第二章硫酸干吸系统设计的计算2.1干燥塔物料计算[16]2.1.1干燥塔入口炉气成分表2.1转化气进口气体成分项目相对分子量%密度kmolkgm3S0264.009.02.55176.984926.911931.370232.008.11.42969.282216.861551.34N228.0182.91.250709.0519862.8515890.28E100.0855.3027006.6319372.98H2018.020.8050.111.942.41表2.2电除雾器出口气体成分项目相对分子量%密度kmolkgm3SO264.0010.302.55176.984926.911931.370232.007.701.42957.551841.411288.60N228.0182.001.250612.8317167.4713733.97E100.00747.3523935.7916953.94H2O18.020.80561.941115.811386.10则：干燥塔入口补加空气量=19372.98-16953.94=2419.05m3/h2.1.2干燥塔入口炉气含水量设补加空气全部在电除雾器之后加入，空气温度20摄氏度、相对湿度75%，由湿含图查得水含量为10g/干空气m3,则补加空气带水量为：2419.05x0.01=24.19kg/h=1.34kmol/h=30.8m3/h2.1.3干燥塔入口气体带水设出塔气体中含水量为0.1g/m3,则干燥后气体带水量为：(0.1m1000)x19372.98=1.94kg/h2.1.4循环酸量决定循环酸量的方法一般有两种，一种是根据进出口酸浓度差决定，酸浓度差一般选在0.2%~0.4%范围内，第二个是根据塔的喷淋密度来决定，喷淋密度一般选在14〜20m3/(m2・h)的范围内。在这里采用浓度差计算循环酸量。入塔酸：浓度93.00%HSO比重1.799324温度50OC酸量xm3/h出塔酸：浓度92.7%干燥塔吸收水量=(+24.19)—1.94=1138.06kg/h由物料平衡得：Xx1.7993x1000x93%=(Xx1.7993x1000+1146)x92.7%X=195.44m3/h所以采用扬量为200m3/h酸泵,型号为IHIHF125-100-250酸泵。2.2干燥塔热量衡算2.2.1炉气带入热量Q1t=40OC时SO2带入热量：q]=76.98x40x41.57=127997.80KJ/hO2带入热量：q2=69.28x40x29.37=81389.60KJ/hQ2-Q1X4.186893%HSOT92.7%HSO,2424n二0.41N2带入热量：q3=709.05x40x28.45=806894.52KJ/hH2O带入热量：q4=(1.34+61.94)x40x32.716=82810.74KJ/h式中41.57,29.37,28.45,32.716分别为0〜40OC时S02、02、N2、H2O的摩尔热熔KJ/(mol・K)。Q1=q1+q2+q3+q4=1099092.66KJ/h2.2.2水的冷凝热Q2水在40OC时冷凝热为2406KJ/kgQ2=(1115.81+24.19—1.94)x2406=2738177.35KJ/h2.2.3入塔酸带入热Q350OC时93%H2SO4的热焓I1=78.7KJ/kgQ3=195.44x1.7993x1000x78.7=27675734.96KJ/h2・2・493%酸稀释热Q4Q二nX1234786<04.18n+1.7983式中：Q—稀释热,/moln一对于1molH2SO4所用水的mol数对于浓度为C的硫酸，当稀释到浓度为C时，放出的热量按下式计算:12X17860nX17860Q二13900n二0.429Q二143941222・2・5炉气带出热Q5SO2带出热量：q]=76.98x45x41.64=144245.12KJ/hO2带出热量：q2=69.28x45x29.395=91641.852KJ/hN2带出热量：q3=709.05x45x28.51=909675.70KJ/hH2O带出热量：q4=0.11x45x32.74=162.06KJ/h式中41.64,29.395,28.51,32.74分别为0〜450C时SO、O、N、HO的摩尔2222热熔KJ/(mol・K)。Q5=q1＋q2＋q3＋q4=1143475.48KJ/h1n+1.79323-^―n+1.7934Q—Q二493.8KJ/kmol21Q4195.X41.X993X9817719K4J1.h75则出塔酸的热焓1232141471.24351655.19+1138.0二91.1KJ/kg查表得：92.7%H2SO4I2=91.1KJ/kg时的温度为t=57.2OC2・3干燥塔循环酸槽的物料衡表2・3干燥塔循环槽物料衡算表上塔循环=X=195.44m3/h*1.7993kg/m3=351655.19kg/h进物料/kg/h出物料/kg/h从干燥塔冷却器来92.7%H2SO4352793.25上塔循环93%H2SO4351655.1998%酸串来98.5%H2SO419243.27去98%酸循环槽20381.33372036.52372036.522・4干燥塔酸循环槽热量衡算2・2・6出塔酸带出热Q6和酸温Q6=Q1＋Q2＋Q3＋Q4－Q5=32141471.24KJ/h干燥塔循环系统流程图45摄氏干燥塔系统流程炉气40摄氏2・4・1从干燥塔冷却器来到92・7%H2SO4带入热Qi=352793.25xIKJ/h2・4・2从98%酸循环系统串来到98・5%H2SO4带入热Q2=19243.27x79.34=1526760.91KJ/h式中：79.34为98.5%H2SO4的热焓，KJ/kg。2・4・3混合热由98.5%H2SO4、92.7%H2SO4两种浓度的硫酸，混合成93%H2SO4n二0.429q二0.429%17860x4.1868二14403KJ/kmol110.429+1.79830.083x17860n=0.083q=x4.1868=3295KJ/kmol220.083+1.7983n二0.41q二0.41x17860x4.1868二13900KJ/kmol330.41+1.7983m1=(352793.25x0....
