脱硫和烟气量计算书.docx

1、脱硫和烟气量计算书脱硫计算书序号夕I称符号单位计算公式或数值来源*烟气量计算1理论空气量V03Nm/kg0.0889(C ar +0.375S ar)+0.265H ar-0.03330 ar2燃烧产物理论体积V0yNm/kgVN2 +V RO2 +V H2O 1)氮气VN2 03Nm/kg0.79V +0.008N ar2)二氧化物0VRO23Nm/kg0.01866(C ar +0.375S ar)3)水蒸汽H20 0VNm/kgO.lllHar +0.0 1 24M ar +0.0 161V3燃烧产物实际体积Vy*sNm/kgo 0Vy +0.01 6 l(a Ifa 1-1)V Hai

2、fa f-l)V4干烟气量Vgy*Nm/kg0 0 0VRO2 +V N2 +(aifa f-l)V5烟气含氧量和含湿量计 算0 01)烟气中的水分VH20 3Nm/kgVH20 +0.0161 (a ita -1)V2)烟气中的氧量V02Nm/kg0.21 (a *-l)V3)干烟气中含氧量ngo21%VO2 7V gy*4)湿烟气中含氧量nsho2%VO2 7V y 5)湿烟气中含湿量I1H20 1%VH20 7V y6)湿烟气中CO2含量HshC02%0.01866Car/V y*7)干烟气中CO2含量ngC02%0.01866Car/V gyr8)湿烟气中SO2含量nshS02r%0.

3、01866*0.375Sar/V y*9)干烟气中SO2含量ngS02f%0.01866*0.375Sai7V gy*10)湿烟气中N2含量nshN2 1%(0.79a Ifa V+0.008Nar)/Vy11)干烟气中N2含量ngN2*%(0.79a Ifa V+0.008Nar)/Vgy6总燃烧产物实际湿体积Vt shyNm/hVy*B j*10007总燃烧产物实际干体积Vtgy3Nm/hVgy *Bj*10008总燃烧产物6%O2干体积Vt gy-023Nm/h1Vtgy *(21-n go2 )/(21-6)二烟气含硫量及脱硫量计 算1脱硫进口 SO2量Mkg/hBj*1000*Sy/

4、l 00 切.7*64/22.41kmol/hM/642脱硫进口 S 02实际浓度Cso23ms/NmM/Vt shy （林态，丨基，6%O2）ppmCso2*22.41/643妥吝月兄阮車Mkg/hM*n *n/100kmol/hMs/64三吸收剂消耗量计算1石灰（CaO）理论消耗量M?kmol/hMs/64*(Ca/S)kg/hM3*M12石灰（CaO）实际消耗星kg/hM3*M1 /(P/100)t/ht/a3傑碱的理论消耗量M12kmol/hMs/64 *(Na/S)kg/hMoh*M12NaOH的实际耗量kg/h四脱硫产物计算12H O戈量CaSO4 2M4t/hM s/64*M i

5、o/IOOO3脱硫产物中飞灰含量M5t/hm2 *2/3引风机出口飞灰总量m2t/hV tgy-o2 *m h4未反应的CaCO3M6t/hM 3/(ca/s)*(ca/s)-l)5带入的朵质CaCChM7t/hM3*(l-P/100)6脱硫产物总量Mst/hM 4+M 5+M6+M77皮带机岀口石膏产量M9t/hM 8/0.98石膏纯度ni%M4/Ms9总的脱硫产物量Mst/hMs10皮带机出口的石膏总产 hlM9t/hM911年石膏生成量t/年M9*H五脱硫耗水量计算1吸收塔蒸发水量（假定吸收塔内温度为50C,工业水温10C）1) 13水蒸发需要热量：mshkj/|R(50-10)*418

6、+2510 |脱硫反应热蒸发水量 (CaCO 3+SO2 +1/20 2 +H 20一一CaSO 4 .2H? O+339kJ/mol)%t/hMs/64*339/m sh 12)烟气降温蒸发水量（未计放热损失 ）热交换器放热端：126 1 吸热端：50-85烟气比热kcal/Nm 3 .C100 Ckcal/Nm 3 .C200 C1 1kcal/Nm 3 .C插值法：tpyi 2插值法求85 C比热tCt=126-i 2*(85-50)/i i1 3kcal/Nm 3 C插值法:t塔内烟气放热量QikJ/hV *i3 *4.18*(1-50)塔内烟气放折蒸兌水吊mt/hOi /m sh3)

7、 1塔蒸发水量Mwet/hmshl+msh2V3Nm/h6M wc/1 8*10 4A10002甲堆蒸友水注体积脱磕耗水量we1)脱硫结晶水Mgvct/hM 4/M 10 *T2*1 812)脱硫濟表面水Mjvst/hM 13)FGD废水Mwwt/h(B j*0.063%*1000+(M gyc +M gys +M we)*l000*0.000018-Vtgy *0.4*0.000001-M 9*1000*0.01%)/O.O2/10004)脱硫蒸发水量Mwet/h5)清洁冲j先水VWt/h估计6)泵弓风机冷却用水Mwat/h估计7)单査呻磕奘罟軽水畐Mu/t/hrt rz* a w 1T x

8、i.iir 4-a jij 4- 1K/T8)总的脱磕奘詈耗水最t/li In *M w八1氧化空气量计算X 71Vo2kg/hSO 21/20 2kmol/hVo2/322需空气量VkTNm/hVo2 /32*22.41/0.21七主要参数汇总一台炉的数据1吸收塔进口烟气量V*Nm/h2吸收塔岀口烟气量V”7Nm/hVt shy +V k-V o2+V we-V so23脱水机出口石膏Myt/h含水10%4旋流站出口石膏浆液量Milt/hM 8/0.5(含水 50%)5石膏旋流站出口回流量M12t/hM13-Mll-Mww（不包括废水）6吸收塔排岀浆液量M13t/hM8/0.15(含水 85

9、%)7石灰石粉耗量t/h8工艺水量Mwt/h包括冷却水等FGD废水M-wwt/h八主要设备选择1吸收塔烟气流速Vm/s取值烟气量Qm/hV”273+50)/273计算直径Dm(4*Q/34/ v /3600) 0 5液气接触时间Ss取值吸收塔高度Hmv *S液气比L7G取值浆液循环量Qc3m /h( /G1W71000浆液停留时间Tmin取值吸收塔浆池容积VIm3Oc/602石灰粉仓容积m3按 7 天储量：Ms * X7X24/0.93石灰浆池容积按4小时储量：M3nr1 X4/0.3/1.219计算结果备注5.505.834.351.020.469.368.840.510.738.237.7

10、8烟气带水按13%考虑13.0010.7011.330.220.2475.8180.21969731一台炉843666一台炉718145一台炉4458.4269.666208.252173.864235.50一台炉66.1869.493891.374864.21一台炉43.31132.361149.032456453.9601270.120.0062 0.030158 0.000502635 0.0713740.0034 0.016538 0.000179764 0.03091911.382.553.820.190.9715.0916.7675.4415.090.06770616.76134116二台炉0.33000.33500.33130.329391.220.329622023929282.2690.641 12802.4014.540.01911.9690.6410.002.00129.17二台炉129.171058.8833.093531.16969731108387616.7630.1858.45100.594.86129.1711.963.80128238810.933.5013.303.003251.636.00325.16801.1653.201083.883.47114 118.7915