【正文】 CH3OCH3 0 CH3CH2OH C2H4O2 Mass Frac CO 00 CO2 0 H2 00 N2 0 CH4 00 CH3OH H2O 0 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0Mole Flow kmol/hr CO 0 CO2 0 H2 0 N2 0 CH4 0 CH3OH H2O 0 CH3OCH3 0 CH3CH2OH 0 C2H4O2 Mole Frac CO 00 CO2 0 H2 0 N2 0 CH4 0 CH3OH H2O 0 CH3OCH3 00 CH3CH2OH 0 C2H4O2 0表33 第一精餾塔物料流股衡算表（4）第二精餾塔的物料衡算圖35 第二精餾塔物料流股圖項目進料塔頂出料塔底出料Temperature C 78Pressure bar 3Vapor Frac 000Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy Gcal/hr Mass Flow kg/hr CO 000 CO2 000 H2 000 N2 000 CH4 000 CH3OH H2O CH3OCH3 000 CH3CH2OH C2H4O2 0Mass Frac CO 000 CO2 000 H2 000 N2 000 CH4 000 CH3OH 1 H2O 0 CH3OCH3 000 CH3CH2OH 0 C2H4O2 000Mole Flow kmol/hr CO 000 CO2 000 H2 000 N2 000 CH4 000 CH3OH H2O CH3OCH3 000 CH3CH2OH C2H4O2 0Mole Frac CO 000 CO2 000 H2 000 N2 000 CH4 000 CH3OH 1 H2O 0 CH3OCH3 000 CH3CH2OH 0 C2H4O2 000表34 第二精餾塔物料流股衡算表（5）閃蒸罐的物料衡算圖36 閃蒸罐物料流股圖項目進料塔頂出料塔底出料Temperature C Pressure bar 201010Vapor Frac 10Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy Gcal/hr Mass Flow kg/hr CO CO2 H2 N2 CH4 CH3OH H2O CH3OCH3 CH3CH2OH C2H4O2 Mass Frac CO 0 CO2 H2 0 N2 CH4 0 CH3OH H2O CH3OCH3 CH3CH2OH 0 C2H4O2 Mole Flow kmol/hr CO CO2 H2 N2 CH4 CH3OH H2O CH3OCH3 CH3CH2OH C2H4O2 Mole Frac CO 0 CO2 H2 N2 CH4 CH3OH H2O 0 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0表35 閃蒸罐物料流股衡算表 熱量衡算 為了使生成保持在適宜的工藝條件下進行，必須掌握物料帶入或帶出體系的熱量，控制熱量的供給速率和放熱速率，并且熱量衡算可為提高熱量利用率，降低能耗提供依據(jù)。它的能量平衡方程為：其中，——表示輸入設(shè)備熱量的總和； ——表示輸出設(shè)備熱量的總和； ——表示損失熱量的總和。在進行全廠的能量衡算時，是以單元設(shè)備為基本單位，考慮由機械能轉(zhuǎn)換、化學(xué)反應(yīng)釋放和單純的物理變化帶來的熱量變化。（1）甲醇反應(yīng)器的熱量衡算 圖 37 甲醇反應(yīng)器模擬負荷圖Heat duty MMBtu/hr Q= MMBtu/hr表36甲醇反應(yīng)器負荷計算表項目進料出料Temperature CPressure barVapor Frac11Mole Flow kmol/hrMass Flow kg/hrVolume Flow cum/hrEnthalpy MMBtu/hr∑H MMBtu/hr表37 甲醇反應(yīng)器能量信息表Q總W總Error00 表38 能量平衡計算表 （單位：MMBtu/hr）（2）分離器的熱量衡算圖38 分離器模擬負荷圖Heat duty MMBtu/hr Q= MMBtu/hr表39甲醇反應(yīng)器負荷計算表項目進料塔頂出料塔底出料Temperature C404040Pressure barVapor Frac1Mole Flow kmol/hrMass Flow kg/hrVolume Flow cum/hrEnthalpy MMBtu/hr∑H MMBtu/hr表310 甲醇反應(yīng)器能量信息表Q總W總Error00