南昌大學(xué)甲醇水連續(xù)精餾塔的課程設(shè)計

1、化工原理課程設(shè)計3.1.1 一、設(shè)計題目甲醇-水連續(xù)精僻塔的設(shè)計二、設(shè)計條件1、常壓操作：p=1atm2、進(jìn)精僻塔的料液含甲醇61%（質(zhì)量），其余為水3、產(chǎn)品的甲醇含量不得低于99%（質(zhì)量）4、殘液中甲醇含量不得高于3%（質(zhì)量）5、生產(chǎn)能力為日處理（24h）66.5噸粗甲醇三、設(shè)計內(nèi)容:設(shè)計方案的確定及流程說明:選擇塔型精僻塔屆氣一液傳質(zhì)設(shè)備。氣一液傳質(zhì)設(shè)備主要有板式塔和填料塔兩大類。該塔設(shè)計生產(chǎn)時日要求較大，由板式塔與填料塔比較知：板式塔直徑放大時，塔板效率較穩(wěn)定，且持液量較大，液氣比適應(yīng)范圍大，因此本次精僻塔設(shè)備選擇板式塔。篩板塔是降液管塔板中結(jié)構(gòu)最簡單的，制造維修方便，造價低，相同條件下

2、生產(chǎn)能力高于浮閥塔，塔板效率接近浮閥塔。本次設(shè)計為分離甲醇與水，所以由各方面條件考慮后，本次設(shè)計應(yīng)用篩板塔。3.1.2 :精僻方式3.1.3 由設(shè)計要求知，本精僻塔為連續(xù)精僻方式:裝置流程的確定為獲取也液相產(chǎn)品，米用全凝器。含甲醇61%（質(zhì)量分?jǐn)?shù)）的甲醇-水混合液經(jīng)過預(yù)熱器，預(yù)熱到泡點進(jìn)料。進(jìn)入精僻塔后分離，塔頂蒸汽冷凝后有一部分作為產(chǎn)品經(jīng)產(chǎn)品冷卻器冷卻后流入甲醇貯存罐，一部分回流再進(jìn)入塔中，塔底殘留液給再沸器加熱后，部分進(jìn)入塔中，部分液體作為產(chǎn)品經(jīng)釜液冷卻器冷卻后流入釜液貯存罐。3.1.4 :操作壓強(qiáng)的選擇常壓操作可減少因加壓或減壓操作所增加的增、減壓設(shè)備費用和操作費用，提高經(jīng)濟(jì)效益，在條件

3、允許下常采用常壓操作，因此本精僻設(shè)計選擇在常壓下操作。3.1.5 :進(jìn)料熱狀態(tài)的選擇泡點進(jìn)料時，塔的操作易于控制，不受環(huán)境影響。飽和液體進(jìn)料時進(jìn)料溫度不受季節(jié)、氣溫變化和前段工序波動的影響，塔的操作比較容易控制。此外，泡點進(jìn)料，提僻段和精僻段塔徑大致相同，在設(shè)備制造上比較方便。冷液進(jìn)塔雖可減少理論板數(shù)，使塔高降低，但精僻釜及提僻段塔徑增大，有不利之處。所以根據(jù)設(shè)計要求，可采用泡點進(jìn)料,q=1。3.1.6 :加熱方式3.1.7 本次采用間接加熱，設(shè)置再沸器:回流比的選擇選擇回流比，主要從經(jīng)濟(jì)觀點出發(fā)，力求使設(shè)備費用和操作費用最低，一般經(jīng)驗值為：R=（1.22）Rmin經(jīng)后面簡捷法計算對應(yīng)理論板數(shù)

4、N時，可知，R=2Rmi出寸，理論板數(shù)最少，所以回流比選擇為最小回流比的2倍。3.2:二元連續(xù)板式精僻塔的工藝計算3.2.1:相對揮發(fā)度的確定根據(jù)安托因方程logpO=ABr"cABC甲醇7.197361574.99238.86水7.074061657.46227.02查表得安托因常數(shù)塔頂產(chǎn)品濃度為99%因此，可近似看成純甲醇溶液；同理，塔底濃度為3%可近似看成純水溶液。所以，塔頂溫度為甲醇沸點為64.6C,塔底溫度為水的沸點100C。因此塔底的相對揮發(fā)度aW=3.497塔頂?shù)南鄬]發(fā)度aD=4.1383.2.2:全塔物料衡算總物料：F=D+W易揮發(fā)組分：FxF=DxD+WxWF、W

5、分別為進(jìn)料、僻出液和釜液的流量（kmol/h）xF、x»xW分別為進(jìn)料、僻出液和釜液中易揮發(fā)組分的組成、摩爾分率由操作條件得；F66.51000=86.475kmol/h2432.0420.610.99xf32.042=0.46770.610.3932.042180.03x-0.9832.04218xW:32.042=0.0170.030.97即:32.0421886.475=D+W86.475*0.4677=0.98D+0.017W解得：D=40.752kmol/hW=45.7233kmol/h3.2.3:平衡線方程:x3.804xy=1（：-1）x12.804x3.2.4:精僻段

6、操作線方程已知q=1、即xe=xF=0.4677a=3.804Y10.98x10.927960003Y20.94978x20.832543565Y30.894257x30.689745445Y40.811163x40.530345371Y50.718408x50.40143852Y60.581773x60.26776421Y70.385392x70.141513587Y80.199918x80.061637695Y90.082572x90.023113414y100.025976x100.0069618813.2.6:理論板數(shù)的求算(1)逐板計算法第一層板上升蒸汽組成等丁塔頂產(chǎn)品組成:根據(jù)操作

7、線方程以及平衡線方程可得如下:即：可知理論板數(shù)為10塊第5層理論版為進(jìn)料板精僻段理論板數(shù)為4層提僻段理論板數(shù)為5層(2)直角梯級圖解法3)簡捷法Rmin=0.6958x5<xFx10<xW即Ye3.8040.46771(:-1)x一12.8040.4677=0.7698即=土業(yè)我98一0.7698=0.4103Rmin1Xd-xF0.98-0.4677解得：Rmin=0.6958即R=2Rmin=1.3916所以精僻段的操作線方程為R1Yn1=XnXd=0.5819Xn0.4098R1R1xn:見第八頁yn+1:同上3.2.5:提僻段操作線方程Yn1rdf(R1)DXnF-D(R1

8、)DXw=1.4691x0.00798Y1=xD=0.98l0.980.983Nming0020.017=5.95lg3.804根據(jù)吉利蘭經(jīng)驗關(guān)聯(lián)圖以及關(guān)系式求得：R(R-Rmin)/(R+1)(N-5.95)/(N+1)N1.2Rmin0.8350.0758583110.57773345915.458798731.3Rmin0.904540.1096012690.5387147414.066598911.4Rmin0.974120.1409843370.50479389813.03456051.5Rmin1.04370.1702304640.4912.627450981.6Rmin1.113

9、280.1975507270.4812.365384621.7Rmin1.182860.2231292890.4611.870370371.8Rmin1.252440.2471275590.4411.410714291.9Rmin1.322020.26968760.42511.086956522Rmin1.39160.2909349390.410.58333333可知：R=2RmirH理論板數(shù)最少xF=0.4677由甲醇-水氣液平衡數(shù)據(jù)可知348.51Kx1=0.4346.31Kx2=0.5即用內(nèi)插法算348.51-346.31T-346.310.4-0.5一0.4677-0.5xF=0.46

10、77時T=347.02K=73.87C即由安托因方程得aF=3.94aD=4.138:m'=F；D=j3.944.138=4.038idxd、/1xf"0.980.5323log()()log(乂即Nmin精=2.883.2.7 _1-xdxf一_0.020.4677log：mlog4.038即精僻段理論板數(shù)為3層加料板為第4塊板:塔效率的估算(1)Drickarner法塔頂溫度64.6C塔釜溫度100C平均溫度為T二空=100一646.355.156K=82C,T2,100273.15lnlnT164.6273.115即82CT甲醇=0.272mpa.s水=0.3485mp

11、a.s即mxfi"=0.46770.272(1-0.4677)0.3485=0.3127mpasET=0.17-0.616lgm=°.17-0.616lg0.3127=0.481(2)Oconnell法卜L=0.4677*0.272+(1-0.4677)*0.3485=0.312782CT的相對揮發(fā)度a為a=3.787Et=0.49(Wl)°245=0.47實際塔板數(shù)為N=旭=21.280.47約為22塊3.3:塔和塔板主要工藝尺寸的設(shè)計3.3.1:塔徑的計算精僻段精僻段平均溫度為Tm=73.87-64.6=342.36k=69.21Cm,73.87273.15l

12、n64.6273.15查t-x-y圖得xa=0.72,ya=0.878查表得：p甲醇=0.75g/cm3p水=0.978g/cm3液相平均分子量：Ml=XaM甲醇+(1-Xa)M水=0.72*32.042+(1-0.72)*18=28.11kg/kmol氣相平均分子量：Mv=yaM甲醇+(1-ya)M水=0.878*32.042+(1-0.878)*18=30.33kg/kmol液相密度：Ml;?LMaXaMbXb?b28.11=0.783g/cm3=783kg/m332.0420.7218(1-0.72)0.9780.75氣相密度一、PMvV-RT_一_51.0131030.33=1079.

13、42g/m3=1.079kg/m38.314342.36液相體積流量36LA1.391640.75228.11-4=5.6610m3/s3600783氣相體積流量VMvVS=36002.391640.75230.33=0.761m3/s36001.079即氣液動能參數(shù)FLVL5.6610783、0.020.7611.079取塔板間距HT=0.45m板上液層高度hl=0.07m那么分離空間：HT-h1=0.45-0.07=0.38m即由史密斯關(guān)聯(lián)圖得：C20=0.078甲醇與水在各溫度下的表面張力溫度(C)60708090100甲醇18.7617.8216.9115.8214.89水66.264

14、.362.660.758.8即69.21C時pa=17.89mN/mb=64.45mN/m液相平均表面張力：Xj%=0.7217.890.2864.45=30.927mN/m02-C=C20().=0.08520C:負(fù)荷系數(shù)A冠.Ln。.0851.079783-1.0792.288m/siimax最大空塔氣速令p=0.7pmax=0.7*2.288=1.6m/s根據(jù)流量公式計算塔徑D4Vs40.761D=、=0.778mV業(yè)V兀x1.6圓整取0.8m塔截面積A=)25=(08)25=0.5m222實際空塔氣速=頭=0761=1.522m/sA0.5提僻段提僻段平均溫度為Tm100-73.87&

15、#39;_100273.15In73.87273.15=359.927K=86.777C查t-x-y圖得xa'=0.111,ya'=0.443查表得：p甲醇=0.728g/cm3p水=0.967g/cm3液相平均分子量：Ml'=Xa'M甲醇+(1-Xa')M水=0.111*32.042+(1-0.111)*18=19.559kg/kmol氣相平均分子量：Mv'=ya'M甲醇+(1-ya')M水=0.443*32.042+(1-0.443)*18=24.221kg/kmol液相密度：MlP|_，=LMaXa.MbXb柘?b19.55

16、932.0420.111.18(1-0.111)0.7280.967=0.913g/cm3=913kg/m3氣相密度PM_一_5_1.0131024.221RT8.314359.927=819.93g/m3=0.82kg/m3液相體積流量L'=L+qFL'xMl(1.391630.752+86.475)婦9.559。仁dn-4=8.510m3/s36003600913氣相體積流量V，=V-(1-q)F=VVMv2.391640.75224.221、=0.8m3/s3600七36000.82即氣液動能參數(shù)F'8.510-49130.0350.80.82取塔板間距HT=0.

17、45m板上液層高度hl=0.07m那么分離空間：HT-h1=0.45-0.07=0.38m即由史密斯關(guān)聯(lián)圖得：C2(T=0.08286.777C時a=16.17mN/mb=61.31mN/m液相平均表面張力：xZ=0.11仆16.17+(1-0.111)x61.31=56.3mN/mC，=0.082(竺3)0.220=0.1=。.1913-0.820.82=3.34m/siimax最大空塔氣速令小'=0.7小ma乂=0.7*3.34=2.34m/s40.8KX2.34根據(jù)流量公式計算塔徑D=0.66m圓整取0.8m塔截面積A'=(D-)25=(08)25=0.5m222實際空塔

18、氣速山=生=Q8=1.6m/sA0.53.3.2:塔高的計算rNt42精=Ht=x0.45=3.83mEt0.47NtetHt0.45=4.787m0.47此外在精僻段和提僻段分別設(shè)2人孔，人孔處板間距為0.7m令塔頂空間為1.5HT=2.5*0.45=1.125m令塔底空間為1.4mL'13.76600.00085Hd=1.4mL'=0.00085m3/s0.5A所以塔局為Z=z精+z提+（0.7-0.45）*4+0.675+2=3.83+4.787+0.5+1.125+1.4=12.642m約為12.7m3.3.3:溢流裝置與液體流型選用單溢流，弓形降液管。因為弓形降液管具

19、有較大容積，乂能充分利用塔面積，且單溢流液體流徑長，塔板效率高，結(jié)構(gòu)簡單，廣泛用丁直徑小丁2.2米的塔中。溢口堰(出口堰)為維持塔板上一定高度的均勻流動的液層，一般采用平直溢流堰。(1) 堰長取堰長lw=0.6D=0.8*0.6=0.48m(2) 堰上液層高度how平直堰的how精僻段Lh=5.66*10A-4*3600=2.0376m3/h即（項）25=（冬嚴(yán)=37.13lw0.48Lw/D=0.48/0.8=0.6查液流收縮系數(shù)計算圖得所以how2.84匚戶嚴(yán)1000lwE=1.082.84,2.0376、2/33x1.08尺（）=8.04x10m10000.48提僻段Lh'=8.

20、5*10A-4*3600=3.06m3/h即（W）2.5=（3°6）2.5E02.61lw0.48Lw/D=0.48/0.8=0.6查液流收縮系數(shù)計算圖得E'=1.22.84Lh'2/32.84J.21322/3.3所以how=E()=x1.2x()=6.3210m1000lw10000.48堰高h(yuǎn)whw=hL-how=0.07-8.04*10A-3=0.062m取0.07m提僻段hw'=hL-how'=0.07-6.32*10A-3=0.064取0.07m所以：hl=hw+how=0.07+8.04*10A-3=0.078mhl'=hW+ho

21、w'=0.07+6.32*10A-3=0.076m修正后hL對in影響不大，顧塔徑計算不用修正.3.3.3.2降液管降液管的寬度Wc西截面積Af由lw/D=0.6查弓形降液管的寬度與面積關(guān)聯(lián)圖可得WAf-=0.098-=0.052DA所以Wd=0.098<0.8=0.0784m二22Af=0.0520.82=0.026m24液體在降液管內(nèi)的停留時間精僻段LS0.0260.45er=20.67s5.6610一提僻段.，=3Ls'0.0260.45=13.76s8.510降液管底隙高度h0因物系較活潔，不會有臟物堵塞降液管底隙，取液體通過降液管底隙速度0=0.08m/s精僻段

22、h0=5.6610=0.015m過小，取0.02mlw甲。0.48X0.08hw-h0=0.07-0.02=0.05m>0.006m提僻段,Ls'8.510-4ch0=0.022mlwV。0.48X0.08hw'-h0=0.07-0.022=0.048m>0.006m故降液管底隙高度設(shè)計合理3.3.3.3受液盤及進(jìn)口堰選用平形受液盤。不設(shè)進(jìn)口堰。3.3.4:塔板設(shè)計:塔板布置開孔區(qū)(鼓泡區(qū))面積Aa計算取邊緣區(qū)寬度Wc=0.05mx=(D/2)-(Wd+Wc)=0.4-(0.0784+0.05)=0.2716mR=(D/2)-Wc=0.4-0.05=0.35m即A,

23、=2xR2-x2R2sin(x/R)=20.2716.0.352-0.271620.352sin(0.2716/0.35)=0.338m2_180_180溢流區(qū)溢流區(qū)面積Af及Af'分別為降液管和受液盤所占面積安定區(qū)(破沫區(qū))取溢流堰前的安定區(qū)寬度為Ws=0.07m取進(jìn)口堰后的安定區(qū)為WS=0.05m無效區(qū)取無效區(qū)寬度為0.03m3.3.4.2:篩板的篩孔與開孔率孔徑d0本設(shè)計所處理的物系無腐蝕性，可選用碳鋼板，取篩孔直徑d0=5mm篩板厚度取a=0.8d0=4mm孔心距t篩孔在篩板上按正三角形排歹0,取孔心距t=3d0=15mm開孔率小9=&=0.907(業(yè))2=0.907(

24、5)2=10.1%Aat15篩孔數(shù)11581031158103、nooo人n=(2)Aa=(2)X0.338=1740個t153.3.5篩板的流體力學(xué)驗算:塔板壓降Pp氣體通過篩板的壓降Pp以相當(dāng)?shù)囊褐叨缺硎緯r可由下式計算：hp=hc+hl+ho-hp:氣體通過每層塔板壓降相當(dāng)?shù)囊褐叨?，m(1)干板阻力hc的計算精僻段篩孔氣速0=VsA00.7610.00521740一.（）22=22.27m/sd0/a=5/4=1.25查干篩孔的流量系數(shù)圖可知流量系數(shù)22.2721.079八八）=0.049mC0=0.84C0即he=0.051（土）2（衛(wèi)）=0.051（0.84783提僻段.Vc

25、9;篩孔氣速U=VsA00.8=23.416m/s0.005、21740:（）2C0=0.84即he'=0.051（%）2（但）=0.051（23.416）2（082）=0.036mC0J0.84913（2）氣體通過液層阻力hl的計算精僻段按有效流通面積計算的氣速七VsAt-Af0.761-：（°8）2-0.0262=1.597m/sFa=%_飛;=1.5971.079=1.659查找充氣系數(shù)e0與Fa的關(guān)聯(lián)圖可知：£0=0.58即hl=£0hL=s0（hw+how）=0.58*0.078=0.045m提僻段.，Vs0.8a=S=1.678m/sAt二（箜

26、）2-0.0262Fa'='=1.678,0.82=1.519查找充氣系數(shù)c0與Fa的關(guān)聯(lián)圖可知：£0'=0.6即hl'=£0'hL=£0'(hw'+hoW)=0.6*0.076=0.0456m液體表面張力的阻力h(r的計算精僻段4。h；=gd。=0.0032m430.92710$7839.820.005提僻段h。'口4：':L'gcb456.310-9139.820.005=0.005m即精僻段板壓降hp=hc+hl+hb=0.049+0.045+0.0032=0.0972mPp=h

27、ppLg=0.0972*783*9.82=747.38pa=0.747kpa提僻段板壓降hp'=hc'+hl'+hb'=0.036+0.0456+0.005=0.0866mPp=hppLg=0.0866*913*9.82=776.43pa=0.776kpa3.3.5.2:霧沫夾帶量ev的計算精僻段5"10'。HT-hf5.7尺10630.92710'1.597)3.20.45-2.50.078=0.065kg液/kg氣提僻段5.710-6了，3.25.710-61.6783.2Ht-hf56.3100.45-2.50.0760.0395

28、kg液/kg氣故本設(shè)計液沫夾帶量在允許范圍ev<0.1kg液/kg氣內(nèi)，所以符合要求。3.3.5.3:漏液點氣速ow的計算精僻段5w=4.4Co/(0.0056+0.13hLhgPL/Pv=4.4X0.840.0056+0.13/0.078-0.0032)783/1.079=11.149m/s穩(wěn)定性系數(shù)K2227所以無明顯漏液現(xiàn)象2227=1.9971.52.0ow11.149提僻段Pow'=4.4Coj'(0.0056+0.13hL'-hQPL'/Pv'=4.0.84J(0.0056+0.13><0.076-0.005)913/0.8

29、2=12.625m/s穩(wěn)定性系數(shù)K總23416K'=仁=芝也6=1.855>1.52.0所以無明顯漏液現(xiàn)象ow12.6253.3.5.4:液泛（淹塔）條件的校核降液管內(nèi)的活液層高度Hd的計算精僻段液體流過降液管的壓強(qiáng)降相當(dāng)?shù)囊褐叨萮d的計算hd=0.153(lw*hg2)2=0.153(5.66100.480.02)2=5.31810mHd<即Hd=hp+hL+hd=0.0972+0.078+5.318*10A-4=0.1757m4(HT+hw)=0.5(0.45+0.07)=0.264(HT+hw)=0.26提僻段=9.9110-mLs28.510-2hd'=0

30、.153()2=0.153()2lw也0.480.022即Hd=hp'+hL'+hd'=0.088+0.076+9.91*10A-4=0.165m4(HT+hW)=0.5(0.45+0.07)=0.26Hd<4(HT+hw)=0.26所以不會產(chǎn)生液泛3.3.6塔板負(fù)荷性能圖3.3.6.1霧沫夾帶線(1)精僻段取極限值ev=0.1kg液/kg氣5.710-6%ev=_3Ht-hf30.927105.710Vs0.477)3.20.45-hf=0.1kg液/kg氣hf=2.5(hw+how)=2.5(0.07+284乂1.08乂(3600Ls)2/3)=0.175+2

31、.938LsA2/310000.48Vs整理得0.1=1.96910-3(S)320.275-2.938LSVs=0.938-10.024LsA2/3在操作范圍中，任取幾個Ls值，根據(jù)上式算出Vs值列丁下表中:Ls(m3/s)0.00050.00150.0020.0045Vs(m3/S)0.8750.8070.7790.665提僻段Vs',5.710°ev-4=5.*101(E,)3.2=0.1kg液/kg氣Ht-hf56.3100.45-hfhf'=2.5(hw'+hoW)=2.5(0.07+84勺.2x(3600Ls)2/3)=0.175+3.264Ls&

32、#39;八2/310000.48整理得-3S.3.20.1=1.0810()0.275-3.264LsVs=1.132-13.437Ls'八2/3在操作范圍中，任取幾個Ls'值，根據(jù)上式算出Vs'值列丁下表中:Ls(m3/S)0.00050.00150.0020.0045Vs(m3/s)1.0470.9560.9190.7663.3.6.2:液泛線(2)精僻段由式hp=hc+hl+hbHd=hp+hL+hdhd=0.153"')2Hd=(|)(HT+hw)VsVso23hc=0.051()2(工)C0LA0、2/1.0792,1.0792=0.051(

33、)()=0.051(0.034)()=0.086Vs0.847830.84783hl=£0hL=e0(hw+how)=0.58*(hw+how)=0.58*(0.07+2841.08(3600Ls)2/3)=0.0406+0.682LsA2Z310000.48故hp=0.086VsA2+0.0406+0.682LsA2/3+0.0032=0.0438+0.086VsA2+0.682LsA2/3Ls2/Ls22hd-0.153()=0.153()-1660.156Lslw*h/0.480.02Hd=0.0438+0.086VsA2+0.682LsA2/3+0.078+1660.156L

34、sA2=0.1218+0.086VsA2+0.682LsA2/3+1660.156LsA24(HT+hw)=0.5(0.45+0.07)=0.26即0.26=0.1218+0.086VsA2+0.682LsA2/3+1660.156LsA2整理得：VsA2=1.607-7.93LsA2/3-19304.14LsA2任取幾個Ls值(2-18)式計算Vs值，見下，作出液泛線(2)Ls(m3/s)0.00050.00150.0020.0045Vs(m3/s)1.2461.2081.1851提僻段Vs'hc'=0.051(&)2(立)=0.051(0034)2(082)=0.0

35、56W2C°L'0.84913hl=£0hL=e0(hw+how)=0.6*(hw+how)=0.6*(0.07+2841.2(3600Ls)2/3)=0.042+0.783LsA2/310000.48故hp'=0.056Vs'A2+0.042+0.783LsA2/3+0.005=0.047+0.056Vs'a2+0.783LsA2/3Ls2Ls22hd'=0.153()=0.153(-)=1372.03Lslw，h°0.480.022Hd'=0.047+0.056Vs'A2+0.783LsA2/3+1372

36、.03LsA2+0.076=0.123+0.056V，A2+0.783LsA2/3+1372.03LsA24(HT'+hw')=0.5(0.45+0.07)=0.26即0.26=0.123+0.056Vs'A2+0.783LsA2/3+1372.03LsA2整理得：Vs'A2=2.446-13.98LsA2/3-24500.54LsA2任取幾個Ls'值計算Vs'值，見下，作出液泛線(2)Ls(m3/s)0.00050.00150.0020.0045Vs(m3/s)1.5341.4861.4581.2533.3.6.3:液相上限線(3)以r=3s作

37、為液體在降液管中停留的下限Ls.maxH=0045=3.910*/s33在Ls.max=0.0039m3/s處作出垂線得液相負(fù)荷上限線3.3.6.4:漏液線(氣相負(fù)荷下限線)(4精僻段巳w=44COt'(0.0056+0.13hLhQPL/Pv=4.4x0.84j(0.0056+0.13xhL-0.0032)783/1.079=3.6961.742+94.337hL284z3600LqhL=0.07+84勺.08x(S)2/3=0.07+1.175LsA2/310000.48=Vs.mn=3.696.1.74294.337(0.071.175LS2/3)A。A0=0.034m2即2/3

38、一2/3Vs.min=0.034尺3.696丫1.742+94.337(0.07+1.175LS)=0.126寸'8.346+110.846LS據(jù)上式，取若干個Ls值計算相應(yīng)Vs值，見下表，作漏液線Ls,m3/s0.00050.00150.0020.0045Vs,m3Js0.3790.3940.4010.425提僻段y'=4.4CoJ(0.0056十0.13"'/心')什'/町=4.4乂0.84J(0.0056十0.13乂hL'-0.005913/0.82=3.696'0.668十144.74確'hL'=0.07

39、+84勺.2乂(3600Ls)2/3=0.07+1.306Ls'八2/310000.48ow'=VS.皿=3.696(0.668+144.74(0.07+1.306LS'2/3)=3.696(10.8+189hL'AoA0=0.034m2即：Vmn=0.1257'10.8+189Ls'2/3據(jù)上式，取若干個Ls'值計算相應(yīng)Vs'值，見下表，作漏液線Ls,m3/s0.00050.00150.0020.0045Vs,m3/s0.4350.4580.4670.5023.3.6.5:液相負(fù)荷下限線（5）取堰上液層高度最小允許值how=0.

40、006m精僻段.33600Lsmin2/3-3,3600Lsmin2/3how=0.006=2.8410E()=2.84101.08()Iw0.48整理得Ls.min=3.65*10J4m3/s提僻段how=0.006=2.8410'E(3600Ls.min)2/3=2.8410-31.2(3600Lsmin)2/3Iw0.48整理得Ls.min'=3.11*10A-4m3/s3.3.6.6:塔的操作彈性畫圖看精僻段OP為操作線，OP與液泛線的交點對應(yīng)氣相負(fù)荷為Vs.max,與漏夜線的交點對應(yīng)氣相負(fù)荷為Vs.min可知：操作彈性=史工=坦=3.1>3符合要求Vs.min0

41、.4提僻段操作彈性=史號=148=3.36>3符合要求Vs.min0.44負(fù)荷性能圖精偕1.6、：L操作線-霧沫夾帶線液泛線T漏液線一液相上限線-一液相負(fù)荷下限線提僻Ls操作線-霧沫夾帶線液泛線昨漏液線T1液相上限線-液相負(fù)荷下限線3.4:板式塔的結(jié)構(gòu)與附屆設(shè)備:塔板結(jié)構(gòu)由丁本設(shè)計塔徑為0.8m,即選用整塊式結(jié)構(gòu):冷凝器的選擇本設(shè)計取傳熱系數(shù)K=2000w/m2.C出料液溫度64.6-64.6C冷卻水溫度35-20C逆流操作：t1=44.6Ct2=29.6C冷凝蒸汽量G1二VMv36002.391640.75230.3336001.079=0.821kg/s由丁甲醇的摩爾分?jǐn)?shù)為0.98，所以忽略水的冷凝熱。r=1100.18KJ/kgQ=G1*r=1100.18*0.821=903.38kw水的比熱容為Cp=4.1862KJ/kg.K則水的冷卻用量為G2QCp.：t903.384.186215=14.387kg/s平均溫度差為扁=芒土任=312.5K=39.35Cm,t10.048ln：t23Q903.3