电化学方法合成聚苯胺

1、 (27.12)rc4001.84587.34330.354891.14495.15324.2(54.24)计算所用的各温度下的Cp底平均值，结果如表2-5r=r=ZxrciiC=ZxCpipi表5-10各温度下的Cprc平均值2218.526.7520.521.527.1219.75C19.213618.989720,201129.486119,142130.152225.3696p443753414354.2439.5rc4689.68624781.74024932.3064719.1774709.6864497.04944955.2.2脱重组分塔/D=171.2281)/D=171.22

2、81)、L/D=R=5.1986)=、L=890.1043)V=L+D=1061.332Q=FCAt=179.7279义19,2136义44=151941.7千卡/hTOC o 1-5 h zi_pQ=LCAt=890.1043义18,9897义37=625404.1千卡/hpQ=VCAt+Vr=1061.332x18.9897x37+1061.332x4781.7402=5820728千卡/h3p37Q=WCAt=(FD)CAt=8.4998x20.2011x53.5=9186,234千卡/hppQ=DCAt=171.2281x18.9897x37=120308.1千卡/hpQ=Q+Q+QQ

3、+Q+Q=Q+Q325715416Q=QQQ=2388797.065256818.23949218.2122=5075016千卡/h7325Q=Q+Q+QQ=3917.8604+49218.2432+2082760.58362141.9393=5052568千卡/h64571再沸器循环水由95降到61需热水量M1M=-Q=5052568/(95-61)=148605kg/h.Q=CMAt11CAt6水11水1塔顶冷凝器冷却水由29升到37需冷水量之5.2.3脱轻组分塔热量平衡D=1.9588)(L=225.0812“/D=114.9077)_D=1.9588,V_L+D_227.04Q=FCA

4、t=171.2281x29.4861x41=207002.8千卡/h1pQ=LCAt=225.0812x25.3696x39.5=225553.7千卡/h2pQ=VCAt+Vr=227.04x19.1412x44+227.04x4709.6864=1256166千卡/h3p44Q=WCAt=169.2693x3.1522c54.2427632千卡/h4pQ=DCAt+Dr=1.9588x25.3696x39.5+1.9588x4493.3469=10764.49千卡/h5pQ=QQQ=1019848千卡/h7325Q=1100442千卡/h6设再沸器循环水由95降到61需水量为M1M=-Q-=

5、1100442/(9561)x1=32365.94kg/h需热水量1。水t设再沸器循环水由20升到30需水量为忖2M=-Q-=1019848.1x(3020)=101984.8kg/h需冷水量2。水At26塔及换热器的结构设计及选型61选塔依据浮阀塔版是在泡罩塔板和筛孔塔板的基础上发展起来的，他吸收了两种塔板的优点，结构简单、制造方便、造价低；塔板开孔率大，生产能力大；由于发片可随气量变化自由升降，故操作弹性大；因上升气流水平吹入液层，气泡接触时间较长，故塔板效率较高，压力降较低，课达到更好的分离效果和节省设计费用。塔的设计结果表6.1塔设计计算汇总表序号设备介质位号操作温度/塔顶塔釜回流比最

6、小实际塔板数理论实际气体负荷/(m3/h)精馏段提馏段12T-0201A气相粗脱重丁二烯份塔T-0202丁二烯脱轻组份塔37543.441439.554.2487.93095.2060.4314114.32.5593081396227.40150867.02045544.568911.6169续6.1序号液体负荷/(m3/h)精馏段提馏段空塔气速/(m/s)精馏段提馏段塔板间距/(m)塔直径塔盘形式186.320783.92340.55030.49050.52.3浮阀1.6浮阀222.163640.64450.21772.3浮阀1.6浮阀周口脱醛带役计甥Fig&2Thedesignchanofthererrwe甘油1品由er换热器的选择换热器的设计结果设备位号设备名称型式型号壳体直径mm换热面积m2管长mm管径mmAjVLL.管数管程壳程材质E-0204脱重塔浮FB-2200-6001900123.09000204