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序号名称符号单位计算公式或数值来源计算结果1煤质分析收到基碳Car%48.00收到基氢Har%3.49收到基氧Oar%7.01收到基氮Nar%0.72收到基硫Sar%1.73收到基灰分Aar%30.54收到基全水分Mar%12.00空气干燥基水分Mad%8.49干燥无灰基挥发份Vdaf%30.00收到基低位发热量Qnet.arkcal/kg19118.002耗煤量锅炉实际耗煤量（B-MCR）Bt/h33.90机械未完全燃烧热损失q4%3.00计算耗煤量（B-MCR）Bjt/h根据业主提供实际烟气量试算32.88303引风机出口烟气参数(1)引风机出口实际烟量Vjpym3/h301103.55Nm3/h204064.00引风机出口排烟温度tyin℃130.00引风机出口飞灰浓度mhmg/Nm31330.00引风机出口过剩空气系数alfa'干烟气，实际含氧量8.42％1.6300(2)引风机出口干烟气量（6％O2）VsgyNm3/h业主提供引风机出口SO2浓度mso2mg/Nm3干烟气，含氧量6％2771.004年运行小时数Hh6800.005多年平均气压Pmbar1012.806脱硫及吸收塔相关参数要求脱硫率η%90.00吸收塔进口烟温tpy℃133.00吸收塔出口烟温tck℃50.00吸收塔出口要求含尘浓度mckmg/Nm3300.00吸收塔出口要求含SO2浓度mckmg/Nm3400.007摩尔分子量1摩尔CaCO3分子质量M1g/mol1001摩尔SO2分子质量M2g/mol641摩尔CaSO4.2H2O分子质量M10g/mol1728石灰石资料钙硫摩尔比Ca/S1.03石灰石(CaCO3)纯度P%90.009参加脱硫同容量锅炉台数n台4脱硫计算书原始输入数据列表校核结果序号名称符号单位计算公式或数值来源计算结果一烟气量计算1理论空气量V0Nm3/kg0.0889(Car+0.375Sar)+0.265Har-0.0333Oar5.022燃烧产物理论体积Vy0Nm3/kgVN20+VRO20+VH2O05.491)氮气VN20Nm3/kg0.79V0+0.008Nar3.972)二氧化物VRO20Nm3/kg0.01866(Car+0.375Sar)0.913)水蒸汽VH2O0Nm3/kg0.111Har+0.0124Mar+0.0161V00.623燃烧产物实际体积Vy'Nm3/kgVy0+0.0161(alfa'-1)V0+(alfa'-1)V08.704干烟气量Vgy'Nm3/kgVRO20+VN20+(alfa'-1)V08.045烟气含氧量和含湿量计算1)烟气中的水分VH2O'Nm3/kgVH2O0+0.0161(alfa'-1)V00.672)烟气中的氧量VO2'Nm3/kg0.21(alfa'-1)V00.663)干烟气中含氧量ngo2'%VO2'/Vgy'8.264)湿烟气中含氧量nsho2'%VO2'/Vy'7.625)湿烟气中含湿量nH2O'%VH20'/Vy'13.006)湿烟气中CO2含量nshCO2'%0.01866Car/Vy'10.297)干烟气中CO2含量ngCO2'%0.01866Car/Vgy'11.148)湿烟气中SO2含量nshSO2'%0.01866*0.375Sar/Vy'0.149)干烟气中SO2含量ngSO2'%0.01866*0.375Sar/Vgy'0.1510)湿烟气中N2含量nshN2'%(0.79alfa'V0+0.008Nar)/Vy'74.2711)干烟气中N2含量ngN2'%(0.79alfa'V0+0.008Nar)/Vgy'80.456总燃烧产物实际湿体积VtshyNm3/hVy'*Bj*10003037597总燃烧产物实际干体积VtgyNm3/hVgy'*Bj*10002642708总燃烧产物6%O2干体积Vtgy-O2Nm3/hVtgy*(21-ngo2')/(21-6)224492二烟气含硫量及脱硫量计算1脱硫进口SO2量Mkg/hBj*1000*Sy/100*0.7*64/22.41886.14kmol/hM/6413.852脱硫进口SO2实际浓度Cso2mg/Nm3M/Vtshy（标态，干基，6%O2）3947.32ppmCso2*22.41/641382.183要求脱硫量Mskg/hM*η*n/1003190.11kmol/hMs/6449.85三吸收剂消耗量计算1石灰石(CaCO3)理论消耗量M3kmol/hMs/64*(Ca/S)51.34kg/hM3*M15134.082石灰石(CaCO3)实际消耗量M3'kg/hM3*M1/(P/100)5704.53t/h5.70四脱硫产物计算1CaSO4.2H2O生成量M4t/hMs/64*M10/10008.573脱硫产物中飞灰含量M5t/hm2*2/30.80引风机出口飞灰总量m2t/hVtgy-o2*mh1.194未反应的CaCO3M6t/hM3/(ca/s)*((ca/s)-1))0.155CaCO3带入的杂质M7t/hM3'*(1-P/100)0.57脱硫计算书6脱硫产物总量M8t/hM4+M5+M6+M710.097皮带机出口石膏产量M9t/hM8/0.911.218石膏纯度n1%M4/M884.979总的脱硫产物量M8't/hM810.0910皮带机出口的石膏总产量M9't/hM911.2111年石膏生成量t/年M9'*H76233五脱硫耗水量计算11)1kg水蒸发需要热量:mshkj/kg(50-10)*4.18+25102677.20msh1t/hMs/64*339/msh6.312)热交换器放热端:126------t吸热端:50----85烟气比热kcal/Nm3.℃100℃0.3300kcal/Nm3.℃200℃0.3350i1kcal/Nm3.℃插值法:tpy0.3313i2插值法求85℃比热0.3293t℃t=126-i2*(85-50)/i191.22i3kcal/Nm3.℃插值法:t0.3296塔内烟气放热量Q1kJ/hV'*i3*4.18*(t-50)68987833塔内烟气放热蒸发水量msh2t/hQ1/msh25.773)单塔蒸发水量Mwet/hmsh1+msh232.08单塔蒸发水汽体积VweNm3/hMwe/18*106*22.4/100039922.172脱硫耗水量1)脱硫结晶水Mgyct/hM4/M10*(2*18)10.752)石膏表面水Mgyst/hM9*0.10.0153)FGD废水Mwwt/h(Bj*0.063%*1000+(Mgyc+Mgys+Mwe)*1000*0.000018-Vtgy*0.4*0.000001-M9*1000*0.01%)/0.02/10004.104)脱硫蒸发水量Mwet/h32.085)清洁冲洗水Mgywt/h估计10.006)泵与风机冷却用水Mwqt/h估计2.007）单套脱硫装置耗水量Mwt/hMgyc+Mgys+Mww+Mwe+Mgyw+Mwq58.958）总的脱硫装置耗水量Mw't/hn*Mw58.95六氧化空气量计算1需氧量Vo2kg/hSO2---1/2O2797.53kmol/hVo2/3224.922需空气量VkNm3/hVo2/32*22.41/0.212659.61七主要参数汇总四台炉的数据1吸收塔进口烟气量V'Nm3/h12150352吸收塔出口烟气量VNm3/hVtshy+Vk-Vo2+Vwe-Vso212567713脱水机出口石膏M9t/h含水10%11.214旋流站出口石膏浆液量M11t/hM8/0.5(含水50%)20.185石膏旋流站出口回流量M12t/hM13-M11-Mww(不包括废水)42.98吸收塔蒸发水量(假定吸收塔内温度为50℃,工业水温10℃)脱硫反应热蒸发水量(CaCO3+SO2+1/2O2+H2O----CaSO4.2H2O+339kJ/mol)烟气降温蒸发水量(未计放热损失)6吸收塔排出浆液量M13t/hM8/0.15(含水85%)67.267石灰石粉耗量M3't/h5.708工艺水量Mwt/h包括冷却水等58.959FGD废水Mwwt/h4.10八主要设备选择1吸收塔烟气流速νm/s取值3.30烟气量Qm3/hV*(273+50)/2731486948计算直径Dm（4*Q/3.14/ν/3600)0.513液气接触时间Ss取值3.50吸收塔高度Hmν*S11.55液气比L/G取值12.00浆液循环量Qcm3/h(L/G)*V/100015081.25浆液停留时间Tmin取值6.00吸收塔浆池容积V1m3Qc*T/601508.122石灰石粉仓容积m3按7天储量：M3'×7×24/0.9939.573石灰石浆池容积m3按4小时储量：M3'×4/0.3/1.21962.40备注烟气带水按13％考虑一台炉一台炉一台炉359.1866一台炉四台炉四台炉456453.96010.00620.0353680.0005894680.0837040.00340.0193950.000210820.0362610.050035四台炉四台炉114118.79153770.3112.05标书提供核算结果1BMCR工况烟气成分（标准状态，实际O2）O2（湿基）%Vol8.42（干基）%Vol7.83H2O（湿基）6.962标态，湿基，实际含氧量Nm3/s698698.0025128003标态，干基，实际含氧量Nm3/s649649.424标态，湿基，6%O2Nm3/s595585.39709.45955标态，干基，6%O2Nm3/s548544.659100.030.000331.2771082.002E+091014.6669624.1458