電化學方法合成聚苯胺

1、 (27.12)rc4001.84587.34330.354891.14495.15324.2(54.24)計算所用的各溫度下的Cp底平均值，結(jié)果如表2-5r=r=ZxrciiC=ZxCpipi表5-10各溫度下的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脫重組分塔/D=171.2281)/D=171.22

2、81)、L/D=R=5.1986)=、L=890.1043)V=L+D=1061.332Q=FCAt=179.7279義19,2136義44=151941.7千卡/hTOC o 1-5 h zi_pQ=LCAt=890.1043義18,9897義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再沸器循環(huán)水由95降到61需熱水量M1M=-Q=5052568/(95-61)=148605kg/h.Q=CMAt11CAt6水11水1塔頂冷凝器冷卻水由29升到37需冷水量之5.2.3脫輕組分塔熱量平衡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設再沸器循環(huán)水由95降到61需水量為M1M=-Q-=

5、1100442/(9561)x1=32365.94kg/h需熱水量1。水t設再沸器循環(huán)水由20升到30需水量為忖2M=-Q-=1019848.1x(3020)=101984.8kg/h需冷水量2。水At26塔及換熱器的結(jié)構設計及選型61選塔依據(jù)浮閥塔版是在泡罩塔板和篩孔塔板的基礎上發(fā)展起來的，他吸收了兩種塔板的優(yōu)點，結(jié)構簡單、制造方便、造價低；塔板開孔率大，生產(chǎn)能力大；由于發(fā)片可隨氣量變化自由升降，故操作彈性大；因上升氣流水平吹入液層，氣泡接觸時間較長，故塔板效率較高，壓力降較低，課達到更好的分離效果和節(jié)省設計費用。塔的設計結(jié)果表6.1塔設計計算匯總表序號設備介質(zhì)位號操作溫度/塔頂塔釜回流比最

6、小實際塔板數(shù)理論實際氣體負荷/(m3/h)精餾段提餾段12T-0201A氣相粗脫重丁二烯份塔T-0202丁二烯脫輕組份塔37543.441439.554.2487.93095.2060.4314114.32.5593081396227.40150867.02045544.568911.6169續(xù)6.1序號液體負荷/(m3/h)精餾段提餾段空塔氣速/(m/s)精餾段提餾段塔板間距/(m)塔直徑塔盤形式186.320783.92340.55030.49050.52.3浮閥1.6浮閥222.163640.64450.21772.3浮閥1.6浮閥周口脫醛帶役計甥Fig&2Thedesignchanofthererrwe甘油1品由er換熱器的選擇換熱器的設計結(jié)果設備位號設備名稱型式型號殼體直徑mm換熱面積m2管長mm管徑mmAjVLL.管數(shù)管程殼程材質(zhì)E-0204脫重塔浮FB-2200-6001900123.09000204