附录1-能量衡算一览表

2017年“东华科技-陕鼓杯”第十一届全国大学生化工设计竞赛云天化合成氨装置废气深度脱硫资源化利用项目能量衡算一览表团队名称： 碣石观沧海团队 团队成员：叶阳 曾伟 邵青楠 崔怡洲 王奥诚指导老师： 黄星亮 邓春 孟祥海 杜巍 徐建 2017年8月云天化合成氨装置废气深度脱硫资源化利用项目目 录目 录.1第一章 总论2第二章 热量衡算原理3第三章 热量衡算任务4第四章 热量衡算54.1 硫化氢提浓工段54.1.1 R0101羰基硫水解反应器64.1.2 C0101压缩机64.1.3 T0101 硫化氢吸收塔74.1.4 T0102 MDEA再生塔74.1.5 T0103硫化氢吸收塔84.1.6 T0104 MDEA再生塔94.1.7 T0105硫化氢吸收塔94.1.8 T0106 MDEA再生塔104.2 甲硫醇合成工段114.2.1 R0201甲硫醇合成反应器114.3 产品分离工段134.3.1 V0301气液分离罐134.3.2 V0302气液分离罐144.3.3 T0301甲醇洗涤塔154.3.4 T0302硫化氢汽提塔154.3.5 T0303萃取精馏塔164.3.6 T0304产品精馏塔174.3.7 T0305甲醇-水精馏塔174.3.8 T0306甲醇-水精馏塔184.4 食品级二氧化碳生产工段194.4.1 C0401压缩机194.4.2 V0401气液分离罐204.4.3 T0401二氧化碳精馏塔204.5 总结21第一章 总论本项目以云南省云天化集团下属天安化工50万吨/年合成氨装置含硫化氢废气为原料，经硫化氢提浓工段后，硫化氢气体进入甲硫醇合成反应器，通过硫化氢汽提、萃取精馏等手段将甲硫醇产品分离出来，并且副产二甲硫醚。提浓工段塔顶含二氧化碳气体经过粗脱硫、精脱硫以及分子筛脱水后进入精馏塔产出食品级液态二氧化碳。在已确定化学生产工艺和流程后，对各工段各重要设备进行能量衡算，以确定各单元操作需要热量以及冷量，为后续设计工作中提高热量的利用率，降低能耗提供主要依据。第二章 热量衡算原理系统的热量衡算以能量守恒为理论基础，研究某一系统内各类型的能量的变化，即：输入系统的能量=输出系统的能量+系统积累的能量对于连续系统，有：Q+W=Hout-Hin注：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。本项目的能量衡算以单元设备为对象，计算由机械能转换、化学反应释放能量和单纯的物理变化带来的热量变化。第三章 热量衡算任务从废气入厂到产品输出，其工艺路线四个工段：硫化氢提浓工段、甲硫醇合成工段、产品分离工段，食品级二氧化碳生产工段。 在进行本厂的热量衡算中，主要通过定量计算完成下述基本任务： 确定工艺单元中物料输送机械（如泵）所需要的功率，以便于进行设备的设计和选型； 确定精馏等单元操作中所需要的热量或冷量以及传递速率，计算换热设备的尺寸，确定加热剂和冷却剂的消耗量，为后续设计中比如供汽、供冷、供水等专业提供设备条件； 确定为保持一定反应温度所需移除或者加入的热传递速率，指导反应器的设计和选型； 提高热量内部集成度，充分利用余热，提高能量利用率，降低能耗； 最终计算出总需求能量和能量的费用，并由此确定工艺过程在经济上的可行性。 第四章 热量衡算4.1 硫化氢提浓工段 图4-1 硫化氢提浓工段工艺流程图本工段主要有羰基硫水解反应器，三个吸收塔以及三个解吸塔，主要设备的热量衡算如下：4.1.1 R0101羰基硫水解反应器表4-1 热负荷表WQHeat Duty Gcal/hr0-1.0910-10表4-2 流股焓变计算表进出口inout物流编号S102S103Total Flow kmol/hr238.13238.13Total Flow kg/hr9253.989253.98Total Flow l/min46641.0146641.01Temperature 45.0045.00Pressure atm2.22.2Vapor Frac11Liquid Frac00Enthalpy Gcal/hr-13.65-13.65表4-3 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-1.09E-10-13.65-13.65-1.09E-104.1.2 C0101压缩机表4-4 热负荷表WQHeat Duty Gcal/hr0.370表4-5 流股焓变计算表进出口inout物流编号S103S104Total Flow kmol/hr238.13238.13Total Flow kg/hr9254.009254.00Total Flow l/min46818.1115841.17Temperature 46.17218.72Pressure atm2.210Vapor Frac11Liquid Frac00Enthalpy Gcal/hr-13.65-13.28表4-6 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0.370-13.65-13.28-6.1510-054.1.3 T0101 硫化氢吸收塔表4-7 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0000表4-8 流股焓变计算表进出口inout物流编号S105S116S106S107Total Flow kmol/hr238.13911.22121.59996.62Total Flow kg/hr9254.0034563.334883.6238933.80Total Flow l/min9541.29558.145797.99676.99Temperature 35.0040.0177.4679.99Pressure atm109.89.810Vapor Frac1010Liquid Frac0101Enthalpy Gcal/hr-13.69-69.50-9.50-73.68表4-9 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00-83.19-83.19-2.1610-034.1.4 T0102 MDEA再生塔表4-10 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-3.083.120.05表4-11 流股焓变计算表进出口inout物流编号S109S113S117Total Flow kmol/hr1025.34907.69120.07Total Flow kg/hr38933.7734499.814433.90Total Flow l/min64734.81589.7644182.87Temperature 90.00112.7025.00Pressure atm1.31.31.1Vapor Frac0.1601Liquid Frac0.8410Enthalpy Gcal/hr-71.79-67.40-4.34表4-12 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00.05-71.79-71.74-7.4110-054.1.5 T0103硫化氢吸收塔表4-13 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0000表4-14 流股焓变计算表进出口inout物流编号S119S130S120S121Total Flow kmol/hr120.071049.2426.001127.77Total Flow kg/hr4433.9039254.661080.1642608.47Total Flow l/min22622.67634.165972.35744.97Temperature 35.0040.0065.4367.65Pressure atm2.2222.2Vapor Frac1010Liquid Frac0101Enthalpy Gcal/hr-4.34-79.82-2.34-81.81表4-15 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00-84.16-84.161.0110-034.1.6 T0104 MDEA再生塔表4-16 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-3.994.380.39表4-17 流股焓变计算表进出口inout物流编号S123S127S131Total Flow kmol/hr1141.671047.5295.80Total Flow kg/hr42608.4639223.803384.57Total Flow l/min45806.69670.2835235.03Temperature 90.00112.5325.00Pressure atm1.31.31.1Vapor Frac0.101Liquid Frac0.910Enthalpy Gcal/hr-80.06-77.58-2.09表4-18 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00.39-80.06-79.67-1.9710-034.1.7 T0105硫化氢吸收塔表4-19 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0000表4-20 流股焓变计算表进出口inout物流编号S134S135S136S137Total Flow kmol/hr120.401179.4018.871273.36Total Flow kg/hr4301.3243310.25771.6246840.03Total Flow l/min29522.98697.605755.13830.31Temperature 35.0040.0063.4864.23Pressure atm1.71.51.51.7Vapor Frac1010Liquid Frac0101Enthalpy Gcal/hr-2.95-89.42-1.67-90.69表4-21 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00-92.36-92.361.2610-034.1.8 T0106 MDEA再生塔表4-22 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-2.192.650.46表4-23 流股焓变计算表进出口inout物流编号S139S144S145Total Flow kmol/hr1280.09102.661178.28Total Flow kg/hr46840.023531.0143308.94Total Flow l/min47653.9037748.17739.33Temperature 90.0025.00112.35Pressure atm1.31.11.3Vapor Frac0.110Liquid Frac0.901Enthalpy Gcal/hr-88.80-1.37-86.98表4-24 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00.46-88.80-88.34-1.3810-034.2 甲硫醇合成工段图4-2 甲硫醇合成工段工艺流程图本工段主要有甲硫醇合成反应器，主要设备的热量衡算如下：4.2.1 R0201甲硫醇合成反应器表4-25 热负荷表WQHeat Duty Gcal/hr0-9.6610-01表4-26 流股焓变计算表进出口inout物流编号S204S205Total Flow kmol/hr377.10377.10Total Flow kg/hr13051.6013051.60Total Flow l/min14834.1514746.57Temperature 450450Pressure atm2525Vapor Frac11Liquid Frac00Enthalpy Gcal/hr-11.02-11.98表4-27 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-0.97-11.02-11.981.9210-044.3 产品分离工段图4.3 产品分离工段工艺流程图本工段主要由两个气液分离罐、甲醇洗涤塔、硫化氢汽提塔、萃取精馏塔、产品精馏塔以及两个甲醇双效精馏塔组成，主要设备的热量衡算如下：4.3.1 V0301气液分离罐表4-28 热负荷表WQHeat Duty Gcal/hr0-0.38表4-29 流股焓变计算表进出口inout物流编号S207S301S303Total Flow kmol/hr377.10207.08170.02Total Flow kg/hr13051.608106.194945.42Total Flow l/min18970.6214840.5698.53Temperature 656565Pressure atm6.26.26.2Vapor Frac0.710Liquid Frac0.301Enthalpy Gcal/hr-14.75-6.30-8.83表4-30 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-0.38-14.75-15.131.1410-044.3.2 V0302气液分离罐表4-31 热负荷表WQHeat Duty Gcal/hr0-8.7710-14表4-32 流股焓变计算表进出口inout物流编号S302S304S305Total Flow kmol/hr207.08176.7030.38Total Flow kg/hr8106.196882.271223.92Total Flow l/min10862.5210838.7523.76Temperature 202020Pressure atm6.26.26.2Vapor Frac0.8510Liquid Frac0.1501Enthalpy Gcal/hr-6.62-5.64-0.98表4-33 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-8.7710-14-6.62-6.627.2010-054.3.3 T0301甲醇洗涤塔表4-34 热负荷表WCondenserReboilerQHeat Duty Gcal/hr000-0.11表4-35 流股焓变计算表进出口inout物流编号S309S311S312S314Total Flow kmol/hr202.1880.00164.05118.13Total Flow kg/hr7870.162563.376111.654321.88Total Flow l/min12142.8353.6311291.7488.63Temperature 15.0015.0030.5028.11Pressure atm65.85.86Vapor Frac0.96010Liquid Frac0.04101Enthalpy Gcal/hr-6.05-4.59-5.79-4.97表4-36 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-0.11-10.65-10.761.8010-04注：甲醇洗涤塔存在盘管取热，所以有热量损失。4.3.4 T0302硫化氢汽提塔表4-37 热负荷表WCondenserReboilerQHeat Duty Gcal/hr000.660.66表4-38 流股焓变计算表进出口inout物流编号S303S306S307S315Total Flow kmol/hr170.02148.5125.48293.05Total Flow kg/hr4945.425545.80987.899503.33Total Flow l/min98.53112.291807.12214.84Temperature 65.0026.5353.98111.78Pressure atm6.2666.2Vapor Frac0010Liquid Frac1101Enthalpy Gcal/hr-8.83-5.95-0.35-13.77表4-39 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00.66-14.78-14.111.9010-044.3.5 T0303萃取精馏塔表4-40 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-2.062.360.30表4-41 流股焓变计算表进出口inout物流编号S316S317S318Total Flow kmol/hr293.0575.41217.63Total Flow kg/hr9503.333864.595638.73Total Flow l/min3276.449139.49127.70Temperature 93.5854.44114.39Pressure atm3.73.53.7Vapor Frac0.0810Liquid Frac0.9201Enthalpy Gcal/hr-13.77-0.45-13.01表4-42 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError00.30-13.77-13.46-1.8110-044.3.6 T0304产品精馏塔表4-43 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-0.700.28-0.42表4-44 流股焓变计算表进出口inout物流编号S319CH3SHC2H6STotal Flow kmol/hr75.4158.6316.78Total Flow kg/hr3864.592823.991040.60Total Flow l/min9417.6556.1922.35Temperature 54.2539.9177.17Pressure atm3.43.23.4Vapor Frac100Liquid Frac011Enthalpy Gcal/hr-0.45-0.64-0.23表4-45 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-0.42-0.45-0.873.3410-074.3.7 T0305甲醇-水精馏塔表4-46 热负荷表WCondenserReboilerQHeat Duty Gcal/hr001.181.18表4-47 流股焓变计算表进出口inout物流编号S320S326S321S322Total Flow kmol/hr217.6382.61144.92155.32Total Flow kg/hr5638.732659.164665.203632.70Total Flow l/min127.7768.199462.8783.21Temperature 114.73127.49127.51150.52Pressure atm87.87.88Vapor Frac00 10Liquid Frac1101Enthalpy Gcal/hr-13.01-4.45-6.79-9.49表4-48 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError01.18-17.46-16.28-2.3510-044.3.8 T0306甲醇-水精馏塔表4-49 热负荷表WCondenserReboilerQHeat Duty Gcal/hr0-1.260-1.26表4-50 流股焓变计算表进出口inout物流编号S323S324S329S330Total Flow kmol/hr155.32106.13204.1057.35Total Flow kg/hr3632.701938.063727.041843.72Total Flow l/min11328.4544616.9965.8341.67Temperature 88.15104.83104.0364.53Pressure atm1.21.21.21Vapor Frac0.180.9800Liquid Frac0.820.0211Enthalpy Gcal/hr-9.49-6.07-13.61-3.21表4-51 热量平衡计算一览表W Gcal/hrQ Gcal/hrHin Gcal/hrHout Gcal/hrError0-1.26-15.55-16.82-1.4110-044.4 食品级二氧化碳生产工段图4-4 食品级二氧化碳生产工段工艺流程图本工段主要由赤泥粗脱硫塔、气液分离罐、氧化锌精脱硫塔、分子筛脱水塔以及二氧化碳精馏塔，主要设备的热量衡算如下：4.4.1 C0401压缩机表4-52 热负荷表WQHeat Duty Gcal/hr0.340表4-53 流股焓变计算表进出口inout物流编号S403S404Total Flow kmol/hr166.22166.23Total Flow kg/hr6727.626727.62Total Flow l/min48689.4512377.34Temperature 49.82265.18Pressure atm1.509.87Vapor Frac11Liquid Frac00Ent