石灰石石膏湿法脱硫计算

1校核煤质Car=64%Nar=1%Har=5%War=8%Oar=6.6%Aar=16%Sar=0.4%Var=15%换算成干燥无灰基的元素含量Cdaf=84.21053%取Cdaf=84%Hdaf=6.578947%Hdaf=6.6%Odaf=8.684211%Odaf=8.7%Sdaf=0.526316%Sdaf=0.5%Qdaf,net=344.3447MJ/kg取Qdaf,net=34.4MJ/kgQar,net=26.144MJ/kg取Qar,net=25.8MJ/kg石灰石/石膏湿法脱硫339Cdaf+1030Hdaf-109(Odaf-Sdaf)=换算成低位收到基发热量Qdaf,net*76/100=38%含硫量为0.4%燃烧计算mcoal=mcoal=0.073439=73.4t/h2Qa’=6.804325m³/kg取Qa’=6.8m³/kg3Qs’==7.345681m³/kg取Qs’=7.35m³/kg4α=1.3Qs==9.42264m³/kg取Qs=9.4m³/kg5dsh=16%4.76*（1.867CY+5.56HY+0.7SY-0.7OY）=标准状况下理论烟气量（空气含湿量为12.93g/m³）全厂效率为标准状况下理论空气量1.867（CY+0.375SY)+11.2HY+1.24WY+0.016Qa'+0.79Qa'+0.8NY标准状况下实际烟气量空气过剩系数Qs’+1.016(α-1)Qa'标准状况下烟气含尘浓度排烟中飞灰占煤中不可燃组分的比例uelHP*600.3*C==0.002723kg/m³取C=0.002723kg/m³6CSO2==851.0638mg/m³取CSO2=852mg/m³6%CSO2,at4.6%=CSO2,at4.6%=931.52mg/m³取CSO2,at4.6%=932mg/m³200mg/m³CSO2,at6%=218.6667mg/m³取CSO2,at6%=219mg/m³76.52582%取77%7mSO2==0.5872t/h取mSO2=0.59t/hmSO2,removal=0.4543t/h二氧化硫排放标准（标准状态下）：除硫效率为标准状况下SO2燃烧产量SO2的脱除量标准状况下烟气中浓度SO2浓度的校准基准氧含量为sYshQA*d610*2sYQS%6,,%6.4,,%6.4,22222*OairOOairOatSOCCCCCcoalYSSOmSMM**2取mSO2,removal=0.45t/h8ρ=0.778501kg/Nm³取ρ=0.78kg/Nm³9689960Nm³/h取690000Nm³/h632730Nm³/h取633000Nm³/hVwater=57000Nm³/h10烟气体积流量Vfluegas,wet=mfluegas,dry=Vdry.ρfluegas,dryVfluegas,dry=烟气质量流量烟气中水蒸气密度由理想气体状态方程得Vfluegas,wet=mcoal.VfluegasVfluegas,wet=Vfluegas，dry=Vfluegas,wet.(1-0.083)=PVwater=nwaterRTRTPVwaterwaternwaterwatwewaterMmn100015.272314.81897860RTPMVmwaterwaterwater1.34kg/m³848220kg/h取848000kg/hmwater=44460kg/h892460kg/h取892000kg/h11135°C108°Cx1=0.052429取x1=0.052248kJ/kgT=48°Cx2=0.077GGH出口温度为干烟气水含量在h,x图上，108°C和0.052的交点的焓h=mfluegas,wet=吸收塔饱和温度计算假定电除尘器出口温度为沿等焓线到饱和线可得到饱和温度Tmwater,vapourised=(xwater,outlet-xwater,inlet).mfluegas,dry烟气密度（标准状态）：ρ=mfluegas,dry=mfluegas,dry=mfluegas,wet=mfluegas,dry+mwatermfluegas,wet=dryfluegaswatermmx,121200kg/h=27179.49Nm³/h取27000Nm³/h1284000Nm³/h717000Nm³/h13Vwet=690000Nm³/hVdry=633000Nm³/hmwet=892000kg/hmdry=848000kg/hVwater57000Nm³/hmwatewr44460kg/hT1=108°CO2=6%(dry)Vcleangas,wet=吸收塔烟气计算结果汇总13.1吸收塔入口：吸收塔出口净烟气的计算Vwater,vapourised,cleangas=Vwater+Vwater,saturationVwater,vapourised,cleangas=Vcleangas,wet=Vinlet,dry+Vwater,vapourised,cleangasmwater,vapourised=Vwater,saturation=saturationwatervapourisedwatersaturationwatermV,,,SO2=852mg/m³SO2,6%O2=932mg/m³Vwet=717000Nm³/hVdry=633000Nm³/hmwet=913200kg/hmdry=848000kg/hVwater84000Nm³/hmwatewr65520kg/hT1=48°CO2=%(dry)SO2=200mg/m³SO2,6%O2=219mg/m³1446mg/Nm³9815g/LmCl-=28.53564kg/h假定烟气中HCl的浓度CHCl，fluegas=HCl的去除率为废水中Cl-含量保持mCl-=0.98.CHCl,fluegasVdry13.2吸收塔出口：废水流量的计算取mCl-=28.5kg/hmwater=1900kg/h150.709844t/h取0.7t/h石膏产量1.220931t/h取1.2t/h16mwater=23484.5kg/h取mwater=23484kg/hVmater=23.484m³/h172.3kg/l1kg/l假定13%50%90%水的密度ρwater=吸收塔石膏浓度Cgypsum=旋流器底流石膏浓度Cgypsum=真空皮带机石膏浓度Cgypsum=mwater=mwater,vapourised+mwashwater+mcrystalwater+mgypsum,moisture石膏脱水（石膏密度ρgypsum=石灰石消耗量/石膏产量SO2+CaCO3+2H2O+1/2O2→CaSO4.2H2O+CO2石灰石耗量工艺水消耗量ClwaterClwashwaterCmm.3%ρs=1.079305kg/l取ρs=1.079kg/l1.393939kg/l取1.394kg/l1.017249kg/l取1.017kg/lmbeltfilter==1333.333kg/h取mbeltfilter=1330kg/h=2400kg/h=1.721664m³/h取1.72m³/hρs,hydrocyclone,overflow=17.1石膏浆液密度计算17.2旋流器底流密度计算ρs,hydrocyclone,underflow=ρs,hydrocyclone,underflow=ρs,hydrocyclone,overflow=旋流器顶流石膏浓度Cgypsum=17.3旋流器顶流密度计算17.4脱水石膏产量mhydrocyclone,underflow=Vhydrocyclone,underflow=Vhydrocyclone,underflow=)).(100(1gypsumwatergypsumgypsumwatersCbeltfirtergypsumgypsumCm,underflownehydrocyclogypsumgypsumCm,,underflownehydrocyclosunderflownehydrocyclom,,,11280kg/hmgypsum=1466.4kg/h取mgypsum=1466kg/h9814kg/h=10.45412m³/h取10.45m³/h180.7t/h30%2.8kg/l=2.333333t/h取2.33t/hmfrom,absorbor=mgypsum=mfrom,absorbor.Cgypsum17.5吸收塔来石膏浆液计算mfrom,absorbor=mhydrocyclone,underflow+mhydeocyclone,overfloemfrom,absorbor.Cgypsum=mhydrocyclone,underflow.Cgypsum,underflow+mhydeocyclone,overfloe.Cgypsum,overflow联立以上方程组解得msuspension=msuspension=18.2石灰石浆液密度mwater=mfrom,absorbor-mgypsum=Vfrom,absorbor=Vfrom,absorbor=石灰石浆液供给石灰石耗量mCaCO3=假定石灰石浆液浓度CCaCO3=石灰石固体密度ρCaCO3=18.1石灰石浆液质量流量sabsorborfromm,33CaCOCaCOCm1.238938kg/l取1.24kg/lVsuspension==1.879032m³/h取Vsuspension=1.88m³/h192h3.76m³1.495751m取D=1.5m2.25m205t/h以50%浆液罐体积Vtank=Vsuspension.△t=H=1.5×D=滤池箱尺寸计算ρsuspension=ρsuspension=18.3石灰石浆液体积流量浆液池尺寸D=(0.89.Vtank)1/3=假定浆液停留时间△t=假定滤布冲洗水量mwater,beltfilter=的石膏质量流量作为石膏冲洗水量20.1滤液量)).(100(1333CaCOwaterCaCOCaCOwatersuspensionCsuspensionsuspensionm5.6t/h5.6m³/h1h5.6m³1.70815m取D=1.7m2.55m21690000Nm³/h932mg/m³二氧化硫脱除率77%12l/Nm³48°C842996.7Nm³/h假定滤液箱停留时间△t=Vtank=Vwater,filtrate.△t=mwater,filtrate=二氧化硫浓度CSO2=假定液气比L/G=吸收塔出口净烟气温度T2=mwater,filtrate=mwater,beltfilter+mwater,washVwater,filtrate≈20.2滤液箱容积Vwet,actual=D=(0.89.Vtank)1/3=H=1.5×D=吸收塔尺寸的设计21.1循环浆液流量烟气流量Vwet=Vwet,actual=wetcleangasVT,2.15.27315.273取843000Nm³/h=234.1667Nm³/s取234Nm³/s10116Nm³/h3Q单循=3372Nm³/h=0.936667Nm³/s取Q单循=0.937Nm³/s3.7m/sd==8.973505m取d=9m4.3min724.98m³取725m³Vwet,actual=Vwet,actual=循环浆液流量设计喷淋塔层数为每层循环浆液流量21.2吸收塔直径假定吸收塔烟气流速ω=21.3吸收塔循环区体积假定循环浆液停留时间t=Vabsorbersump=Vabsorbersump=21.4吸收塔总高浆液池位高度1000/,GLVQactualwet循n循QactualwetV,460.tQ循H1=11.39628m取H1=11.4