乙烯-乙烷體系對(duì)篩板精餾塔的設(shè)計(jì)【含CAD圖紙】【GC系列】
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第三章 精餾塔設(shè)計(jì) 31設(shè)計(jì)條件工藝條件：飽和液體進(jìn)料，進(jìn)料乙烯含量(摩爾百分?jǐn)?shù))塔頂乙烯含量，釜液乙烯含量，總板效率為0.6。操作條件：塔頂操作壓力2.6MPa(絕)。安裝地點(diǎn)：大連。塔板設(shè)計(jì)位置：塔頂塔板形式：篩板處理量：180kmol/h回流比系數(shù)：1.73.2操作方程D=117.55kmol/h W=62.45kmol/h相對(duì)揮發(fā)度由P-T-K圖求得為1.464x=0.65, y=*x/(1+(-1)x)=0.731R=1.7Rmin=5.436精餾段操作方程：提餾段操作方程：3.3塔板數(shù)計(jì)算編程運(yùn)算得Nt=37,第18塊板為進(jìn)料板運(yùn)算結(jié)果為x1=0.985428,y1=0.990000x2=0.979837,y2=0.986139x3=0.973029,y3=0.981419x4=0.964778,y4=0.975670x5=0.954836,y5=0.968703x6=0.942941,y6=0.960308x7=0.928828,y7=0.950263x8=0.912249,y8=0.938346x9=0.892999,y9=0.924346x10=0.870950,y10=0.908092x11=0.846083,y11=0.889473x12=0.818523,y12=0.868475x13=0.788565,y13=0.845204x14=0.756677,y14=0.819907x15=0.723484,y15=0.792980x16=0.689729,y16=0.764953x17=0.656204,y17=0.736450x18=0.623680,y18=0.708141x19=0.585894,y19=0.674408x20=0.541425,y20=0.633498x21=0.490905,y21=0.585354x22=0.435760,y22=0.530658x23=0.378131,y23=0.470954x24=0.320584,y24=0.408561x25=0.265670,y25=0.346258x26=0.215493,y26=0.286804x27=0.171428,y27=0.232479x28=0.134061,y28=0.184772x29=0.103302,y29=0.144316x30=0.078595,y30=0.111014x31=0.059137,y31=0.084265x32=0.044051,y32=0.063199x33=0.032495,y33=0.046866x34=0.023724,y34=0.034354x35=0.017115,y35=0.024859x36=0.012160,y36=0.017703x37=0.008461,y37=0.012339nf=0,nt=0程序：#include #include #define N 200main()int i=0,nt,nf;FILE *fp;double xN,yN,e,f,R,Rm,L,V;double a=1.464,d=0.99,w=0.01,z=0.65,q=1,D=117.55,F=180;fp=fopen(text.txt,w);e=0.65;f=a*e/(1+(a-1)*e);Rm=(d-f)/(f-e);R=Rm*1.7;x0=d;y0=d;y1=d;while(xiz)i+;xi=yi/(a-(a-1)*yi);yi+1=R*xi/(R+1)+d/(R+1);printf(x%d=%lf,y%d=%lfn,i,xi,i,yi);fprintf(fp,x%d=%lf,y%d=%lfn,i,xi,i,yi);printf(the %dth tray is the input trayn,i);L=D*R;V=D*(R+1);while(xiw)i+;yi=(L+F)/V*(xi-1-w)+w;xi=yi/(a-(a-1)*yi);printf(x%d=%lf,y%d=%lfn,i,xi,i,yi);fprintf(fp,x%d=%lf,y%d=%lfn,i,xi,i,yi);printf(the total population of the trays is %dn,i);fprintf(fp,nf=%d,nt=%dn,nf,nt);fclose(fp);3.4 精餾塔工藝設(shè)計(jì)1、物性數(shù)據(jù)：操作溫度： 塔頂：-6.0， 塔底9.8塔頂按純乙烯處理：t=-6.0,P=2.6Mpa(絕)物性：摩爾質(zhì)量：M=28.052kg/kmol ， 2、流量精餾段氣液相流量：提餾段氣液相流量：3、塔徑塔高計(jì)算選取塔板間距Ht=0.45m， 查圖得：=0.0061C=液泛氣速 取泛點(diǎn)率0.8，所需氣體流通截面積選取Ad/At=0.08，塔徑D= =1.583m圓整取D=1.6m根據(jù)塔徑、流量，塔板間距合適，液流形式為單流型。實(shí)際塔板尺寸如下：1.850實(shí)際氣速：實(shí)際泛點(diǎn)率：=0.7833實(shí)際塔板數(shù) 精餾31，提餾29塔有效高度釜液流出量4.836設(shè)釜液停留時(shí)間20min則釜液高度m進(jìn)料板兩板間距0.9m設(shè)6人孔，=0.8m裙座取5m塔頂及釜液上方氣液分離高度取1.5m總塔高Z= + +(0.8-0.45)*6+1.52+5=37.9m3.5溢流裝置設(shè)計(jì)采用單流型弓形降液管D=1.6m =2.011 查得，堰長(zhǎng)=1.088m取塔板厚4mm，堰高50mm，底隙30mm3.6 塔板布置及其他結(jié)構(gòu)尺寸選取取進(jìn)出口安定區(qū)寬度=0.07m，邊緣寬度=0.05m，查圖得=0.14，降液管寬度=0.224m)=0.653m=0.75m=1.670取篩孔直徑，篩孔中心距t=3=120mm篩孔總截面積篩孔氣速 篩孔個(gè)數(shù)個(gè)3.7塔板校核1、液沫夾帶量校核，泛點(diǎn)率0.7833，查得0.0533小于0.1,液沫夾帶量符合校核要求2、塔板阻力計(jì)算干板阻力d/=4/4=1,可查得=0.82故=0.055m塔板清液層阻力，由m/s氣體動(dòng)能因子查圖得，故=0.0667m表面張力阻力塔板阻力3降液管液泛校核，取，=1.18=0.0256，不會(huì)產(chǎn)生降液管液泛4 液體在降液管內(nèi)停留時(shí)間，符合校核要求5嚴(yán)重漏液校核0.531k=1.8871.5，不發(fā)生嚴(yán)重漏液3.8塔板性能負(fù)荷圖1 過(guò)量液沫夾帶線(xiàn)設(shè)ev = 0.1（ kg 液體 / kg氣體）得： =8087.54-233.50qVLh2/3 由上述關(guān)系可作得線(xiàn)2 液相下限線(xiàn) 整理出：qVLh=3.3402 由上述關(guān)系可作得線(xiàn)3 嚴(yán)重漏液線(xiàn)將下式分別代入得：qVVh =a(b+cqVLh2/3)1/2其中：a= =2456.24 b=0.0056+0.13hw-h=0.01201 c= =0.000349得：qVVh =2456.24(0.01201+0.000349qVLh2/3)1/2 由上述關(guān)系可作得線(xiàn)4 液相上限線(xiàn)令 =5s 得： =52.115由上述關(guān)系可作得線(xiàn)5 降液管液泛線(xiàn) Hd=HT+hW= 將 以及how與qVLh , hd 與qVLh ，hf 與qVVh , qVLh 的關(guān)系全部代入前式整理得： 式中：a= =1.6568 b= =0.211 c= =1.107610 d= =0.004779 上述關(guān)系可作得降液管液泛線(xiàn)上五條線(xiàn)聯(lián)合構(gòu)成負(fù)荷性能圖操作點(diǎn)為：qVLh =51.52m/s qVVh =687.26 m/s負(fù)荷性能圖： 設(shè)計(jì)點(diǎn)位于四條線(xiàn)包圍的區(qū)間內(nèi)操作彈性：qVVhmax / qVVhmin=2.337
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