《化工原理課程設(shè)計》板式精餾塔 設(shè)計報告

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《化工原理課程設(shè)計》報告

4萬噸/年甲醇~水板式精餾塔設(shè)計

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目錄一、概述························································································41.1設(shè)計依據(jù)··················································錯誤！未定義書簽。1.2技術(shù)來源··················································錯誤！未定義書簽。1.3設(shè)計任務(wù)及要求···································································5二：計算過程··················································································61.塔型選擇··············································································72.操作條件的確定·····································································72.1操作壓力······································································72.2進料狀態(tài)······································································72.3加熱方式······································································72.4熱能利用······································································73.有關(guān)的工藝計算·····································································83.1最小回流比及操作回流比的確定··············錯誤！未定義書簽。3.2塔頂產(chǎn)品產(chǎn)量、釜殘液量及加熱蒸汽量的計算錯誤！未定義書簽。3.3全凝器冷凝介質(zhì)的消耗量···············································153.4熱能利用············································錯誤！未定義書簽。3.5理論塔板層數(shù)的確定·····················································153.6全塔效率的估算···································錯誤！未定義書簽。3.7實際塔板數(shù)NP····································錯誤！未定義書簽。4.精餾塔主題尺寸的計算··································錯誤！未定義書簽。4.1精餾段與提餾段的體積流量····················錯誤！未定義書簽。4.1.1精餾段·······························································184.1.2提餾段·······························································204.2塔徑的計算·································································224.3塔高的計算·································································305.塔板結(jié)構(gòu)尺寸的確定·····························································245.1塔板尺寸····································································255.2弓形降液管·········································錯誤！未定義書簽。5.2.1堰高··································································265.2.2降液管底隙高度h0················································275.2.3進口堰高和受液盤························錯誤！未定義書簽。5.3浮閥數(shù)目及排列···························································28

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5.3.1浮閥數(shù)目····························································285.3.2排列··································································285.3.3校核··································································296.流體力學驗算······································································306.1氣體通過浮閥塔板的壓力降(單板壓降)hp··························306.1.1干板阻力hc························································306.1.2板上充氣液層阻力h1············································316.1.3由表面張力引起的阻力h?······································316.2漏液驗算····································································316.3液泛驗算····································································316.4霧沫夾帶驗算······························································327.操作性能負荷圖···································································327.1霧沫夾帶上限線···························································327.2液泛線·······································································337.3液體負荷上限線···························································337.4漏液線·······································································337.5液相負荷下限線···························································347.6操作性能負荷圖···························································348.各接納尺寸的確定································································368.1進料管·······································································368.2釜殘液出料管······························································368.3回流液管····································································378.4塔頂上升蒸汽管···························································378.5水蒸汽進口管······························································383

一、概述1.1設(shè)計背景塔設(shè)備是化工、煉油生產(chǎn)中最重要的設(shè)備之一。塔設(shè)備的設(shè)計和研究，已經(jīng)受到化工行業(yè)的極大重視。在化工生產(chǎn)中，塔設(shè)備的性能對于整個裝置的產(chǎn)品產(chǎn)量、質(zhì)量、生產(chǎn)能力和消耗定額，以及三廢處理和環(huán)境保護等各個方面，都有十分重大的影響。精餾過程的實質(zhì)是利用混合物中各組分具有不同的揮發(fā)度。即在同一溫度下，各組分的飽和蒸汽壓不同這一性質(zhì)，使液相中的輕組分轉(zhuǎn)移到汽相中，汽相中的重組分轉(zhuǎn)移到液相中，從而達到分開的目的。因此精餾塔操作彈性的好壞直接關(guān)系到石油化工企業(yè)的經(jīng)濟效益。為了加強工業(yè)技術(shù)的競爭力，長期以來，各國都在加大塔的研究力度。如今在我國常用的板式塔中主要為泡罩塔、浮閥塔、篩板塔和舌型塔等。填料種類出拉西、環(huán)鮑爾環(huán)外，階梯環(huán)以及波紋填料、金屬絲網(wǎng)填料等規(guī)整填料也常采用。更加強了對篩板塔的研究，提出了斜空塔和浮動噴射塔等新塔型。同時我國還進口一些新型塔設(shè)備，這些設(shè)備的引進也帶動了我國自己的塔設(shè)備的科研、設(shè)計工作，加速了我國塔技術(shù)的開發(fā)。國外關(guān)于塔的研究如今已經(jīng)放慢了腳步，是由于已經(jīng)研究出了塔盤的效率并不取決與塔盤的結(jié)構(gòu)，而是主要取決與物系的性質(zhì)，如：揮發(fā)度、黏度、混合物的組分等。國外已經(jīng)轉(zhuǎn)向研究“在提高處理能力和簡化結(jié)構(gòu)的前提下，保持適當?shù)牟僮鲝椥院蛪毫?，并盡量提高塔盤的效率。〞在新型填料方面則在努力的研究發(fā)展有利于氣液分布均勻、高效和制造便利的填料。經(jīng)過我國這些年的努力，在塔研究方面與國外先進技術(shù)的差距正在不斷的減小4

目前，精餾塔的設(shè)計方法以嚴格計算為主，也有一些簡化的模型，但是嚴格計算法對于連續(xù)精餾塔是最常采用的，我們此次所做的計算也采用嚴格計算法。1.2設(shè)計條件原料：甲醇、水原料溫度：泡點進料處理量：4萬噸/年原料組成：甲醇的質(zhì)量分率wf=0.35（質(zhì)量分數(shù)）產(chǎn)品要求：塔頂甲醇的質(zhì)量分率wd=0.94（質(zhì)量分數(shù)），塔底甲醇質(zhì)量分率=0.02（質(zhì)量分數(shù)）生產(chǎn)時間：300天/年冷卻水進口溫度：25℃加熱劑：0.9MP飽和水蒸汽單板壓降：小于或等于0.7kpa生產(chǎn)方式：連續(xù)操作，泡點回流全塔效率：Et=50%1.3設(shè)計要求1.撰寫課程設(shè)計說明書一份2.帶控制點的工藝流程圖一張3.塔裝備的總裝圖一張

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1.4設(shè)計說明書的主要內(nèi)容1.設(shè)計方案的確定2.帶控制點的工藝流程圖的確定3.操作條件的選擇（包括操作壓強、進料狀態(tài)、加熱劑、冷卻劑、回流比）4.塔的工藝計算（1）全塔物料衡算（2）最正確回流比的確定（3）理論板及實際板的確定（4）塔徑的計算（5）降液管及溢流堰尺寸的確定（6）浮閥數(shù)及排列方式（篩板孔徑及排列方式）的確定（7）塔板滾動性能的校核（液沫夾帶校核，塔板阻力校核，降液管液泛校核，液體在降液管內(nèi)停留時間校核，嚴重漏液校核）（8）塔板負荷性能圖的繪制（9）塔板設(shè)計結(jié)果匯總表5.輔助設(shè)備工藝計算（1）換熱器的面積計算及選型（2）各種接納管徑的計算及選型（3）泵的揚程計算及選型6.塔設(shè)備的結(jié)構(gòu)設(shè)計：（包括塔盤、裙座、進出口料管）二：計算過程6

1.塔型選擇根據(jù)生產(chǎn)任務(wù)，若按年工作日300天，每天開動設(shè)備24小時計算，由于產(chǎn)品粘度較小，流量較大，為減少造價，降低生產(chǎn)過程中壓降和塔板液面落差的影響，提高生產(chǎn)效率，選用浮閥塔。2.操作條件的確定2.1操作壓力壓力為P0?1.01325?105（Pa）2.2進料狀態(tài)雖然進料方式有多種，但是飽和液體進料時進料溫度不受季節(jié)、氣溫變化和前段工序波動的影響，塔的操作比較簡單控制；此外，飽和液體進料時精餾段和提餾段的塔徑一致，無論是設(shè)計計算還是實際加工制造這樣的精餾塔都比較簡單，為此，本次設(shè)計中采取飽和液體進料（q=1）。2.3加熱方式精餾塔的設(shè)計中多在塔底加一個再沸器以采用間接蒸汽加熱以保證塔內(nèi)有足夠的熱量供應(yīng)；由于乙醇~水體系中，乙醇是輕組分，水由塔底排出，且水的比熱較大，故可采用直接水蒸氣加熱，這時只需在塔底安裝一個鼓泡管，于是可省去一個再沸器，并且可以利用壓力較底的蒸汽進行加熱，無論是設(shè)備費用還是操作費用都可以降低。2.4熱能利用精餾過程的原理是屢屢部分冷凝和屢屢部分汽化。因此熱效率較低，尋常進入

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再沸器的能量只有5%左右可以被有效利用。雖然塔頂蒸汽冷凝可以放出大量熱量，但是由于其位能較低，不可能直接用作為塔底的熱源。為此，我們擬采用塔釜殘液對原料液進行加熱。3.物料的工藝計算由于精餾過程的計算均以摩爾分數(shù)為準，需先把設(shè)計要求中的質(zhì)量分數(shù)轉(zhuǎn)化為摩爾分數(shù)。原料液的摩爾組成：甲醇的摩爾質(zhì)量為：32kg/kmol水的摩爾質(zhì)量為：18kg/kmol0.35/32xF??0.230.35/32?0.65/18xD?0.94/32?0.8980.94/32?（1?0.94）/180.02/32xW??0.010.02/32?（1?0.02）/18以年工作日為300天，每天開車24小時計，進料量為：進料液的平均摩爾數(shù)MF?32?0.23?18?(1?0..23)?21.22kg/kmolm4?107F???261.8kmol/hMF21.22?24?300根據(jù)公式D?F.xF?xW0.23?0.01?261.8?xD?xW0.898?0.018

可求出D?64.86kmol/h由全塔的物料衡算方程可寫出：F?D?W求得W?196.94kmol/h表1.原料液、餾出液與釜殘液的流量名稱w(質(zhì)量分數(shù))x(摩爾分數(shù))原料液0.350.23261.8餾出液0.940.89864.86釜殘液0.020.01196.94流量kmol/h3.1相對揮發(fā)度可根據(jù)平衡線圖（圖3-1）查得塔頂、塔底溫度1—汽相2—液相

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圖3-1甲醇-水的等壓曲線或用計算法求得：①塔頂：y1?0.957，P?101.325kpao假設(shè)t=83℃,利用安托因方程lgPA?6.03055?1211.033，t?220.79lgPBo?6.07954?1344.8t?219.48oo計算得出PA?110.70kpa，PB?43.016kpaP?PBoPAoxy?再利用x?oo，PPA?PB求得x1?0.8615,y1?0.9412oo假設(shè)t=82℃，同理求得PA?107.39kpa，PB?41.58kpax1'?0.9078,y1'?0.9622利用比例差值法求出塔頂溫度：t?820.957?0.9622?，則t1?82.25℃83?820.9412?0.9622當t=82.25℃時，計算得出PAo?108.21kpa，PBo?41.93kpaoPA108.21?2.581此時的相對揮發(fā)度?1?o?PB41.93②塔進料處：x2?0.54110

oo假設(shè)t=90℃,同理求得PA?136.12kpa，PB?54.233kpax2?0.5751oo假設(shè)t=91℃,同理求得PA?140.1kpa，PB?56kpa'x2?0.5389利用比例差值法求出塔進料處溫度：t?900.541?0.5751?，則t2?90.94℃91?900.5389?0.5751當t=90.94℃時，計算得出PAo?139.85kpa，PBo?55.89kpaoPA139.85?2.502此時的相對揮發(fā)度?2?o?PB55.89③塔底：x3?0.035oo假設(shè)t=108℃,同理求得PA?222.46kpa，PB?93.98kpax3?0.0572oo假設(shè)t=109℃,同理求得PA?228.253kpa，PB?96.723kpa'x3?0.0350則得出塔底溫度：t3?109℃當t=109℃時，oPA228.253????2.360此時的相對揮發(fā)度3oPB96.723

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全塔的相對揮發(fā)度??3.2回流比R的確定?1?2?3?2.581?2.502?2.360?2.479由于是泡點進料（q=1），xq?xF?0.541相平衡方程y??x1?(??1)x當x?xF,求出夾緊點xP?0.541，yP?0.745，因此：Rmin?xD?yP0.957?0.745??1.039yP?xP0.745?0.541操作回流比R?(1.1?2)Rmin最少理論板數(shù)Nmin的確定：利用芬斯克方程??xD??1?xWlg????1?x?D??xW??lg?????0.541??1?0.035????lg?????????1?0.541??0.035?????7.07lg2.479Nmin由于設(shè)備的綜合費用與N(R+1)有直接的關(guān)系，因此繪制N(R+1)~R圖就可以求當R值時N(R+1)最小的為實際R令??R，由不同β得到R值Rmin利用吉利蘭圖

N?NminR?Rmin~求出N值，進而能得到N(R+1)N?1R?112

吉利蘭圖分別取β=1.1、1.2、1.3、1.4、1.45、1.5、1.55、1.6、2，將查上圖或計算出相應(yīng)的值，見下表：βRR?RminR?1N?NminN?11.11.1430.0490.591.21.2470.0930.521.31.3510.1330.511.41.45460.1690.4951.451.5070.1870.4913

NN(R+1)βR18.740.01.51.560.2030.4613.935.715.835.51.551.610.2190.46514.0836.7615.4736.371.61.66240.2340.4613.9437.1314.9836.7722.0780.3380.3711.836.3214.8237.16R?RminR?1N?NminN?1NN(R+1)驗算：若lgR?Rmin?0.17時，可以用下公式：R?1???0.17?N?Nmin?R?Rmin??0.9?N?1?R?1①若R=1.2，則Rmin?1.039,利用公式lgN?Nmin?R?Rmin??0.9?N?1?R?1N?Nmin??0.17?0.581，則N?18.26，求得求出?N?1?N?R?1??40.172。②若R=1.3，利用公式lgN?Nmin?R?Rmin??0.9?N?1?R?1???0.17求出?N?Nmin?0.5344，則N?16.33，求得N?R?1??37.559N?1③若R=1.4，利用公式lgN?Nmin?R?Rmin??0.9?N?1?R?1N?Nmin??0.17?0.495，求出?N?1?則N?14.98，求得N?R?1??35.95。14

計算結(jié)果說明在R=（1.15~1.35）范圍內(nèi)R?Rmin?0.17，但N?R?1?值確隨RR?1值增大而減小，無最小值，所以根據(jù)作圖找到最適回流比R=(1.56~1.61).取R=1.573.3物料平衡①精餾段操作方程：y?xR1.570.957x?D?x??0.611x?0.372R?1R?12.572.57精餾段液體的摩爾流量：L?RD?1.57?45.142?70.873kmol/h氣體的摩爾流量：V??R?1?D?2.57?45.142?116.015kmol/h②提餾段操作方程：液體的摩爾流量：L'?L?qF?70.873?82.255?153.128kmol/h氣體的摩爾流量：V'?V??q?1?F?116.015?0?116.015kmol/hWxL'153.12837.613?0.035y?'x?W?x??1.32x?0.011'VV116.015116.015q線方程：x?0.54115

3.5理論塔板層數(shù)的確定精餾段操作線方程：y?0.611x?0.372提餾段操作線方程：y?1.32x?0.011q線方程：xf?xF?0.541相平衡方程：y??x2.479x?1????1?x1?1.479x利用逐板法計算理論塔板層數(shù)：相平衡方程y1?xD?0.957?????x1?0.900y2?0.922???x1?0.827y3?0.877???x3?0.742y4?0.825???x4?0.655y5?0.772???x5?0.577y6?0.725???x6?515?xF?0.541（進料板）y7?0.669???x7?0.449y8?0.582???x8?0.360y9?0.464???x9?0.259y10?0.331???x10?0.166

16

y11?0.208???x11?0.096y12?0.116???x12?0.050y13?0.055???x13?0.023?xW?0.003從上計算中可以得出理論塔板層數(shù)N理?13塊（含塔釜）其中，第6塊為進料板。N理?52%由條件知全塔效率Et?N實N理13??25（含塔釜）則可計算出實際塔板層數(shù)N實?Et0.524.基本物性數(shù)據(jù)計算根據(jù)苯~甲苯系的相平衡數(shù)據(jù)可以查得：y1?xD?0.957x1?0.902(塔頂?shù)谝粔K板)yF?0.719xF?0.541(加料板)xw?0.035yw?0.032(塔釜)全塔的相對平均揮發(fā)度：???1?2?3?2.581?2.502?2.360?2.479全塔的平均溫度：tm?tD?tF?tW82.25?90.94?109??91.115oC3317

4.1精餾段整理精餾段的已知數(shù)據(jù)列于表3(見下頁)，由表中數(shù)據(jù)可知：表3精餾段的已知數(shù)據(jù)位置進料板'xF?0.5塔頂(第一塊板)y1'?xD'?0.95x1'?0.884y1?xD?0.957x1?0.9ML1?79.4MV1?78.60282.25質(zhì)量分數(shù)'yF?0.684xF?0.541摩爾分數(shù)yF?0.719MLF?84.426摩爾質(zhì)量/kg/kmolMVF?81.934溫度/℃90.94①液相平均摩爾質(zhì)量：MLF?ML184.426?79.4??81.913kg/kmol22t?t90.94?82.25?86.6oC平均溫度：tm?FD?22M?在平均溫度下查得?苯?807kg/m3,?甲苯?803.4kg/m3液相平均密度為：1?Lm?'xLm?苯?'1?xLm?甲苯18

其中，平均質(zhì)量分數(shù)x'Lm'xF?x1'0.5?0.884???0.69222所以，?Lm?805.9kg/m3精餾段的液相負荷L?70.873kmol/hLn?LM?Lm?70.873?81.913?7.204m3/h805.9②汽相平均摩爾質(zhì)量：M?MVF?MV181.934?78.602??80.268kg/kmol22壓強PN?101.325?N?0.65kpa汽相平均密度為：?Vm?PMRT其中，平均壓強P?P101.325?0.65?101.325?6?0.651?PF??103.6kpa22所以，?Vm?2.78kg/m3精餾段的汽相負荷V?116.015kmol/hVn?精餾段的負荷列于表4。表4精餾段的汽液相負荷名稱液相汽相VM?Vm?116.015?80.268?3349.7m3/h2.7819

平均摩爾質(zhì)量/kg/kmol平均密度/kg/m體積流量/m/h3381.913805.97.204(0.002m/s)380.2682.783349.7(0.93047m/s)34.2提餾段整理提餾段的已知數(shù)據(jù)列于表5，采用與精餾段一致的計算方法可以得到提餾段的負荷，結(jié)果列于表6。表5提餾段的已知數(shù)據(jù)位置塔釜'x2?0.03進料板'xF?0.5'yF?0.684質(zhì)量分數(shù)'y2?0.047x2?0.035摩爾分數(shù)xF?0.541yF?0.719y2?0.055ML2?91.51摩爾質(zhì)量/kg/kmolMLF?84.426MVF?81.93490.94MV2?91.23溫度/℃109①液相平均摩爾質(zhì)量：MLF?ML284.426?91.51??87.968kg/kmol22t?t90.94?109?95.63oC平均溫度：tm?FD?22M?20

在平均溫度下查得?苯?797kg/m3,?甲苯?794.4kg/m3液相平均密度為：1?Lm?'xLm?苯?'1?xLm?甲苯''xF?x20.5?0.03???0.45722其中，平均質(zhì)量分數(shù)x所以，?Lm''Lm?795.6kg/m3提餾段的液相負荷L'?153.128kmol/hLn?''LM?Lm?153.128?87.968?16.931m3/h795.6②汽相平均摩爾質(zhì)量：M?MVF?MV281.934?91.23??86.582kg/kmol22PMRT汽相平均密度為：?Vm?平均壓強P?P2?PF101.325?13?0.65?101.325?6?0.65??107.5kpa22Vm'3??3.036kg/m所以，提餾段的汽相負荷V'?116.015kmol/hVn?'V'M?Vm?116.015?86.582?3308.6m3/h3.036表6提餾段的汽液相負荷名稱

液相21

汽相

平均摩爾質(zhì)量/kg/kmol平均密度/kg/m體積流量/m/h3387.968795.616.931(0.004703m/s)386.5823.0363308.6(0.9190m/s34.3全塔的流量由于精餾段和提餾段的上升蒸汽量相差不大，為便于制造，我們?nèi)啥蔚乃较嗟?。有以上的計算結(jié)果可以知道：汽塔的平均蒸汽流量：(Vn?Vn')3349.7?3308.6VS???3329.15m3/h?0.92476m3/s22汽塔的平均液相流量：(Ln?L'n)7.204?16.931LS???12.068m3/h?0.00335m3/s22汽塔的汽相平均密度：?V??Vm??'2Vm?2.78?3.036?2.908kg/m32汽塔的液相平均密度：?L??Lm??'2Lm?805.9?795.6?800.75kg/m325.塔徑的計算塔徑可以由下面的公式給出：22

D?4VS?u由于適合的空塔氣速u?(0.6~0.8)umax，因此，需先計算出最大允許氣速umax。umax?C?L??V?V初步設(shè)定板間距HT?0.45mL?12.068800.75功能參數(shù)：FLV?()L??0.06V?V3329.152.908從史密斯關(guān)聯(lián)圖查得：C20?0.081，由于C?C20(?20t?t?t82.25?90.94?109?91.115oC全塔的平均溫度：tm?DFW?33)0.2，需先求平均表面張力：23

在此溫度下，平均摩爾分數(shù)為81.913?87.968?89.9682查《化工原理》書379頁液體表面張力共線圖并計算出液體表面張力??20.4mN/m2史密斯關(guān)聯(lián)圖是按液體表面張力??20mN/m2的物系繪制的，若所處物系的表面張力為其他值，則需按式C?C20(C?0.081?(20.40.2)?0.081320?20)0.2校正查出的負荷系數(shù)，即：umax?C?L??V800.75?2.908?0.0813??1.347m/s?V2.908u=（0.6~0.8）umax=（0.808~1.077）m/s則取適合的空塔氣速u?0.85m/s塔徑的確定：①精餾段：氣相流量Vn?3349.7m3/h?0.93047m3/s塔徑D?4Vn4?0.93??1.181m?u??0.85②提餾段：氣相流量Vn'?3308.6m3/h?0.9190m3/s塔徑D'?根據(jù)塔徑系列尺寸圓整為D?1200mm6.塔板結(jié)構(gòu)尺寸的確定4Vn'?u?4?0.919?1.173m??0.8524

6.1確定塔板的流型由于塔徑大于800mm，所以采用單溢流型分塊式塔板。6.2塔板尺寸選取lW，而lW/D?（0.6~0.8）所以lW?（0.72~0.96），取lW?0.8m即lW/D?0.667然后根據(jù)上表弓形降液管的寬度與面積即可查出AWd?0.13，f?0.07DAT從而計算出：25

塔板總面積AT??4D2?1.1304m2弓形溢流管寬度Wd?156mm弓形降液管面積Af?0.079m2驗算：液體在精餾段降液管內(nèi)的停留時間??AfHTLn?0.079?0.45?17.775s?5s0.002液體在精餾段降液管內(nèi)的停留時間??'AfHTL'n?0.079?0.45?7.56s?5s0.047036.3弓形降液管6.3.1堰上液流高度how本設(shè)計采用平堰，則堰上液頭高how應(yīng)在（6~60mm之間）。對于平堰，則堰上液頭高how可用佛蘭西斯公式計算：?Lh?how?2.84?10E???lW??323對于式中液流收縮系數(shù)E可用下表差得E?1.0526

則計算how?2.84?10?1.05??3?12.068???18.2mm?6mm0.8??23當平堰上液頭高how?6mm時，堰上溢流會不穩(wěn)定，需改為齒形堰。6.3.2堰高采用平直堰，一般應(yīng)使塔板上得清夜層高度hL?50~100mm，而清夜層高度hL?hW?hOW，因此有：50?hOW?hW?100?hOW取hW?50mm，則hL?50?18.2?68.2mm6.3.3溢流管底與塔盤間距離h0因hW?h0?6mm，而hW?50mm若取精餾段取h0?30mm，那么液體通過降液管底隙時的流速為u0?

LS0.00335??0.14m/s?0.1m/s（舍棄）lWh00.7?0.0327

若取精餾段取h0?42mm，那么液體通過降液管底隙時的流速為u0?LS0.00335??0.0997m/s?0.1m/slWh00.7?0.042u0的一般經(jīng)驗數(shù)值為0.07~0.25m/s所以取h0?42mm6.4浮閥數(shù)目及排列采用F1型重閥，重量為33g，孔徑為39mm。6.4.1浮閥數(shù)目閥孔數(shù)n取決于操作時的閥孔氣速u0，而u0由閥孔動能因數(shù)F0決定。浮閥數(shù)目n?4VS?d02u0氣體通過閥孔時的速度u0?F0?v一般F0?8~11，對于不同工藝條件，也可以適當調(diào)整。取動能因數(shù)F?11，那么u0n?11?6.451m/s，因此2.9083329.15?4?120個??0.0392?6.4516.4.2排列閥孔的排列方式有正三角形排列和等腰三角形排列。

28

若按等邊三角形排列：孔心距t?d0150mm）0.907（常用有：75mm，100mm，125mm，A0/APn?d02120?3.1415?0.0392??0.143m2閥孔面積：A0?44??x??開孔鼓泡區(qū)面積：AP?2?xr2?x2?r2sin?1????r???D??Wd?Ws??0.6??0.156?0.05??0.394m2Dr??Wc?0.6?0.025?0.575m2x???0.394??則計算可得到AP?2?0.394?0.5752?0.3942?0.5752sin?1?????0.575???取t'?80mm時畫出的閥孔數(shù)目只有60個，不能滿足要求，取t'?65mm畫出閥孔的排布圖如圖1所示，其中t?75mm,t'?65mm圖中，通道板上可排閥孔41個，弓形板可排閥孔24個，所以總閥孔數(shù)目為N?41?24?2?89個6.4.3校核4VS?10.38m/s2?d0N氣體通過閥孔時的實際速度：u0?實際動能因數(shù)：F0?10.38?1.0335?10.55(在9~12之間)開孔率：?d02N閥孔面積??(0.039)2?89?100%??100%??13.5%塔截面積4AT4?0.7854

29

開孔率在10%~14之間，滿足要求。4.3塔高的計算塔的高度可以由下式計算：Z?HP?(N?2?S)HT?SHT?HF?HW已知實際塔板數(shù)為N?40塊，板間距HT?0.4m由于料液較清潔，無需經(jīng)常清洗，可取每隔8塊板設(shè)一個人孔，則人孔的數(shù)目S為：S?40?1?4個8取人孔兩板之間的間距HT?0.6m，則塔頂空間HD?1.2m，塔底空間HW?2.5m，進料板空間高度HF?0.5m，那么，全塔高度：Z?1.2?(40?2?4)?0.4?4?0.6?0.5?2.5?20.2m6.流體力學驗算6.1氣體通過浮閥塔板的壓力降(單板壓降)hp氣體通過浮閥塔板的壓力降(單板壓降)hp?hc?h1?h?6.1.1干板阻力hc浮閥由部分全開轉(zhuǎn)為全部全開時的臨界速度為uoc：uoc?1.82573.1/?V1.82573.1/1.0335?10.32m/s

30

由于uoc?uo?10.38m/s2?Vu01.0335?10.382所以hc?5.34?5.34??0.0367m2?Lg2?863?9.816.1.2板上充氣液層阻力h1取板上液層充氣程度因數(shù)??0.5，那么：h1??hL?0.5?0.06?0.03m6.1.3由表面張力引起的阻力h?由表面張力導致的阻力一般來說都比較小，所以一般狀況下可以忽略，所以：hp?0.0367?0.03?0.667m?0.667?863?9.81?564.7Pa6.2漏液驗算動能因數(shù)F0?5，相應(yīng)的氣相最小負荷VSmin為：VSmin??4d02Nu0min其中u0min?F所以VSmin??V?5/1.0335?4.92m/s2?0.0390?89?4.92?0.523m3/s?1.103m3/s?4可見不會產(chǎn)生過量漏液。6.3液泛驗算溢流管內(nèi)的清液層高度Hd?hp?hd?hL?h?

31

其中，hp?0.0667m,hL?0.06m所以，Hd?0.667?0.06?0.003?0.1297m為防止液泛，尋常Hd??(HT?hw)，取校正系數(shù)??0.5，則有：?(HT?hw)?0.5?(0.4?0.05)?0.225m可見，Hd??(HT?hw)，即不會產(chǎn)生液泛。6.4霧沫夾帶驗算VS?V?L??V?1.36LSZL泛點率=KCFAb查得物性系數(shù)K?1.0，泛點負荷系數(shù)CF?0.097ZL?D?2Wd?1?2?0.146?0.708mAb?AT?2Af?0.7854?2?0.0706?0.6442m2所以，1.103?1.0335?1.36?0.00146?0.708863?1.0335?63.4%?80%1?0.097?0.6442泛點率=可見，霧沫夾帶在允許的范圍之內(nèi)7.操作性能負荷圖7.1霧沫夾帶上限線32

取泛點率為80%代入泛點率計算式，有：VS0.8??V?L??V?1.36LSZL?VSKCFAb1.0335?1.36?0.708LS863?1.03350.097?0.6442整理可得霧沫夾帶上限方程為：VS?1.444?27.8LS7.2液泛線2/3液泛線方程為aVS2?b?cL2S?dLS其中，a?1.91?105?V?LN2?1.91?105?1.0335?0.0309863?86b??HT?(??1??0)?0.5?0.4?(0.5?1?0.5)?0.05?0.15c?0.1530.153??192.422lwh00.7052?0.015212/3lwd?(1??0)E(0.667)?(1?0.5)?1.02?0.667?1?3.55320.7052/3?114.9L代入上式化簡后可得：VS2?4.85?6.217L2SS7.3液體負荷上限線取??5s，那么LSmax?AfHT5?0.0706?0.4?0.00565m3/s57.4漏液線

33

取動能因數(shù)F0?5，以限定氣體的最小負荷：VSmin??42d0N5?V?0.523m3/s7.5液相負荷下限線L2.84?1.02?[Smin]2/3?0.006100