雙組分連續(xù)精餾篩板塔的設計

....遼寧科技大學課程設計說明書設計題目： 化工原理課程設計雙組分連續(xù)精餾篩板塔的設學院、系： 化學工程學院專業(yè)班級： 應化13-1學生姓名：指導教師成 績2016年 7月 8日目 錄一．序… 2二．原始數(shù)據(jù)… 3三．設計計算… 3四．物料衡算… 3五．塔頂溫度、塔底溫度及最小回流比計算… 4六．確定最佳操作回流比及塔板層數(shù)… 5七．塔板結(jié)構(gòu)計算… 10八．溢流堰高度及堰上液層高度的確定… 12九．板面篩孔布置的設計… 12十．水力學性能參數(shù)及校核… 13十一．塔板負荷性能圖… 14十二．篩板設計計算的主要結(jié)果：… 17十三．主要符號說明（略）… 18十四.十五十六

主要參考文獻… 18雙組分連續(xù)精餾的流程圖… 19結(jié)束語… 20序相物系,非均相物系的分離主要依靠質(zhì)點運動與流體流動原理實現(xiàn)分離,而化學工業(yè)中通常遇到的是均相分離,通常有精餾，吸收，萃取和干燥等單元的操作。精餾是分離液體混合物（含可液化的氣體混合物）最常用的一種典型單元操作，在化工、煉油、石油化工等工業(yè)中得到廣泛應用。按蒸餾方式分為簡單蒸餾，平衡蒸餾，精餾和特殊精餾等。當混合物各組分揮發(fā)度差別很小或形成共沸時，采用精餾。精餾是多級分離過程,即同時進行多次部分汽化和部分冷凝的過程,因此可使混合液得到幾乎完全的分離。工（有時加質(zhì)量劑本次設計任務為設計一定產(chǎn)品純度的精餾塔，實現(xiàn)二甲苯－三甲苯同時對篩板塔的結(jié)構(gòu)，性能做了較充分的研究，認識到只要設計合理，操本設計的具體流程：原料液（二甲苯和三甲苯，且泡點進料）經(jīng)預熱器加熱到指定的溫度后，送入塔的進料板上與自塔上部下降的回流液體匯本課程設計的主要內(nèi)容是過程的物料衡算、熱量衡算，工藝計算，結(jié)構(gòu)設計和校核。20167化工原理課程設計Ⅰ.原始數(shù)據(jù)1.設計題目：雙組分連續(xù)精餾篩板塔的設計2.原料處理量：1.6×104kg/h原料組成：組分名稱組分名稱組成（質(zhì)量分率）0.440.56（10.975（質(zhì)量分率。（20.965（質(zhì)量分率。（1：操作壓力：常壓。（2：進料及回流狀態(tài)：泡點液體。Ⅱ.設計計算一、 物料衡算二甲苯的摩爾質(zhì)量：M=106kg/kmolA三甲苯的摩爾質(zhì)量：M=120kg/kmolB原料液摩爾分率： x F塔頂產(chǎn)品摩爾分率： x D

0.47080.44/1060.44/1060.44/1060.44/106(10.44)1200.975/1060.975/106(10.975)120原料液的平均摩爾質(zhì)量：M=0.4708×106＋(1－0.4708)×120＝113.4088kg/kmol物料衡算原料處理量：FDX

16000 141.08kmol/h113.4088塔頂易揮發(fā)組分回收率：

D 0.965FXF∴D=65.54kmol/h總物料衡算：FDW ∴WFD＝141.08－65.54＝75.54kmol/hFx DxF D

WxW

141.08×0.4708＝65.54×0.9779＋75.54×xW∴x =0.03083W二、 塔頂溫度、塔底溫度及最小回流比的計算確定操作壓力：塔頂壓力：760mmHg塔底壓力：760mmHg+25×100/13.6mmHg=943.8235mmHg計算塔頂溫度（露點溫度：根據(jù)塔頂壓力及塔頂汽相組成用試差法計算塔頂溫度。其中二甲苯、三甲苯的飽和蒸氣壓由安托因方程計算。設t頂=141.49℃由lgPA由lgPB

7.0007.074

1463t 214.7頂1608t 頂

P=781.1904mmHgAP=348.2324mmHgBP0 781.1904 P0 348.2324k A 1.02788 k B 0.45820A P 760 B P 760x yAA kA

0.97790.951374 x1.02788

BykyB

0.97790.45820

0.048232 x10.9513740.04823210.000394=0.0004it頂=141.5℃假設正確，為所求露點溫度。P0781.1904A頂P0348.2324∴ 2.2433B計算塔底溫度（泡點溫度）根據(jù)塔底壓力及塔底殘液組成用試差法計算塔底溫度。其中二甲苯、三甲苯的飽和蒸氣壓由安托因方程計算。底設t =177.67℃底由lgPA由lgPB

7.0007.074

1463t 底1608t 213.3底

P=1867.9984mmHgAP=914.4342mmHgBP0 1867.9984 P0 914.4342K A 1.9792 K B 0.9689A P 943.8235 B P 943.8235Y X KA A

0.030831.97920.0610Y XKB B

(10.03083)1.97920.9559 y10.04430.955910.0002=0.0004i底t =177.67℃假設正確，為所求泡點溫度。底A∴ 底 BA

1867.99842.0248914.4342底頂2.24242.0248∴ 底頂2.24242.0248Rmin：q1 x

0.4708

0.6556e F ee 11xex y 0.97790.6556DeR Demin

yx

1.74400.65560.4708e e三、 確定最佳操作回流比與塔板層數(shù)y ynXnn列操作線方程：

yn

2.13131.1313yn

n1

R xR1

DxR1xLF W

x xm1

LD m LD w由塔頂向下逐板計算精餾段的汽、液相組成，即y=xxy1 D 1 2xxx≤xn-1n n F由進料口向下逐板計算提餾段的汽、液相組成，即x=xyx1 n 2 2yxx≤xZmm m w逐板法計算塔板層數(shù)：R=(1.1-2.0)Rmin0.1Rmin，具體計算結(jié)果如下表：1)R=1.1Rmin精餾段：y =0.6573x+0.3351n1 n2)提餾段：y =1.3873x -0.0086.m1 m3)精餾段（包含加料板：n=1y=0.9779 x=0.9539n=2y=0.9621x=0.9223n=3y=0.9414x=0.8824n=4y=0.9152x=0.8345n=5y=0.8837x=0.7803n=6y=0.8481x=0.7229n=7y=0.8104x=0.6664n=8y=0.7733x=0.6145n=9y=0.7392x=0.5698n=10y=0.7098x=0.5334n=11y=0.6859x=0.5051n=12y=0.6674x=0.4839n=13y=0.6534x=0.4683提餾段提餾段（包含釜：m=0 x=0.4708m=1y=0.6448 x=0.459m=2y=0.6284 x=0.4414m=3y=0.6038 x=0.4159m=4y=0.5682 x=0.3808m=5y=0.5192 x=0.3354m=6y=0.4559 x=0.2814m=7y=0.3805 x=0.223m=8y=0.299 x=0.1662m=9y=0.2197m=10y=0.1501m=11y=0.0941m=12y=0.0524NT=24（包括釜）

=12N精

=12（包括釜）4)R=1.2Rmin yn1=0.6767xn+0.3162提餾段：y =1.3655x -0.0081m1 m精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9617x=0.9215n=3y=0.9398x=0.8794n=4y=0.9113x=0.8276n=5y=0.8763x=0.768n=6y=0.836x=0.7043n=7y=0.7929x=0.6415n=8y=0.7504x=0.5842n=9y=0.7117x=0.5357n=10y=0.6789 x=0.497n=11y=0.6527 提餾段（包含釜：m=0x=0.4708m=1y=0.635m=2y=0.6043m=3y=0.5603m=4y=0.501m=5y=0.427m=6y=0.3432m=7y=0.2581m=8y=0.1805m=9y=0.1166m=10y=0.0683m=11y=0.0339NT=21（包括釜）

=10N精

=11（包括釜）5)R=1.3Rmin 精餾段：y =0.6939x+0.2993n1 n提餾段：y =1.3460x -0.0077m1 m精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9613x=0.9207n=3y=0.9382x=0.8765n=4y=0.9076x=0.8211n=5y=0.8692x=0.7564n=6y=0.8243x=0.6867n=7y=0.776x=0.6181n=8y=0.7284x=0.5562n=9y=0.6855x=0.5046n=10y=0.6497 x=0.4643提餾段（包含釜：m=0x=0.4708m=1y=0.6263x=0.4392m=2y=0.5835x=0.3956m=3y=0.5245x=0.3401m=4y=0.4494x=0.2761m=5y=0.3628x=0.2101m=6y=0.2734x=0.1495m=7y=0.1914x=0.0996m=8y=0.1239x=0.062m=9y=0.073x=0.0355m=10y=0.0372 x=0.0177N =19（包括釜）N =9N =10（包括釜）T 精 提6)R=1.4Rmin 精餾段：y =0.7094x+0.2841n1 n提餾段：y =1.3284x -0.0073m1 m精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9609x=0.9199n=3y=0.9368x=0.8738n=4y=0.9041x=0.815n=5y=0.8624x=0.7455n=6y=0.8131x=0.6703n=7y=0.7598x=0.5965n=8y=0.7075x=0.5306n=9y=0.6608x=0.4765n=10y=0.6224 x=0.4351提餾段（包含釜：m=0x=0.4708m=1y=0.6184x=0.4309m=2y=0.5651x=0.3778m=3y=0.4942x=0.3135m=4y=0.4083x=0.2438m=5y=0.3152x=0.177m=6y=0.226x=0.1201m=7y=0.15x=0.0762m=8y=0.0914x=0.0449m=9y=0.0496x=0.0238NT=18（包括釜）N精=9N提=9（包括釜）7)R=1.5Rmin yn1=0.7235xn+0.2704提餾段：y =1.3126x -0.0069m1 mn=1y=0.9779x=0.9539n=2n=1y=0.9779x=0.9539n=2y=0.9605x=0.9191n=3y=0.9354x=0.8712n=4y=0.9008x=0.8093n=5y=0.856x=0.7353n=6y=0.8025x=0.655n=7y=0.7444x=0.5764n=8y=0.6876x=0.507n=9y=0.6374x=0.451餾段（包含釜：m=0x=0.4708m=1y=0.6113 x=0.4236m=2y=0.549x=0.3626m=3y=0.4685x=0.2917m=4y=0.375x=0.219m=5y=0.2791x=0.1532m=6y=0.1923x=0.1001m=7y=0.1222x=0.0611m=8y=0.0708x=0.0344m=9y=0.0355x=0.0169提NT=17（包括釜）

=8N精

=9（包括釜）8)R=1.6Rmin yn1=0.7362xn+0.2580ym1=1.2982xm-0.0066精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9602x=0.9185n=3y=0.9342x=0.869n=4y=0.8978x=0.8041n=5y=0.85x=0.7259n=6y=0.7925x=0.6409n=7y=0.73x=0.5582n=8y=0.6691x=0.4858n=9y=0.6158x=0.4282提餾段（包含釜：m=0x=0.4708m=1y=0.6048x=0.417m=2y=0.5346x=0.3493m=3y=0.4463x=0.2736m=4y=0.3475x=0.1993m=5y=0.2506x=0.1351m=6y=0.1669x=0.0856m=7y=0.1023x=0.0506m=8y=0.0566x=0.0273N=16（包括釜）N =8N =8（包括釜）精 提9)R=1.7Rmin 精餾段：y =0.7479x+0.2466n1 n提餾段：y =1.28951x -0.0063m1 m精餾段（包含加料板：n=1y=0.9779 x=0.9539n=2y=0.96x=0.9181n=3y=0.9332x=0.8672n=4y=0.8952x=0.7997n=5y=0.8447x=0.7176n=6y=0.7834x=0.6283n=7y=0.7166x=0.5416n=8y=0.6518x=0.4666提餾段（包含釜：m=0x=0.4708m=1y=0.5989x=0.411m=2y=0.5217x=0.3376m=3y=0.4269x=0.2582m=4y=0.3244x=0.1833m=5y=0.2277x=0.1211m=6y=0.1474x=0.0747m=7y=0.0875x=0.0429m=8y=0.0464x=0.0222NT=15（包括釜）N精=7 N提=8（包括釜）10)R=1.8Rmin yn1=0.7584xn+0.2363ym1=1.2731xm-0.0061精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9597x=0.9175n=3y=0.9321x=0.8651n=4y=0.8924x=0.7949n=5y=0.8392x=0.7092n=6y=0.7742x=0.6157n=7y=0.7034x=0.5257n=8y=0.6351提餾段（包含釜：x=0.4485m=0x=0.4708m=1y=0.5935x=0.4056m=2y=0.5101x=0.3273m=3y=0.41x=0.2451m=4y=0.3049x=0.1701m=5y=0.2089x=0.1098m=6y=0.1318x=0.0662m=7y=0.0761x=0.0371m=8y=0.0388x=0.0185N =15（包括釜）N =7N =8（包括釜）T 精 提11)R=1.9Rmin 精餾段：y =0.7682x+0.2267n1 n提餾段：y =1.2620x -0.0058m1 m精餾段（包含加料板：n=1y=0.9779x=0.9539n=2y=0.9595x=0.9172n=3y=0.9313x=0.8637n=4y=0.8902x=0.7912n=5y=0.8346x=0.7022n=6y=0.7662x=0.605n=7y=0.6916x=0.5117n=8y=0.62x=0.4326提餾段（包含釜：m=0x=0.4708m=1y=0.5886x=0.4007m=2y=0.4997x=0.3182m=3y=0.3951x=0.2338m=4y=0.2881x=0.159m=5y=0.1933x=0.1007m=6y=0.1194x=0.0596m=7y=0.0673x=0.0326m=8y=0.0331x=0.0157NT=15（包括釜）N精=7N提=8（包括釜）12)R=2.0Rmin yn1=0.7772xn+0.2179ym1=1.2519xm-0.0056精餾段（包含加料板：n=1y=0.9779 x=0.9539n=2y=0.9593x=0.9168n=3y=0.9304x=0.862n=4y=0.8879x=0.7873n=5y=0.8298x=0.695n=6y=0.7581x=0.5942n=7y=0.6798x=0.498n=8y=0.6051x=0.4173提餾段（包含釜：m=0x=0.4708m=1y=0.584 x=0.3961m=2y=0.4901x=0.3099m=3y=0.3817x=0.2239m=4y=0.2736x=0.1497m=5y=0.1803x=0.0932m=6y=0.1092x=0.0542m=7y=0.0602x=0.0291NT=14（包括釜）對上表塔板數(shù)列表：

=7精

=7（包括釜）提R=nRmin1.11.21.31.41.51.61.71.81.92.0精餾段121099887777提餾段1211109988887N(含釜)24211918171615151514R-NT本題取回流比 R——1.6R1.6Rmin

1.61.74402.7904N =16（包括釜）T

=8精

=8（包括釜）提查取塔板效率：t tt底t頂

178.04141.5178.04

159.07℃lnt底頂

ln141.5 A 20

()(t20)0.6870.0042(159.0720)0.1029t B

()(t20)0.8390.004200.2827t x

0.47080.10290.28270.1981L i iE T

0.2450.492.13980.1980.2450.6047L計算全塔理論板數(shù)：N 17N TP 1.1ET

24.12 251.10.6047四、 塔板結(jié)構(gòu)計算（設計塔頂?shù)谝粔K板）計算塔頂實際的汽液相體積流量：（1）液相體積流量計算： A 20

(t)(t20)864-0.875×(141.49-20)=757.6875kg/m3 B

(t)(t20)878-0.707×(141.49-20)=792.0995kg/m3xx D

0.9779 0.9539

10.95390.0461A

1xD

2.13981.13980.9779 BAAx xxM AA

0.9539106 0.9481WA xMA A B

0.95391060.0461120x 10.94810.0519WBA1 (xA

)'(xBB

)'

0.9539 0.0461757.6875 792.0995L A B∴L759.2092 kg/m3ML0.95391060.0461120106.6454 kg/kmolVLRDML/L2.790460.0161106.6454/759.209223.5242m3/h（2）汽相體積流量計算：PM AA RT

1013251068.314273.15141.53.115 kg/m3PM BB RT

1013251208.314273.15141.53.527 kg/m3 0.97793.1150.02213.5273.1251 kg/mVM =0.9779×106＋(1－0.9779)×120＝106.3094kg/kmolGV (R1)DM/G

(2.79041)60.0161106.6454/3.12517763.0257m3/h選取塔板間距H ：T選取塔板間距HT

＝0.45m HT

＝0.7mC：VVLG

23.5242 7763.0257LV759.2092LV759.20923.1251L

=0.05m，HT

-h=0.45-0.05=0.40mL查史密斯關聯(lián)圖，查得汽相負荷參數(shù)C 0.08420液體表面張力的計算： A 20 B 20

()(t20)28.99-0.109(141.5-20)=15.7465dyne/cmt()(t20)28.93-0.101(141.5-20)=16.6585dyne/cmtx 15.74650.9779+16.6585(1-0.9779)=15.7667yne/cmi iiCC20

()0.220

0.08415.7667 20 20

0.0801計算液泛速度u (u )：F maxLVVF

0.0801 1.2459km/s759.2092759.20923.12513.12510.7，則空塔氣速uG=0.7uF=0.71.2459=0.8721m/s選取溢流方式及堰長同塔徑的比值lw/D:選用單溢流弓形降液管，取lw

/D=0.7。查弓形降液管的參數(shù)圖，查取降液管面積同塔截面積的比值AAd T

0.088及降液管寬度同塔徑的比值W /D=0.14。d計算塔徑:V 7763.0257/3600A GG

0.8721

2.4726m2截塔面積：A T塔徑：D

G1AAfA4A4AT42.7112

/ 2.47260.088ATA1.8609m

2.7112m2按標準塔徑圓整后D=1.9m計算塔徑圓整后的實際氣速:A D2T 4

1.822.8353m24A AG

(1Ad

A)2.83530.088)2.5858m2Tu

7763.0257/3600

0.8341m/sG A 2.5853Gu 0.8721液泛分率：GuF

1.2459

0.7000m/s 在（0.6～0.8）范圍內(nèi)D=1.9m堰長：lw

0.7D0.71.81.33m降液管寬度：Wd

=0.14D=0.141.8=0.266m降液管面積：Ad

0.088AT

0.0882.83530.2495m2五.溢流堰高度hw

及堰上液層高度how

的確定選取溢流堰高度hw

=50mm,lw

/D=0.7查取液流收縮系數(shù)圖，得液流收縮系數(shù)E=1.020選用平直堰，堰上液層高度h

L 23Lh

0.00281.02020.082221.020

0.0174m

oww 1.33 ∴h=hL w

+h =0.05+0.0174=67.4mow六.板面篩孔布置的設計：d=5mm，o孔中心距孔徑=3,t=3d=3×5=15mm0選塔板厚度t =3.5mm（碳鋼板。pA：aA=Aa T

－2Ad

=2.8353－2×0.2495＝2.3363m2開孔率：A d 2

12=o=0.907 o=0.907× =0.1008=10.08%Aa

t

3A=Amso ms

=0.1008×2.3363=0.2354m25.氣體通過篩孔的流速：U =o

7763.0257/3600= 0.2354

=9.1606o6.N=Ao

0.2354=

Ao=11990個 d2 0.00524 o 4七． 學性能參數(shù)計算及校核液沫夾帶分率的檢驗：0.057

0.057 0.8341 eG H h 15.7667 0.452.50.0674G = =0.0107kg液/kg氣2.5hT w ow＜0.1kg液/kg氣故在本設計液沫夾帶量eG

在允許范圍內(nèi)。塔板壓降：干板壓降：查表得孔流系數(shù)c=0.7901U 2 1h o V=

9.16062

3.1251 0.0282mo 2g C 2o L

0.79

759.2092對單溢流板：查充氣系數(shù)關聯(lián)圖，得充氣系數(shù)=0.61。h L

h =0.61×0.0674=0.0411mow液層表面張力壓降:h

4103

410315.7667

0.0017mgdL

759.20929.80.005單板總壓降:Hh ho L

h =0.0282+0.0411+0.0017=0.0710m液面落差的校驗：對于篩板塔，液面落差很小,本設計塔徑和液流量均不大，可忽略液面落差影響。塔板漏液狀況的校驗:產(chǎn)生漏液的干板壓降h'0.0051o

h =0.00510.050.06740.0085mow工作狀態(tài)下u

h 12 0.028212穩(wěn)定系數(shù)k=ou'

ho'

= 0.0085

1.8214>1.5 o o故不會產(chǎn)生嚴重漏液。降液管液泛情況的校驗：選取降液管下緣至下層塔板的距離h0

=20mm：則降液管下緣縫隙通道的截面積A =hda

l =0.02×1.33=0.0266m2w液體流出降液管的阻力損失h： 0086 1.39 Vh (

) 1.39 23.5242/360022d g A2da

9.8 0.0266 H'：dDlb W2

h 2.5(hf

h )0.1685mOWZD2WW

1.820.2661.268mH=h h 0.0282+0.0411=0.0699mt 0 L0.0476

(b4h)2vf l l

0.00002456m(bh)3f lH =Hd t

+h+hw

++hd=0.0699+0.05+0.0174+0.00002456+0.0086＝0.1459m二甲苯—三甲苯物系屬一般物系，取=0.5，則H'Hdd 校核：

=0.14590.5

0.2918mH +hT w

=0.45+0.05=0.5m ∴H'H hd T w故在本設計中不會發(fā)生液泛現(xiàn)象。液體在降液管內(nèi)停留時間的校驗：AH3600AH d VL

36000.16640.295423.5242

7.5223s>5s故降液管設計合理。八.塔板負荷性能圖(一) 負荷性能圖：最大氣相負荷線: 2 V 8812

13.2H

2.5h 0.0028F

V L

3G G

w w L w

2 =88122.585815.766713.20.450.050.00281.02

L 1.33 23=17532.6185-318.487023Lh10510h105101520253016601.35617532.6185 916054.332815595.516215185.986214809.592914457.6603V /m316601.35617532.6185 916054.332815595.516215185.986214809.592914457.6603G最大液相負荷線:m3h以m3hAH33600V d 33600L

0.16640.295458.985473/3600最小液相負荷線: 6

6 32LV 2.8F Lw

l = w 2.8x1.020

1.33=4.0499m3h最小氣相負荷線:0.5

2 0.5V

L

A0.0056h

V L

3h G o o

w wl V =

w 759.20920.5

V 3

0.52 159460.79 0.23540.00560.130.050.00281.02 L 0.00172 3.1251 1.33 0.01040.01040.00030699VL23V V /m3h1L051015202530V /m3/hG4713.5784913.300625020.82505126.09485208.77915269.94115350.4028l A 降液管液泛線:l A 0.5

V 2 V 0.5 L V 15946C A 0.5H (0.5 L G o o T V

)0.0028F( L)30.142( L )2w 3600w da0.5 L0.50.45(0.50.050.00281.02(V0.5 L759.2092

0.5)23159460.790.2354

1.33 3.1251 V 0.142(3600L )2 0.0282 0.16950.16950.003802V230.00001378V2LLV V /m3h1L051015202530VG/m3/h19029.13018372.26117930.91017496.74117045.25616562.14516037.8930805345根據(jù)以上各線方程，可作出篩板的負荷性能圖。（如圖）250002000015000100005000

1系列2系列系列系列00 10 20 30 40 50 60 70(二)操作性能的評定：1)本設計的操作條件為VL=23.5242m3h,VG=7763.0257m3h，P（VL,VGOP，即作出操作線。根據(jù)負荷性能圖及操作線的交點，可以看