化工原理課程設(shè)計苯與氯苯的分離

化工原理課程設(shè)計說明書設(shè)計題目：苯一氯苯精儲過程板式塔設(shè)計設(shè)計者：班級化工095閆宏陽日期：2011年12月13號指導(dǎo)教師：勝凱設(shè)計成績：日期：目錄TOC\o"1-5"\h\z設(shè)計任務(wù)書3設(shè)計計算書4?設(shè)計方案的確定4?精儲塔物料衡算4?塔板數(shù)的確定5?精儲塔的工藝條件及有關(guān)物性數(shù)據(jù)的計算8?塔體工藝尺寸計算13?塔板主要工藝尺寸15?塔板流體力學(xué)驗算17?浮閥塔的結(jié)構(gòu)20?精微塔接管尺寸23?產(chǎn)品冷卻器選型25?對設(shè)計過程的評述和有關(guān)問題的討論25附圖：生產(chǎn)工藝流程圖精儲塔設(shè)計流程圖設(shè)計任務(wù)書（一）題目試設(shè)計一座苯一氯苯連續(xù)精儲塔，要求年產(chǎn)純度99.8%的氯苯21000噸，塔頂儲出液中含氯苯不得高于2%原料液中含氯苯45%（以上均為質(zhì)量分數(shù)）。（二）操作條件（1）塔頂壓力4kPa（表壓）；（2）進料熱狀況泡點；(3)回流比R=1.4Rmin;（4）塔底加熱蒸汽壓力0.5Mpa（表壓）；(5)單板壓降<0.7kPa;（三）塔板類型浮閥塔板（F1型）（四）工作日每年按300天工作計，每天連續(xù)24小時運行（五）廠址廠址為地區(qū)一、設(shè)計方案的確定設(shè)計計算書本任務(wù)是分離苯一氯苯混合物。對于二元混合物的分離，應(yīng)采用連續(xù)精儲流程，本設(shè)計采用板式塔連續(xù)精儲。設(shè)計中采用泡點進料，將原料液通過預(yù)熱器加熱至泡點后送進精儲塔。塔頂上升蒸氣采用全凝器冷凝，冷凝液在泡點下一部分回流至塔，其余部分冷卻后送至儲物罐。該物系屬易分離物系，最小回流比較小，故操作回流比取最小回流比的1.4倍，且在常壓下操作。塔釜采用間接蒸汽加熱，塔底產(chǎn)品經(jīng)冷卻后送至儲物罐。、精微塔物料衡算（以輕組分計算）1.原料液及塔頂、塔釜產(chǎn)品的摩爾分率苯的摩爾質(zhì)量氯苯的摩爾質(zhì)量MA78.11kg/kmolMB112.56kg/kmolXf0.55/78.110.55/78.110.45/112.560.638XD0.98/78.110.98/78.110.02/112.560.986Xw0.002/78.110.002/78.110.998/112.560.0032.原料液及塔頂、塔釜產(chǎn)品的平均摩爾質(zhì)量Mf0.63878.11(10.638)112.5690.58kg/kmol0.98678.11(10.986)112.5678.59kg/kmolMw0.00378.11(10.003)112.56112.46kg/kmol3.物料衡算原料處理量W21000100025.93kmol/h30024112.46總物料衡算FD25.93苯物料衡算0.638F0.986D0.00325.93聯(lián)立解得D47.31kmol/h聯(lián)立解得F73.24kmol/h三、塔板數(shù)的確定1.理論板數(shù)N的求取(1)由手冊查得苯一氯苯物系的氣液平衡數(shù)據(jù)，繪出x—y圖，見圖1T/oC8090100110120130131.8pA/kPa101.33136.66179.99234.60299.99378.65386.65pB/kPa19.7327.3339.0753.3372.4095.86101.33oxPPbx——ooPaPb1.0000.6770.4420.2650.1270.0190.000oPAy-xP1.0000.9130.7850.6130.3760.0720.000

1.0000.0000.8000.6000.4000.200qa0.0000.2000.4001.0000.0000.8000.6000.4000.200qa0.0000.2000.4000.600Xq0.8001.000X圖1圖解法求最小回流比(2)由于泡點進料q=1,在圖上作直線x=0.986交對角線于a點，作直線x=0.638交平衡線于q點，連接a、q兩點，過q點作橫軸的平行線交縱軸于一點，讀得圖1x—y圖yq=0.896,則最小回流比如下：c0.9860.896…Rmin0.350.8960.638取操作回流比為R1.4Rmin1.40.350.49(3)求精儲塔的氣、液相負荷LRD0.4947.3123.18kmol/hV(R1)D(0.491)47.3170.49kmol/hLLF23.1873.2496.42kmol/hVV70.49kmol/h（4）求操作線方程精微段操作線方程LD23.1847.31,y—x—xDx0.9860.328x0.662TOC\o"1-5"\h\zVV70.4970.49提儲段操作線方程LW96422593y—xWxW9642x25930.0031.369x0.001VV70.4970.49（5）圖解法求理論板層數(shù)如附圖1,將x=0.638帶入精儲段操作線方程，得出y=0.871,在圖中找出該點記為d,連接ad兩點即得精儲段操作線；在對角線上找到c點（0.003,0.003）,連接cd兩點即得提儲段操作線。自a點開始在操作線和平衡線之間作階梯線。求解結(jié)果為：總理論板層數(shù)Nt11（包括再沸器）進料板位置Nf4.實際板層數(shù)的求解（試差法）假設(shè)總板效率Et=0.49精儲段實際板層數(shù)N精22/0.4944.945提儲段實際板層數(shù)N提4/0.4918.1-17（不包括再沸器）實際板層數(shù)為26/0.49-1=52（不包括再沸器）試差法計算如下：N=52塔頂壓力：PD101.34105.3KPa塔底壓力：Pw105.30.66752139.984Pa已知塔底組成為四、精儲塔的工藝條件及有關(guān)物性數(shù)據(jù)的計算1.操作壓力的計算塔頂操作壓力每層塔板壓降進料板壓力PD101.34105.33kPaP0.7kPaPF105.330.79111.63kPa精微段平均壓力Pm1(111.63105.33)/2108.48kPa塔底操作壓力PD105.330.723121.43kPa提儲段平均壓力Pm2(111.63121.43)/2116.53kPa2.操作溫度的計算ABC溫度圍（K）苯6.019071204.682-53.072279-3776.068321236.034-48.99353-4226.36071466.083-15.44420-521氯苯6.104161431.83-55.515335-4056.629881897.415.21405-597表1苯、氯苯Antoine常數(shù)數(shù)據(jù)表ABC溫度圍（K）苯6.019071204.682-53.072279-3776.068321236.034-48.99353-4226.36071466.083-15.44420-521氯苯6.104161431.83-55.515335-4056.629881897.415.21405-597（表1苯、氯苯Antoine常數(shù)數(shù)據(jù)表①假設(shè)塔頂?shù)呐蔹c溫度t83.2oC,則純組分的飽和蒸氣壓為對苯lgpA6.06832pA111.53kPa1236.03448.9983.2273.152.04742對氯苯lgpO6.10416pO22.11kPa1431.8355.51583.2273.151.34464oPPoPPBooPaPb0.931代入泡點方程和露點方程，得(101.334)22.11111.5322.11oPa——XP111.530.931105.330.986XD故假設(shè)正確，塔頂溫度為tD83.2oC②假設(shè)塔頂?shù)倪M料板溫度t94.4°C,則純組分的飽和蒸氣壓為對苯lgpA6.06832PA154.26kPa1236.03448.9994.4273.152.18825對氯苯lgpo6.10416p②假設(shè)塔頂?shù)倪M料板溫度t94.4°C,則純組分的飽和蒸氣壓為對苯lgpA6.06832PA154.26kPa1236.03448.9994.4273.152.18825對氯苯lgpo6.10416pO32.77kPa1431.8355.51594.4273.151.51548代入泡點方程和露點方程，得PPoooPaPb110.2332.77154.2632.770.638假設(shè)正確，故進料板溫度為tF94.4oC③假設(shè)塔底的泡點溫度t1370c，則純組分的飽和蒸氣壓為對苯lgpA6.06832pA442.51kPa1236.03448.99137273.15對氯苯lgp06.629881897.415.21137273.15po115.28kPa代入泡點方程，得ppB

ppB

00PaPb116.53115.28442.51-115.280.00380.003假設(shè)正確，故塔頂溫度為tW1370C精微段平均溫度tm1(83.294.4)/288.8°C提儲段平均溫度tm2(94.4137)/2115.7oC全塔平均溫度tm(83.2137)/2110.1oC.平均摩爾質(zhì)量的計算塔頂：由yXd0.986,查平衡曲線得X0.920MVDm0.98678.11(10.986)112.5678.60kg/kmolMLDm0.92078.11(10.920)112.5680.87kg/kmol進料板：由圖理論板得yF0.885,查平衡曲線得Xf0.621MVFm0.88578.11(10.885)112.5682.07kg/kmolMLFm0.62178.11(10.621)112.5691.17kg/kmol塔底：由圖理論板得yn0.003,查平衡曲線得xn0.001MVWm0.00378.11(10.003)112.56112.46kg/kmolMLWm0.00178.11(10.001)112.56112.53kg/kmol精微段平均摩爾質(zhì)量MVm1(78.6082.07)/280.34kg/kmolMLm1(80.8791.17)/286.02kg/kmol提儲段平均摩爾質(zhì)量MVm2(82.07112.46)/297.27kg/kmolMLm2(91.17112.53)/2101.85kg/kmol.平均密度的計算(1)氣相平均密度計算由理想氣體狀態(tài)方程計算，得爐衲卬Pm1MVm1108.4880.343植俑反Vm12.90kg/mRTm18.314(88.8273.15)提儲段Vm2^M-116.5397.273.51kg/m3RTm28.314(115.7273.15)(2)液相平均密度計算1wiLm

塔頂tD83.2oC時,TOC\o"1-5"\h\z___3a9121.18783.2813.24kg/m__3b11271.11183.21034.56kg/m13LDm816.73kg/m0.98/813.240.02/1034.56進料板t進料板tF94.4oC時,9121.18794.4799.95kg/m311271.11194.41022.12kg/m3LFm0.62178.110.62178.110.379112.56

LFm0.62178.110.62178.110.379112.56

10.532/803.70.468/1025.70.532894.28kg/m3塔底tw1370c時,a9121.187137749.38kg/B11271.111137974.79kg/m3LWm974.20kg/m3LWm974.20kg/m30.002/749.380.998/974.79精儲段液相平均密度為Lm1(816.73894.28)/2855.51kg/m3提儲段液相平均密度為3Lm2(894.28974.20)/2934.24kg/m.液相平均表面力的計算Lmxii塔頂tD83.2oC時，查得A20.82mN/mB25.84mN/mLDm0.92020.820.0825.8421.22mN/m進料板tF94.4oC時，查得A19.35mN/mB24.57mN/mLFm0.62119.350.37924.5721.32mN/m塔底tW1370c時，查得A14.25mN/mB19.48mN/m

LWm精儲段液相平均表面力為m(21.2221.32)/221.27mN/m提儲段液相平均表面力為m2(21.3219.47)/220.40mNm2(21.3219.47)/220.40mN/m.液體平均粘度計算lgmxlg塔頂tD83.2oC時,A0.299mPaA0.299mPa0.303mPaslgLDm0.920lg0.2990.08lg0.303lgLDm0.920lg0.2990.08lg0.303LDm0.299mPas進料板t進料板tF94.4oC時,lg0.268mPasb0.275mPasLDmlg0.268mPasb0.275mPasLDm0.621lg0.2680.379lg0.275LDm0.271mPas塔底tW137oC時,a0.184mPasa0.184mPasb0.197mPaslgLDmlgLDm0.001lg0.1840.999lg0.197LDm0.197mPas精儲段液相平均粘度為m1(0.2990.271)/20.285mN/m提留段液相平均粘度為m2(0.2710.197)/20.234mN/mm2全塔液相平均粘度為L(0.2990.197)/20.248mPas又塔頂和塔底平均溫度為(83.2+137)/2=110.1C則此溫度下的相對揮發(fā)度為二23474.40pB53.3根據(jù)奧康奈爾關(guān)聯(lián)法，Et0.49(L)0.2450.49(4.400.248)0.2450.48故假設(shè)成立，總板效率Et=0.48五、塔體工藝尺寸計算.塔徑的計算(1)精儲段LS1VMVm170.4980.343600Vm1LMLm1LS1VMVm170.4980.343600Vm1LMLm13600Lm136002.9030.542m3/s23.1886.023600855.10.0006m3/s由UmaxCL——V式中C由公式C0.2，計算,20其中C20可由史密斯關(guān)聯(lián)圖查出，圖的橫坐標為LhVh0.000636000.54136002.90取板間距Ht0.42m,板上液層高度hL0.07m,則HthL0.420.070.35m由史密斯關(guān)系圖得C200.0690.2CC20L200.0690.221.270.070Umax0.070855.512.901.20m/s440.5423.140.72取安全系數(shù)為0.6,則空塔氣速為0.6u440.5423.140.720.979mD=1.0m統(tǒng)一按照《塔板結(jié)構(gòu)參數(shù)系列化標準（單溢流型）》將塔徑圓整后取D=1.0m塔截面積AT—D23141.020.785m244實際空塔氣速u05420.690m/s0.785（2）提儲段VS2VMvm23600Vm270.4997.2736003.510.543m3/sVS2VMvm23600Vm270.4997.2736003.510.543m3/sLs2LM523600Lm296.42101.853600934.243.0.0029m/sLh12LV10.00293600934.240.54336003.510.087HthL0.420.070.35m查圖得C200.068m2200.20.06820.400.2200.068Umax0.068934.243.513.511.12m/sUm2200.20.06820.400.2200.068Umax0.068934.243.513.511.12m/sU2D20.61.120.67m/s0.6Umax40.5433.140.6721.00mD=1000mmD=1000mm統(tǒng)一按照《塔板結(jié)構(gòu)參數(shù)系列化標準（單溢流型）》將塔徑圓整后取塔截面積atZD2個120.785m2實際空塔氣速0.5430.692m/s0.785.塔高的計算(1)精儲塔的有效高度精微段Z精(N精1)Ht(91)0.423.36m提儲段Z提(N提1)Ht(141)0.45.46m在進料板上方開一人孔，提儲段中開兩個人孔，其高度為0.8m,則有效高度為Z有效Z精Z提0.833.365.462.411.2m(2)全塔實際高度取進料板板間距為0.8m,人孔處的板間距為0.8m,塔底空間高度為2.0m,塔頂空間高度為0.7m,封頭高度為0.6m,裙座高度為2.0m,則全塔高為H(nnFnP1)HtnFHFr1PHpHdHbH1H2(23131)0.420.830.80.72.00.62.016.06m六、塔板主要工藝尺寸計算根據(jù)塔徑和液體流量，選用單溢流弓形降液管、凹形受液盤，塔板采用單流和分塊式組裝。1.溢流裝置的計算(1)堰長：lW0.66D0.661.00.66m(2)堰高：由hwhLh°w,選用平直堰，堰上液層高度由弗蘭西斯公式求得222.84Lh132.840.000636003精微段：how1E”0.00626m1000lw10000.66取hL0.07m提儲段:hwihi_howi0.070.006260.06374mhOW22.84E10002L提儲段:hwihi_howi0.070.006260.06374mhOW22.84E10002Lh23lw2.8420.0029360030.0018m10000.66hLhOW20.070.0180.052m(3)降液管面積當回0.66時,D查表得組DAf0.124,Wd當回0.66時,D查表得組DAf0.124,Wd0.1241.00.124m0.0722,Af20.07220.7850.057m2塔的相對操作面積為120.0715100%85.7%(4)液體在降液管里停留的時間精儲段3600AfH精儲段3600AfHtLh136000.0570.4038s5s36000.0006故降液管設(shè)計合理(5)降液管底隙高度hoh036001wh036001wUo精儲段和提儲段降液管下端與塔板間出口處的液體流速分別取精儲段提儲段u01h01h020.075m/sLh136001wUo1Lh2精儲段提儲段u01h01h020.075m/sLh136001wUo1Lh236001wUo2u020.180m/s36000.000636000.660.07536000.002936000.660.1800.012m0.024m2.塔板布置的計算選用F1型浮閥，閥孔直徑39mm閥片直徑48mm閥片厚度2mm最大開度8.5mm靜止開度2.5mm閥質(zhì)量為32~34g。

(1)閥孔臨界速度0.5480.548精儲段U0Kp172.872.85.86m/sV12.900.5480.548提儲段U0Kp272.872.85.27m/sV23.51上下兩段相應(yīng)的閥孔動能因子為：FoiUokpi.-vi5.86,2.909.979F02u°kp21V25.273.519.873均屬正常操作圍取邊緣區(qū)寬度W=0.055m,安定區(qū)寬度Ws0.065m,開孔區(qū)面積Aa2xR2x2叵sin1'180RTOC\o"1-5"\h\z22210.311220.311.0.4450.311——0.445sin—0.504m1800.445其中，RDWc100.0550.445m22xD-WdWs100.1240.0650.31122(2)提福段塔板布置取邊緣區(qū)寬度W=0.030m,安定區(qū)寬度Ws0.055m,開孔區(qū)面積Aa2Aa2xR2x2aR2.sin1801_xR其中,20.321.0.47020.321其中,20.321.0.47020.32122.10.32120.470sin0.552m1.00.0300.470m1.0——0.1240.0550.3212(3)浮閥數(shù)1.00.0300.470m1.0——0.1240.0550.3212(3)浮閥數(shù)n與開孔率F1型浮閥的閥孔直徑為39mm閥孔氣速U0F0=10浮閥數(shù)目n一2——u0d0/4開孔率n當D精福段U0105.87m/s.2.9040.542n5.870.0390.039780.0390.03911.86%1.1提留段785.34m/s40.5435.340.0390.0393.1486860.0390.0391112.94%浮閥排列方式采用等腰三角形叉排，取同一橫排的孔心距t=0.075m,則排間距t為Aa精福段U0105.87m/s.2.9040.542n5.870.0390.039780.0390.03911.86%1.1提留段785.34m/s40.5435.340.0390.0393.1486860.0390.0391112.94%浮閥排列方式采用等腰三角形叉排，取同一橫排的孔心距t=0.075m,則排間距t為Aa0504精微段t-0.0862m86.2mmnt780.075Aa0552提留段tA-0.0856m86.6mmnt860.075考慮到塔的直徑較大,故采用分塊式塔板，而各分快板的支撐與銜接將占去一部分鼓泡區(qū)面積，因此排間距應(yīng)小于計算值，故取t=80mm=0.08m重新計算孔速及閥數(shù)精福段Aa0.504tt0.0750.08u°0.5424nd2/4840.0390.039——5.53m/s3.14F05.53..2.909.4184提留段nAa0.0390.039

n

0.55212.78%92U0F0tt0.0750.080.5434nd(2/4920.0390.0393.144.94.3.519.250.0390.0399213.99%11由此可知，閥孔動能因數(shù)變化不大七、塔板流體力學(xué)驗算1.塔板壓降hphlh(1)u°0.5424nd2/4840.0390.039——5.53m/s3.14F05.53..2.909.4184提留段nAa0.0390.039

n

0.55212.78%92U0F0tt0.0750.080.5434nd(2/4920.0390.0393.144.94.3.519.250.0390.0399213.99%11由此可知，閥孔動能因數(shù)變化不大七、塔板流體力學(xué)驗算1.塔板壓降hphlh(1)干板阻力精儲段U0c11.82573.1/

V提儲段U01hc1U0c2U02U0c1,19.0則0.175U01L11.82573.1/U0C2,則0.17519.0^^L2(2)板上充氣液層阻力取充氣系數(shù)00.5,則hl0hL0.54.94m/sV11.82573.1/2.905.860m/s195530.175195.530.029m液柱855.51V2191.82573.1/3.515.27m/s0.175工94一0.026m液柱934.240.070.035m液柱(3)液體表面力所造成的阻力：此阻力很小，忽略不計因此，上下兩段塔板壓降如下精儲段每層壓降hpihcih0.0290.0350.064m液柱pn1hg0.064855.519.81537.12Pa700PapIpILI提儲段每層壓降hp2hc2hl0.0260.0350.061m液柱pp2hp2L2g0.061934.249.81559.06Pa700Pa上下兩段單板壓降均符合設(shè)計任務(wù)要求。.液泛為了防止液泛現(xiàn)象的發(fā)生，要求控制降液管中清液層高度Hd(Hthw),而MhphLhd(1)與氣體通過塔板壓降所相當?shù)囊褐叨染⒍蝖p10.064m液柱p提儲段hp20.061m液柱p4(2)液體通過降液管的壓頭損失22精儲段hd10.153-LS-0.1530.00060.00088m液柱精儲段Wh010.660.012提儲段2hd20.153-LS^提儲段2hd20.153-LS^!wh020.1530.00290.660.0240.0051m液柱(3)板上液層高度精儲段和提儲段皆為hL0.07m因此，取0.5,降液管中清液層高度如下:精儲段Hd1精儲段Hd1hp1hL1hd10.0640.0700.000880.1349m(HthW1)0.5(0.420.06374)0.2419Hd1可見，精儲段符合防止液泛的要求。(Ht提儲段Hd2hp2hL2hd2(HthW2)0.5(0.420.052)0.236Hd2

可見，提儲段符合防止液泛的要求。.液沫夾帶(1)精儲段液沫夾帶量(1)精儲段液沫夾帶量ev的驗算VsuaAtAf5.7106ex3.25.71065.7106ex3.25.7106UaHthf0.74453.221.271030.422.50.070.0094kg液/kg氣0.1kg液/kg氣故在設(shè)計負荷下不會發(fā)生過量液沫夾帶。(2)提儲段液沫夾帶量ev的驗算5.7106uaevHth5.7106uaevHthf3.25.7100.745820.401030.422.50.073.20.0085kg液/kg^0.1kg液/kg氣故在設(shè)計負荷下不會發(fā)生過量液沫夾帶。.漏液的驗算(1)精儲段漏液的驗算F。-r,U0取F0=5,貝UU05U05一52.94m/s2.905.53m/s故在設(shè)計負荷下不會產(chǎn)生過量漏液。(2)提儲段漏液的驗算5

u02.67m/s.3.514.94m/s故在設(shè)計負荷下不會產(chǎn)生過量漏液。(2)提儲段漏液的驗算5

u02.67m/s.3.514.94m/s故在設(shè)計負荷下不會產(chǎn)生過量漏液。八、塔板負荷性能圖計算(一)精微段塔板負荷性能圖1、漏液線F0u0,取Fo=5,又nVV2U0d0/4故（Vs）min—d2nuF0u0,取Fo=5,又nVV2U0d0/4故（Vs）min—d2nu0—0.0392842.94據(jù)此做出與液體流量無關(guān)的水平漏液線（0.295m3/s1)2.液沫夾帶線5.7106ev3.2Ua

HThf其中，UaVsAtAf0.7850.0570.746Vs(a)hf2.5hwhow2.5hw2.84103E3600LslW近似取E=1.0,hw0.06374m,lW0.66mhf2.50.063742.841031.03600Ls0.660.1592.20Ls2/3(b)取液沫夾帶極限值ev為0.1kg液/kg氣。已知21.7mN/m,HT0.42m并將a,b代入得:0.15.710621.710并將a,b代入得:0.15.710621.71030.746Vs0.420.1592.2LS/3S3.2整理得:2/3Vs2.2318.87LsLs,m3/s0.00060.00150.00300.0045Vs,m3/s2.101.981.841.72在操作圍任取幾個Ls值，依上式算出相應(yīng)的Vs值列于下表中3.液相負荷下限線依表中數(shù)據(jù)在Vs—Ls圖中作出液沫夾帶線（2）。

取平堰、堰上液層高度how0.006m作為液相負荷下限條件，取E1.0則%需a*)"322843600LSmin怎10000.660.0062841.0Smn10000.66整理上式得Ls,min0.00056m3/s依此值在Vs—Ls圖中作線即為液相負荷下限線（3）。4.液相負荷上限線(LS)max叱0.0570.420.006m3/s依此值在Vs—Ls圖中作線即為液相負荷上限線（4)5.液泛線令Hd(Hth4.液相負荷上限線(LS)max叱0.0570.420.006m3/s依此值在Vs—Ls圖中作線即為液相負荷上限線（4)5.液泛線令Hd(HthW)Hdhp，hd;hphch1h;h17;兒hWhow聯(lián)立整理得_2..2aVsbcLsdLs23式中0.051(v、,/、2()(Aoco)L0.0512.90_2((0.1000.772)855.510.029Ht(1)限0.50.42(0.50.601)0.063740.140-20.153/(lWho)——0153—22439(0.660.012)2.84103E(136002.336002.)()32.84103(10.60)()31.40lw0.66故0.029Vs20.142439Ls1.40Ls233Ls,m/s0.00060.00150.00300.0045—3Vs,m/s4.794.013.071.81在操作圍任取幾個Ls,計算出Vs的值列于表中。

依此值在Vs—Ls圖中作線即為液泛線（5）5條線包圍區(qū)將以上5條線標繪于VsLs5條線包圍區(qū)域為精儲段塔板操作區(qū)，A為操作點，OA為操作線。O陽與（2）線的交點相應(yīng)相負荷為Vs,max,OA線與氣相負荷下限線（1）的交點相應(yīng)氣相負荷為Vs,min。圖見坐標紙?？芍驹O(shè)計塔板上限由液沫夾帶控制，下限由漏液控制。讀圖，精儲段白^操作彈性j1684Vs,min0.42二、提福段塔板負荷性能圖1、液沫夾帶線（1）3.25.7106UaeHthf式中vsvsua——S-S1.374Vs（a）ATAf0.7850.057233600Ls3hf2.5hwhow2.5hw2.84103E-lW近似取E-1.0,hw0.052m,lW0.66m2,,33600Ls32/3/「、故hf2.50.0522.841031.0S0.132.2Ls（b）0.66取液沫夾帶極限值ev為0.1kg液/kg氣。已知20.40103N/m,HT0.42m…5.71060.1320.40101.374V…5.71060.1320.40101.374Vs2/30.420.132.2Ls整理得：Vs1.3610.1Ls2/33.23Ls,m/S0.00060.00150.0030.0045VS,m3/S1.291.231.151.08在操作圍任取幾個LS值，依上式算出相應(yīng)的VS值列于下表中依表中數(shù)據(jù)在VS—Ls圖中作出液沫夾帶線（1）。2、液泛線（2）由HdhphLhd和Hd(HtHthwhphwhow3Ls,m/S0.00060.00150.0030.0045VS,m3/S1.291.231.151.08在操作圍任取幾個LS值，依上式算出相應(yīng)的VS值列于下表中依表中數(shù)據(jù)在VS—Ls圖中作出液沫夾帶線（1）。2、液泛線（2）由HdhphLhd和Hd(HtHthwhphwhowhd近似取Elw0.66mhow2.84103e3600Ls

lw2.84101.0223600Ls3.S0.88L30.66hPhohlhhc20.051—Co0.051VsCoAo0.051Vs3.510.7720.100934.240.032Vs20hwhow0.732/30.0520.88L20.0382/30.6424Ls0.0018m（已算出）hP_20.032Vs0.0380.6424L：320.00180.032VS22/30.6424LS0.0398hd0.1532LS

lwho0.1530.660.024_2609.79L；將Ht0.42m,hW0.052m,0.5及以上各式0.50.4222/30.0520.032VS20.03980.6424LS0.0522/30.88Ls一一一2609.79LS整理得V4.5147.58LS/319056.0Ls2在操作圍任取幾個Ls值，依上式計算Vs值列于下表中13/_Ls,m/S0.00060.00150.0030.0045

VS,m3/s2.041.971.831.68依表中數(shù)據(jù)在Vs-Ls圖中作出液泛線（2）。3、液相負荷上限線（3）取液體在降液管中停留時間為4秒，由下式LSmaxHtAf0.420.0573LSmax0.00599m/s4液相負荷上限線（3）在VS—Ls圖中為與氣相流量Vs無關(guān)的垂線。4、漏液線（氣相負荷下限線）（4）F0F0U0,取F0=5,又nV2U0d0/42故（Vs）2故（Vs）min—j0nu0—0.0392922.670.293m3/s4據(jù)此做出與液體流量無關(guān)的水平漏液線（1）5、液相負荷下限線（5）取平堰、堰上液層高度兒卬0.006m作為液相負荷下限條件，取E1.0則how”4E（10003600Ls,min）2/32284則how”4E（10003600Ls,min）2/322843600Lsmin看0.0062841.0210000.66整理上式得Ls,min5.63104m3/s依此彳1在Vs-Ls圖中作線即為液相負荷下限線（5）。將以上5條線標繪于VsLs圖中，即為提儲段負荷性能圖。5條線包圍區(qū)域為提儲段塔板操作區(qū)，P為操作點，OP為操作線。OP線與（2）線的交點相應(yīng)相負荷為vSmax,OP,Imax7線與氣相負荷下限線（4）的交點相應(yīng)氣相負荷為Vs,min。圖見坐標紙?？芍驹O(shè)計塔板上限由液泛控制，下限由漏液控制。讀圖，提微段的操作彈性V讀圖，提微段的操作彈性VS,max1.42338Vs,min0.42.九、精儲塔接管尺寸計算.塔頂蒸氣出口管70.498.314(83.2273.15)。牌1m3公3600Pd3600105.33d40.5513.1418選擇蒸氣速度d40.5513.14180.197m按照GB8163-87,選擇熱軋無縫鋼管2456.5mm核算u4VS40551,11.69m/s,在10~20m/s之間，可用d23.140.2452.塔頂回流液管LsLMLDmLsLMLDm3600LDm35.580.183600823.810.001m3/s選擇回流液流速u0.4m/s,則d40.00063.140.40.043m按照選擇回流液流速u0.4m/s,則d40.00063.140.40.043m按照GB8163-87,選擇冷軋無縫鋼管452mm核算u4LS40.00060.377m/s,在0.2~0.5m/st間，可用d23.140.04523.進料管FsFMLFmFsFMLFm3600LFm73.2491.173600894.280.0021m3/sd40.0021,3.142.0選擇進料液流速u2.0m/s,則d40.0021,3.142.00.037m按照GB8163-87,選擇冷軋無縫鋼管422mm核算u空S40.002121.52m/s,在1.5~2.5m/s之間，可用d23.140.04224,塔釜出料管LSLMLWm96.42112.530.0031m3/s3600LWm3600974.20

選擇塔釜出料液流速u0.8m/s,則d4Ls40.00340.071m;u.3.140.8按照GB8163-87,選擇冷軋無縫鋼管832mm核算u840.0030920.57m/s,在0.5~1.0m/st間，可用d23.140.08325.加熱蒸氣進口管KK0KK0350.2781.261.15選擇蒸氣速度u15m/s,則VRTw70.498.314(137273.15)0573m3/s3600pw3600116.530.22md4Vs40.7470.22m,u.3.1415按照GB8163-87,選擇熱軋無縫鋼管24512mm核算u絲40.747,12.3m/s,在12~20m/st間，可用d23.140.2452十產(chǎn)品冷卻器選型①基本物性數(shù)據(jù)的查?。孩谒斅缺胶枯^少，可按純苯求取苯的定性溫度tD=83.2C設(shè)水的進口溫度為匕25C根據(jù)設(shè)計經(jīng)驗，選擇冷卻水的溫升為8C,則水的出口溫度為t2258水的定性溫度253329C2查得苯在定性溫度下的物性數(shù)據(jù)密度：812.94kg/m3飽和蒸汽氣化熱：r=393.9kJ/kg查得水在定性溫度下的物性數(shù)據(jù)密度：995.5kg/m3

定壓比熱容：Cp4.174kJ/(kg?C)2°導(dǎo)熱系數(shù)：k=0.618W/(m-C)黏度:3.=0.80x黏度:3.=0.80x10Pa?s②熱負荷計算:r=78.11_3r=78.11_3AX47.31X393.9X10/3600=4.04X105W冷卻水耗量:WcQCpc(WcQCpc(t2-口4.041054.174103(33-25)12.11kg/s③確定流體的流徑該設(shè)計任務(wù)的熱流體為苯，冷流體為水，為使苯能通過殼壁面向空氣中散熱,提高冷卻效果，令苯走殼程，水走管程.計算平均溫度：暫按單殼程、雙管程考慮，先求逆流時平均溫度差苯T83.2-----83.2冷去水t33----2550.258.250.258.2t2-t1t2-t1?t2ln——t1^t10.137T1t10.8,選單殼程可行。公稱直徑DN400mm公稱壓力Nh1.6MPA58.2-50.254.10C,58.2ln50.2④計算R和P:RT^^20,Pt2-t1查表得：t1,因t'一tmttm54.10C⑤選擇換熱器型號由于兩流體溫差=50C，殼選用固定管板式換熱器的系列標準(JB/T4715-92)選擇主要參數(shù)如下：管程數(shù)Np4管子尺寸252.5p管子根數(shù)n94管長6000mm管中心距32mm中心排管數(shù)11管子排列方式正三角形管程流通面積0.0163m2實際換熱面積S0nd0(L0.1)943.140.025(60.1)43.5m2選K值，估算傳熱面積2參照《化工流體流動與傳熱》附錄二十六，初選取K=310W/(m?C)cQ4.041052S24.1mKtm31054.10、如一435230...安全系數(shù)：100%89.1%,傳熱面積的裕度可滿足工藝要求。23.0采用此換熱面積的換熱器，則要求過程的總傳熱系數(shù)為：5K0—Q—4.0410172W/(m2.C)S0tm43.554.10驗算：k/310/1.801.15,符合實際標準Ko172設(shè)計結(jié)果一覽表物料衡算結(jié)果序號項目符號單位數(shù)值備注1塔頂摩爾分數(shù)Xd10.9862塔頂平均摩爾質(zhì)量MDkg/kmol78.6080.87氣相液相3塔頂流量Dkmol/h45.074進料摩爾分數(shù)Xf10.6385進料液平均摩爾質(zhì)量Mfkg/kmol82.0791.17氣相液相6進料流量Fkmol/h73.24

7塔釜摩爾分數(shù)xw10.0038塔釜平均摩爾質(zhì)量Mwkmol/h112.46112.53氣相液相9塔釜產(chǎn)品流量W25.93精儲塔工藝條件及有關(guān)物性數(shù)據(jù)計算結(jié)果序號項目符號單位精福段提福段備