年產30萬噸合成甲醇分廠設計書(編輯修改稿)

　

【文章內容簡介】 0CH3OCH30CH3CH2OH0C2H4O20Mass FracCOCO2H2N2CH4CH3OH0H2O0CH3OCH300CH3CH2OH00C2H4O200Mole Flow kmol/hrCOCO2H2N2CH4CH3OH0H2O0CH3OCH30CH3CH2OH0C2H4O20Mole FracCOCO2H2N2CH4CH3OH0H2O0CH3OCH300CH3CH2OH00C2H4O200表31 甲醇反應器物料流股衡算表分離器的物料衡算圖33 分離器物料流股圖項目進料塔頂出料塔底出料Temperature C 404040Pressure bar Vapor Frac 1Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy Gcal/hr Mass Flow kg/hr CO CO2 H2 N2 CH4 CH3OH 0 H2O 0 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0Mass Frac CO CO2 H2 N2 CH4 CH3OH 0 H2O 0 CH3OCH3 00 CH3CH2OH 00 C2H4O2 00Mole Flow kmol/hr CO CO2 H2 N2 CH4 CH3OH 0 H2O 0 CH3OCH3 0 CH3CH2OH 0 C2H4O2 0Mole Frac CO CO2 H2 N2 CH4 CH3OH 0 H2O 0 CH3OCH3 00 CH3CH2OH 00 C2H4O2 00表32 分離器物料流股衡算表第一精餾塔的物料衡算圖34 第一精餾塔物料流股圖項目進料塔頂出料塔底出料Temperature C 65Pressure bar 1023Vapor Frac 010Mole Flow kmol/hr Mass Flow kg/hr Volume Flow cum/hr Enthalpy Gcal/hr Mass Flow kg/hr CO 0 CO2 0 H2 0 N2 0 CH4 0 CH3OH H2O 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