附录1物料衡算

中煤榆林能化公司年产30万吨烯烃联产3万吨甲硫醇含硫尾气资源化利用项目- 21 -目录1.1总述- 2 -1.2物料衡算的意义- 2 -1.3物料衡算的原则：- 3 -1.4物料衡算任务：- 4 -1.5物料衡算- 6 -1.5.1原料预处理工段物料衡算- 6 -1.5.2甲醇合成工段物料衡算- 10 -1.5.3甲醇精制工段- 13 -1.5.4甲硫醇合成工段- 16 -1.5.5烯烃合成工段- 18 -物料衡算1.1总述本项目是利用榆横工业园区煤化工企业生产过程中大量排放的含硫尾气克劳斯尾气为原料，经过原料预处理工段、甲醇合成工段、甲醇精制工段、烯烃合成工段、甲硫醇合成工段，每年可产30万吨烯烃联产3万吨甲硫醇与总厂形成有效融合体系，送至总厂聚合车间生产聚烯烃，提高产品经济附加值。1.2物料衡算的意义物料衡算是质量守恒定律的一种表现形式。凡引入某一设备的物料成分、质量或体积比等于操作后所得产物的成分、质量或体积加上物料损失。通过对整个生产系统、生产工段、以及各个重要的生产单元进行详细的物料衡算，计算得到各个产品的实际产量与规格，各个原料的实际消耗定额，“三废”的排放量及组成，从而定量的评述初步设计阶段所采用的生产工艺是否合理，先进，并通过衡算所得数据，来进一步对各个阶段所采用的设备进行初步设计。1.3物料衡算的原则：物料平衡是指在单位时间内进入系统的全部物料质量必定等于离开该系统的全部物料质量再加上损失掉的和积累起来的物料质量。进行物料衡算时，先必须确定衡算的体系。（1）对一般的体系而言，物料分布均可表示为：(物料的累积率)=(物料进入率)-(物料流出率)+(反应生成率)-(反应消耗率)（2）当系统没有化学反应时，则可简化为：(物料的累积率)=(物料进入率)-(物料流出率)（3）在稳定状态下有：(物料进入率)=(物料流出率)利用上述关系，可以对整个工艺系统或子系统进行物料衡算。物料衡算包括总质量衡算、组分衡算和元素衡算。各种衡算方法的适用情况如下表所示：表1-1 物料衡算式适用范围类别物料衡算形式无化学反应有化学反应总衡算式总物料衡算式适用适用总物质的量衡算式适用不适用组分衡算式组分质量衡算式适用不适用组分物质的量衡算式适用不适用元素原子衡算式元素原子质量衡算式适用适用元素原子物质的量衡算式适用适用由于系统中存在化学反应，我们主要采用总质量衡算的衡算方法，同时列出每种物料组分的质量流量便于查找和计算。1.4物料衡算任务：对于本厂，工艺采取年开工300天（7200小时）的连续操作，其中一年内的四五周（约30天）用于固定的停车设备检修及紧急情况处理。物料衡算的主要任务在于：（1）确定烯烃、甲硫醇的实际产量以及质量指标；（2）确定二氧化碳、硫化氢、氢气等原料的循环量以及损失率等指标；（3）确定工艺中的“三废”排放量等公共经济指标；（4）各主要单元过程的物料衡算，并指导工艺设备的尺寸确定；（5）汇总全流程物料衡算，数据用于完成物料流程图等后续设计任务。1.5物料衡算1.5.1原料预处理工段物料衡算图1-1原料预处理工段流程模拟表1-2原料预处理工段物料衡算表流入物流物流信息S0101S0102S0112S0116Temperature 1772002520Pressure bar1616455Vapor Frac1100Mole Flow kmol/hr25000150127407029.0273Mass Flow kg/hr680318.444302.382398746.495220000Volume Flow cum/hr58479.6195368.805491390.320262214.232697Enthalpy Gcal/hr-775.985860.18260659-937.04724-518.10259CO2159535.525000H20302.38200H2S3237.7786000N2371178.61000CH3OH0000MDEA00199373.248110000CH40000C2H40000C3H60000C4H80000H2O143996.1330199373.248110000CO0000SO22370.3976000CH3SH0000C2H6S0000总和1299367流出物流信息S105S108S112S114S120S121S111S115Temperature C4040115.76768520.22402404025.23217115.7677Pressure bar111.551.51.5451.5Vapor Frac01010110Mole Flow kmol/hr8066.92613470.49665.70873325.9725430.7195188.04863068.5829665.709Mass Flow kg/hr145327.9379236.6305419.84814215.277781.8457047.235134918.7305419.8Volume Flow cum/hr148.3895350719.7332.4237931543.4577.94533264.0631193.141332.4238Enthalpy Gcal/hr-548.403-15.6267-695.58227-29.876-29.2908-6.62773-289.966-695.582CO207976.7765.83E-2013904.0402829.034134825.75.83E-20H2078.84308000000H2S004.36E-13276.372104218.2012.9738444.36E-13N20371178.6000000CH4O00000000MDEA00154672.9950.04045126.286800.92972154673C100000000C200000000C300000000C400000000H2O145327.90150746.85234.816227755.559089.16798150746.9CO00000000SO202.370398000000CH4S00000000C2H6S-200000000总和1299367由上表1-2可以看出，原料预处理工段进、出物料的总体质量保持平衡。1.5.2甲醇合成工段物料衡算图1-2甲醇合成工段流程模拟表1-3甲醇合成工段物料衡算表流入物流流出物流物流信息S0113S0201S0202S0212S0214Temperature 25.232173625104.441871103.31565014Pressure bar45161.54848Vapor Frac11110.00011548Mole Flow kmol/hr3068.582254445.52859309.38405849784.20529910.94607Mass Flow kg/hr134918.749195646.8247414.54045199934.114251735.451Volume Flow cum/hr1193.140526887.56166475.2503824417.1046278.006109Enthalpy Gcal/hr-289.96604-417.82745-15.564801-216.28046-620.90603CO2134825.678195646.8241554.77775721.5956811953.0862H20046913.982934.364712274.7086014H2S2.9738441800.042849610.044406250.69873472N200000CH3OH0039.35871173907.62108129357.819MDEA0.9297203602.8034e-160.007802030.92972033CH400000C2H400000C3H600000C4H800000H2O89.16797806.940964285230.7013897764.0379CO001269.1019716.6110072325.728788SO200000CH3SH00000C2H6S00000总和451669.5451669.5由上表1-3可以看出，甲醇合成工段进、出物料的总体质量保持平衡。1.5.3甲醇精制工段图1-3甲醇精制工段流程模拟表1-4甲醇精制物料衡算表流入物流流出物流物流信息S0214S0315S0216S0225S0301S0401Temperature 3.3156501420-25.23936299.647730564.256686264.2566862Pressure bar480.51111Vapor Frac0.000115480100.073849100.07384910Mole Flow kmol/hr9910.94607129.091561777.1172825336.144031303796.77632Mass Flow kg/hr251735.4512461.4818532437.008496133.46334158.9942121467.467Volume Flow cum/hr278.0061092.5484868816018.0258104.645211274.4928338016.82992Enthalpy Gcal/hr-654.96706-8.7719648-68.807388-357.01888-7.2007792-210.30575CO231757.2816031757.280503.5244e-050.00102933H269.275136069.275136000H2S1.5134485901.5133855202.0881e-066.0984e-05N2000000CH3OH125208.62308.847767142.9143011.244220954150.61335121222.696MDEA0.9297203603.8355e-180.929720369.1915e-312.6845e-29CH4000000C2H4000000C3H6000000C4H8000000H2O94232.552151.701460.7441377696131.28868.34995992243.868693CO465.2809560465.280956000SO2000000CH3SH00.0376589103.2024e-090.001246730.03641217C2H6S00.8949566200.000729470.029604310.86462283总和254196.9329254196.9329由上表1-4可以看出，甲醇精制工段进、出物料的总体质量保持平衡。1.5.4甲硫醇合成工段图1-4甲硫醇合成工段流程模拟表1-5甲硫醇合成工段物料衡算流入物流流出物流物流信息S0128S0301S0308S0315S0319S0321Temperature 4064.2566862-24.395015202525Pressure bar1.5160.531Vapor Frac10.073849101000Mole Flow kmol/hr188.04859713075.8372918129.091561107.541825.57792493Mass Flow kg/hr7047.235454158.99423247.8352461.481855167.62015329.292643Volume Flow cum/hr3264.06285274.492833261.4150672.548486885.993965330.38408783Enthalpy Gcal/hr-6.6277265-7.2007792-6.1318313-8.7719648-1.2158991-0.1080496CO22829.034273.5244e-052829.03431000H2000000H2S4218.201172.0881e-06333.15029907.3097e-060N2000000CH3OH04150.613350.01031858308.84776714.50002288.69095175MDEA09.1915e-310000CH4000000C2H4000000C3H6000000C4H8000000H2O08.349959925.7087e-092151.701462.1442e-203.58568018CO000000SO2000000CH3SH00.0012467385.62308650.037658915147.861241.20512482C2H6S00.029604310.016988830.894956625.25887331315.810886总和11206.2296511206.22965由上表1-5可以看出，甲硫醇精制工段进、出物料的总体质量保持平衡。1.5.5烯烃合成工段图1-5烯烃合成工段流程模拟表1-6烯烃合成工段物料衡算流入物流流出物流物流信息S0401S0409S0410S0414S0424S0427S0428Temperature 64.256686245.0378725151.77340328.630756-47.1737-58.548093-98.437222Pressure bar15589.152432368.043346368Vapor Frac0.07384910100001Mole Flow kmol/hr3796.7763271.2926063761.6432740.82124726.8812615596.64362466.293736Mass Flow kg/hr121467.4673983.1793267837.541331174.03931049.7213216736.3307686.657218Volume Flow cum/hr8016.82992377.21188478.851382852.16621471.2249015834.1974469117.326014E