脱硫设计计算方法演示幻灯片.ppt

单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,单击此处编辑母版标题样式,单击此处编辑母版文本样式,第二级,第三级,第四级,第五级,*,湿式石灰石,-,石膏法烟气脱硫,设计方法及过程,1,湿法脱硫设计,1,、物料平衡计算：建立物料平衡表,烟气平衡,脱硫剂（脱硫产物）平衡,水平衡,2,烟气原始参数,3,确定关键参数,钙硫比,脱硫效率,液气比,石膏品质,石灰品质,4,脱硫剂的选取,脱硫剂矿源品位,脱硫剂的物理化学特性：真实密度、堆积密度、粒径分布、空隙率、分形、比表面积、活性、吸硫特性,影响脱硫剂吸硫特性的因素：水份、温度、浓度、脱硫剂物理特性,5,6,7,8,9,10,11,2,、建立工艺流程图,与物料平衡表同时,12,13,14,15,16,17,3,、关键控制回路,烟气量、烟气中二氧化硫浓度及钙硫比控制进浆量,pH,值调节,18,19,20,21,22,23,4,、脱硫反应塔,上升速度,停留时间,液气比,pH,值,循环浆液浓度,液柱高度,脱硫能力,搅拌,防腐蚀,防堵塞,24,氧化曝气装置,循环氧化槽的容量,氧化空气的停留时间,氧化空气的过量系数,氧化空气的压力、温度,循环浆液的,pH,值,CaSO,3,的结晶与,CaSO,4,结晶,氧化曝气装置的防堵塞,氧化曝气装置的防腐蚀,25,浆液喷射装置,浆液流量的调节,喷嘴的特殊结构,浆液管道的防腐蚀,浆液管道的防堵、防垢,26,27,28,29,5,、平面布置,30,烟气脱硫过程,设计计算,31,烟气平衡,32,燃煤,/,烟气组份,输入数据,机组容量,300 MWel,燃煤热值,(Hu)20.600 kJ/kg,全厂效率,41,3%,含硫量,0,79%,假定,:,1 kg,煤,8,5 Nm,(wet),烟气,含水量,7,2%,33,燃煤烟气组份,燃烧计算,34,燃煤烟气成分,水蒸汽密度,35,烟气密度,assumed data,Density flue gas 1,35 kg/Nm,质量流量,燃煤烟气成分,36,化学过程,输入数据,SO,2,removal efficiency 95%,S proportion in coal 0,79%,Coal 127 t/h,S+O,2,=SO,2,Note atomic mass:,S =32 g/mol,O =16 g/mol,Ca=40 g/mol,C =12 g/mol,H =1 g/mol,燃煤烟气成分,37,SO,2,production&removal,燃煤烟气成分,38,SO,2,-content,Input data,assumed data,O2 content in dry gas 7%,燃煤烟气成分,39,SO,2,content at 6%O2,燃煤烟气成分,40,吸收塔热动力学,/,绝热饱和,假定,电除尘器出口温度,138 C,GGH,出口温度,108 C,干烟气中水含量计算,41,在,h,x,图上,108 C,和,0,046 kg/kg,dry,的交点的焓,h=233 kJ/kg.,沿等焓线到饱和线可得到饱和温度,吸收塔热动力学,/,绝热饱和,42,Thermodynamics for scrubber/adiabatic saturation,43,吸收塔出口净烟气,吸收塔热动力学,/,绝热饱和,44,烟气计算结果,Absorber INLET,Absorber OUTLET,45,液相平衡,13%wt,50%wt,3%wt,46,石灰石消耗,/,石膏产量,1 SO2 +1 CaCO3 +2 H2O +1/2 O2 CaSO4,2H2O +CO2,Note molar mass:,SO2 =64 g/mol,CaCO3 =100 g/mol,H2O=18 g/mol,CO2 =44 g/mol,O2 =32 g/mol,CaSO4,2H2O=172 g/mol,Example:,A flue gas desulphurisation plant with 2 t/h SO2-emissions needs:,and produces:,47,水平衡,废水,(a)keep Cl,-,level ,15,to 20 g/l,(b)keep sulfate level 35 g/l,(b)keep ash+inert level in absorber slurry 13%,Waste water flow based on Cl,-,level,Input(assumption):,Data from experience,HCl-removal 98%,48,废水流量,水平衡,49,工艺水消耗,Sum of:,Water for flue gas saturation,Waste water,Moisture gypsum+crystal water,Droplet emission(negligible),水平衡,50,石膏脱水,For the scrubbing and crystallization process in the absorber,the gypsum solid content is between 5 and 20%.,Input,assumed data,51,石膏浆液的密度,石膏脱水,52,旋流器底流密度,旋流器顶流密度,石膏脱水,53,石膏产量,石膏脱水,54,水力旋流器,From Absorber,To Absorber,To Belt Filter,4,7assumption related to 13%solids in the flow from the absorber,3%solids,in the cyclone overflow and 50%solids in the cyclone underflow,石膏脱水,55,吸收塔来石膏浆液,石膏脱水,56,Absorber,Hydrocyclone underflow,Hydrocyclone overflow,Beltfilter,Filtrate,Mass flow suspension,47.940 kg/h,10.200 kg/h,37.740 kg/h,5.670 kg/h,gypsum wet,4.530 kg/h,Mass flow Gypsum dry,6.232 kg/h,5.100 kg/h,1.132 kg/h,5.100 kg/h,Mass flow,Water,41.708 kg/h,5.100 kg/h,36.608 kg/h,570 kg/h,water in gypsum,4.530 kg/h,Volume flow suspension,44,4 m/h,7,3 m/h,37,1 m/h,石膏脱水,57,水力旋流器顶流成分,(,假定,),50%of solids is gypsum,25%of solids is ash,25%of solids is limestone,石膏脱水,58,石灰石浆液供给,石灰石消耗,石灰石浆液密度,石灰石固体密度,石灰石浆液质量流量,59,石灰石浆液密度,石灰石浆液体积流量,石灰石浆液供给,60,浆池尺寸,浆液罐的停留时间,浆液罐体积,(,假定,),(,假定,),61,滤液箱尺寸,滤布冲洗水量,石膏冲洗水量,take 50%from gypsum mass flow(assumption),滤液量,62,滤液箱停留时间,(,假定,),滤液箱容积,(assumption),滤液箱尺寸,63,吸收塔尺寸,烟气流量,SO2,浓度,SO2-,脱硫率,液气比,:L/G=12 l/Am at absorber outlet(,假定,),64,吸收塔循环浆液流量及每泵的流量,Absorber temperature=48 C,喷淋层数,(pumps)=3,吸收塔尺寸,65,吸收塔直径,吸收塔烟气流速,w=3,7 m/s(assumption),吸收塔循环区体积,循环浆液停留时间,t=4,3 min(assumption),吸收塔尺寸,66,吸收塔循环浆液区高度,Sump height11,9 m,Height till flue gas duct 1,5 m,Flue gas duct height 4,0 m,Height to first spray bank(from flue gas duct)2,5 m,Spraying banks:2x1,5 m 3,0 m,Height till mist eliminator 1,3 m,Height of two stage droplet separators 2,5 m,Height flue gas outlet duct 3,0 m,Sum297 m,Total absorber height:H=30 m,吸收塔尺寸,67,增压风机和循环泵的能耗,增压风机,吸收塔压损,(assumption)10 mbar,GGH,压损,12 mbar,烟道压损,7 mbar,总压损,29 mbar,Specific flue gas transport work,For booster fan with 85%effectiveness,68,功率消耗,Pump efficiency=0,89,Volume flow(pump)=5.300 m/h,Liquid level=11,9 m,Geod.height=1,5 m+4,0 m+2,5 m+1,5 m=9,5 m,Pressure at nozzles=10 m (1 bar),Pressure height pipes=3 m,sum=22,5 m,增压风机和循环泵的能耗,69,中间层泵的能耗,三层泵的总能耗,增压风机和循环泵的能耗,70,烟道尺寸,净烟气烟道直径,Flue gas velocity w=18 m/s(assumption),Saturated clean gas,原烟气烟道直径,71,管道计算,1),石灰石浆液输送管,Particle size limestone=90%44 m,d,50,15,m,Concentration30%total solids amount,Transport velocity 6 x settling velocity,Normallyw,transport,2,5 m/s,Volume flow suspension =8 m,/h,石灰石浆液输送管直径,72,石灰石浆液循环管直径,Volume flow circulation2,V,suspension,(Absorber),管道计算,73,2),石膏浆液管径,Particle size gypsumd,50,=35 50 m,Transport velocity 6 x setting velocity,Normally w,transport,2,5 m/s,至旋流器石膏浆液管径,管道计算,74,氧化风计算,强制氧化,SO2+H2O HSO3,-,+H,+,HSO3,-,+,O2 SO4,2-,+H,+,1 mol SO2 needs,mol O2,1 kg SO2 needs 32:2/64 kg O2,Stoichiometric factor for O2-absorption in absorber sump 2,5,specific weight O2:,75,O2,体积,:,空气体积,:,氧化风计算,76,氧化风压头,Injection point in absorber:,distance to liquid level=6 m,氧化风计算,77,吸收塔搅拌器计算,Need of energy for agitating80 W/m,el,Absorber sump volume 865 m,Agitator capacity,P,el,=865 m x 80 W/m=69 kW,Number of agitators 4,能耗及搅拌器,78,石灰石粉仓计算,Capacity for limestone silo7 days(assumption),Maximum density1.400 kg/m,Normal density1.000 kg/m,Limestone consumption2,97 t/h,Storage volume,79,石膏仓计算,Capacity for gypsum storage 5 days(assumption),Normal density 1.000 kg/m,Gypsum production 5,11 t/h dry,5,11/0,9=5,7 t/h wet(10%moisture),存储容积,80,真空带式脱水计算,过滤面积,1 m for a gypsum production of 1 t/h dry(assumption),Gypsum production,Filter area=5,1 m(no redundance),真空带式脱水机容量,Install 2 filters with each 70%of maximal capacity,2 x 70%complete filter area,2 x 0,7 x 5,1 m,=2 filters each 3,5 m,81,所需真空泵,真空泵电耗,A typical pressure drop is 0,3 bar absolute,The energy needed for one cumicmeter of air is E,el,=40 Wh/m(assumption),The electric power needed for one belt filter is,P,el,=1.050 m/h x 40 Wh/m,P,el,=42 kW each filter,真空带式脱水计算,82,