算表HeatingDutyHeatduty/Gcal/hr-27.864Q=-27.864Gcal/hr表2.23羰化反应器焓变计算表流股信息IN-REACREAC-OUTTemperatureC130.000130.000Pressurebar55VaporFrac1.0001.000MoleFlowkmol/hr15999.43515195.290MassFlowkg/hr517254.210517254.210VolumeFlowcum/hr107021.764101547.139EnthalpyGcal/hr-144.607-172.471表2.24羰化反应器能量平衡表∑HinGcal/hr∑QGcal/hr∑WGcal/hr∑HoutGcal/hr误差-144.607-27.8640.0000-172.47102.3.2闪蒸罐（V0301)表2.25闪蒸罐负荷计算表HeatingDutyHeatduty/Gcal/hr4.316Q=4.316Gcal/hr表2.26闪蒸罐焓变计算表流股信息INOUT1.0002.0003.000TemperatureC80.00080.00080.000Pressurebar5.0001.5001.500VaporFrac0.9481.0000.000Mole