分離乙醇--異丁醇課程設(shè)計(jì)

1、一、設(shè)計(jì)題目：別離乙醇一異丁醇混合液的浮閥精儲(chǔ)塔二、原始數(shù)據(jù)及條件：生產(chǎn)水平：年處理量5萬噸；年開工7200小時(shí)原料：乙醇含量24%質(zhì)量分?jǐn)?shù),下同,泡點(diǎn)進(jìn)料別離要求：塔頂乙醇含量不低于95%塔底乙醇含量不高于5%塔板的工藝設(shè)計(jì)、精儲(chǔ)塔全塔物料衡算F:進(jìn)料量kmol/sXf:原料組成摩爾分?jǐn)?shù),下同D:塔頂產(chǎn)品流量kmol/sXd:塔頂組成塔底殘液流量kmol/sXw:塔底組成原料液乙醇的組成：xF24/4633.7%塔頂組成:Xf塔底組成：xW24/4695/4695/465/745/465/4695/7476/7496.83%7.81%0.76/74)0.03kmol/s5107(0.24/4

2、6進(jìn)料量：F=5萬噸/年=300243600物料衡算式：F=D+W聯(lián)立帶入求解：D=0.0087kmol/sW=0.022kmol/s、常壓下乙醇一異丁醇汽液平衡組成摩爾與溫度的關(guān)系溫度ToC80.082.585.087.590.092.595.097.5100.0102.5105.0107.5Xa0.91280.79190.67250.57390.46780.38520.31030.23800.16910.11030.05390.0026Va0.97190.92530.86740.80980.73300.65780.57760.48410.37620.26040.14140.00741.溫度

3、95.092.5tF92.51')tF-0.31030.38520.3370.3852(2)tD=80.077.5tD77.50.91281.00000.96831.0000(3)1105.0102.5tw102.5tw-0.05390.11030.07810.1103(4)精微段平均溫度：E=tFtD94.178.486.3oC22利用表中數(shù)據(jù)由內(nèi)插法求得：tF、tD、tWtF94.10ctD78.4oCtw103.9oC(5)提儲(chǔ)段平均溫度:F_tFtWt2=294.1103.999.0oC2.密度：混合液密度:aAaB(aA=24%,aB=76%,A為乙醇的密度,b為異丁醇的密度

4、)混合氣密度:T0PM22.4po(M為平均相對(duì)分子質(zhì)量)塔頂溫度:tD=78.4oC氣相組成yD:8077.578.477.5進(jìn)料溫度:tF氣相組成yF：塔底溫度:0.91791o-=94.1CyDyD0.970195.097.50.57760.657894.192.5yF0.6578yF0.6064tW=103.9oC氣象組成yW:105.0102.5103.9102.5(1)精福段液相組成:X1氣相組成:y1所以ML1Mvi(2)提福段液相組成:氣相組成:所以ML2MV20.14140.2604yW0.2604yw0.19664646X2y24646(xDxf)2(yDYf)265.27

5、%78.83%(XwXf)2(yWyF)20.76%40.15%0.96830.33720.97010.6064747465.27%78.83%(165.27%)(178.83%)0.07810.33720.19660.606474(174(1根據(jù)在不同溫度下乙醇和異丁醇的密度求得在tF=94.loC查表得：乙醇=717.0異丁醇20.76%)40.15%)55.72kg/mol51.93kg/mol20.76%40.15%68.19kg/mol62.76kg/mol3、tF'tD'tw下乙醇和異丁醇的留度(單位：kg/m)=736.0那么進(jìn)料液混合液的密度:0.240.767

6、17736F731.0tD=78.4°C查表得：乙醇=733.0異丁醇=751.0,一一、1那么混合液的密度：0.950.05733751734.0tW=103.9°C查表得:乙醇=707.0異丁醇=726.0,一一、1那么混合液的密度：W0.050.95707726725.0所以L1二二23.混合物的粘度731.0734.0732.5L2731.0725.0728.0精微段的平均溫度:ti86.3°C,查表得:乙醇0.39MPa?s,異丁醇0.72MPa?s提儲(chǔ)段的平均溫度:t286.3°C,查表得:乙醇0.32MPa?s,異丁醇0.59MPa?s(1

7、)精微段粘度:乙醇X1異丁醇(1Xi)(2)=0.39提儲(chǔ)段粘度:X65.27%+0.72X(1-65.27%)=0.50MPa?s乙醇X2異丁醇(1X2)=0.324.相對(duì)揮發(fā)度X20.76%+0.59X(1-20.76%)=0.53MPa?s由xF=0.337,yF=0.6064,X,得：0.60641)x0.3371(1)0.337F=3.03f=1.06同理：Xd=0.9683,yD=0.9701Xw=0.0781,yw=0.1966f=2.89那么精微段平均相對(duì)揮發(fā)度:提福段平均相對(duì)揮發(fā)度:3.031.0623.032.892.042.96三、熱量衡算1 .加熱介質(zhì)的選擇本設(shè)計(jì)選用1

8、20°C的飽和水蒸氣作加熱介質(zhì),水蒸氣易獲得、清潔、不易腐蝕加熱管,不但本錢會(huì)相應(yīng)降低,塔結(jié)構(gòu)也不復(fù)雜25°C的冷卻水,選升溫10°C,即冷卻水2 .冷卻劑的選擇常用的冷卻劑是水和空氣,應(yīng)因地制宜地加以選用.本設(shè)計(jì)選用的出口溫度為35°C=3 .熱量衡算(1) 冷凝器的熱負(fù)荷Q=(R+1)D(IVD-ILD)式中IVD：塔頂上升蒸氣的烙,ILD：塔頂儲(chǔ)出液的燃又IVD-ILD=XdHv乙醇(1Xd)Hv異丁醇式中Hv乙醇：乙醇的蒸發(fā)潛熱,Hv異丁醇：異丁醇的蒸發(fā)潛熱蒸發(fā)潛熱的計(jì)算：tD=78.4oC時(shí)：乙醇Tr2T2TC273.1578.4516.250

9、.681Tr1273.1564.7516.250.654蒸發(fā)潛熱Hg醇HV1(OrZ)038846(10.681)0.38820kJ/kg1Tr110.654同理異丁醇：噴詈a653Tr1T1273.15108.1-0.708Tc'538.15蒸發(fā)潛熱HV異丁醇一,1Tr2、0.38erJ0.653,0.38HV2(r2)527()562kJ/kg1Tr110.708IVD-ILD=XdHV乙醇(1Xd)Hv異丁醇=0.9683X820+(1-0.9683)X562=811kJ/kgQC=(R+1)D'(Ivd-Ild)=(4+1)XMdDX811=811X5X0.0087X3

10、600X46.8876=5.9X106kJ/kg(2)冷卻水消耗量Cpc(t2t1)蒸發(fā)潛熱與溫度的關(guān)系HV2HV1(1Tr2).38,式中Tr：比照溫度.1Tri沸點(diǎn)下蒸發(fā)潛沸點(diǎn)/oC蒸發(fā)潛熱4HV(kJ/kg)Tc/K八、"U八乙醇78.4846516.25異丁醇108.1527538.15式中WC：冷卻水消耗量,kg/hCpc：冷卻水在平均溫度下的比熱容,kJ/(kgoC)11,t2：冷卻介質(zhì)在冷凝器進(jìn)出口的溫度,oC-t,tc2535t25-530°C,此溫度下水的比熱容Cpc=4.25kJ/(kg-°Q22也凹QC5.91064所以WCC13.910kg

11、/hCpc(t2tj4.25(3525)(3)再沸器液負(fù)荷及全塔熱量衡算列表計(jì)算乙醇、異丁醇在不同溫度下混合物的比熱容Cp(單位：kJ/(kg-°C)乙醇1.6041.7091.6171.6331.678異丁醇3.2553.4863.3783.3113.426精福段:乙醇：Cpi(tLDtF)1.633(78.494.1)25.638kJ/kg異丁醇：Cp2(tLDtF)3.311(78.494.1)51.983kj/kg提福段：乙醇：Cp1(tWtF)1.678(103.994.1)16.444kJ/kg異丁醇：Cp2(tWtF)3.426(103.994.1)33.575kJ/k

12、g塔頂儲(chǔ)出液的比熱容：Cp1Cp1?xD'(1xD')?Cp20.951.6330.053.3111.717kJ/kg塔釜儲(chǔ)出液的比熱容：Cp2Cp1?xW'(1xW')?Cp20.051.6780.953.4263.339kJ/kg為簡(jiǎn)化計(jì)算,現(xiàn)以進(jìn)料崎,即94.1°C時(shí)的始值為基準(zhǔn).1D'Md?D0.00873600460.968374(10.9683)1468kgh1W'MW?W0.0223600460.078174(10.0781)5687kg-hQdD'tDCp1dtDCp1(tDtF)1.717(78.494.1)1

13、4683.96104kg-h-1tF_tW5-1QwW'Cp2dtDCp2(tWtF)3.39(103.994.1)56871.89105kg-htF對(duì)全塔進(jìn)行熱量衡算：&+Q=Q+Q+Q：6所以,再沸器實(shí)際熱負(fù)荷Qs'QS6.0106.72106kg-h-10.9Qs'加熱烝氣消耗重：查得：Hv7K基氣=2201.7kJ/kg,Wh3053kJ/hHv(4)熱量衡算結(jié)果表Q(kJ/h)W(kg/h)Q(kJ/h)QD(kJ/h)Q(kJ/h)Q'(kJ/h)W(kg/h)數(shù)值5.910613.91040-3.961041.891056.72106305

14、3四、理論塔板的計(jì)算泡點(diǎn)進(jìn)料q=1,那么q線方程y-qqXf-為直線,即1Xq=Xf(Xf=33.7%),那么根據(jù)最小回流比公式:精福段:Rmin110.96832.0410.337提福段:Rmin22.96最小回流比取較大的一個(gè),0.968310.337那么操作回流比2.04(10.9683)10.3372.96(10.9683)2.671.3910.337R=1.5min=1.5X2.67=4.00精微段操作線方程為ynRXnR1XDR1yn10.8xn0.1937提儲(chǔ)段操作線方程為ynqn,LXnqn,V皿？Xwqn,VLqn?FLqn?FWXnLqn?FW?xWyn13.16xm0.1

15、689用梯形圖解法得出實(shí)際理論板數(shù)ET,板效率可用奧康奈爾公式：Et0.49(l)0.245計(jì)算,其中:塔底與塔頂平均溫度下的相對(duì)揮發(fā)度,L：塔頂與塔底平均溫度下的液相粘度(1) 精微段：產(chǎn)2.04,L1=0.50MPa?sEt10.49(2.040.50)0.2450.49那么NP精NT9塊ET0.49(2) 提福段：2=2.96,l2=0.53MPa?sET20.49(2.960.53)0.2450.44那么NP提NT包工10塊Et0.44全塔所需實(shí)際塔板數(shù)為19塊全塔效率：N工100%=100%42.1%,而加料板位置在第10塔板.NP19五、塔徑的初步設(shè)計(jì)1 .氣液相體積流量的計(jì)算由前

16、面計(jì)算可知：Rmin=2.67,取R=1.5Rmin=1.5X2.67=4.0(1)精儲(chǔ)段：L=RXD=4.0X0.0087=0.035kmol/sV=(R+1)D=0.0435kmol/s：ML1=55.72kg/molMV1=51.93kg/molL1=732.5kg/m3V1=1.755kg/m3那么質(zhì)量流量：LML1?L0.03555.721.9502kg/sV1Mvi?v0.043551.932.2590kg/s體積流量：LS1LiL11.9502732.5332.66210m/sVS1vV12.25901.75531.287m/s提儲(chǔ)段：L=L+qxF=0.035+0.03=0.0

17、65kmol/sV=0.0435kmol/s：ML2=68.19kg/molMV2=62.76kg/mol.3.3L2=728.0kg/m3V2=2.05kg/m3那么質(zhì)量流量：L2Ml2?L68.190.0654.43kg/sV2MV2?V0.043562.762.73kg/s體積流量：LS2上出36.09103m3/sL2728.0VS2V2V22.732.05一一31.33m3/s2 .精福段0.7由U二平安系數(shù)XUmax,平安系數(shù)=0.60.8,此處取平安系數(shù)為UmaxC?j-L一上,式中C可由史密斯關(guān)聯(lián)圖查出3mel橫坐標(biāo)數(shù)值：LS1生產(chǎn)2.6621073250.50.042Vs1V

18、11.2871.755取板間距：HT0.45m,hL0.07mhL為板上液層高度,對(duì)于常壓塔一般取0.05m0.08m；對(duì)于減壓塔常取為0.025m0.03m,此處為常壓塔貝UHthL0.38m,查得C20=0.048D1.(41.287)/(3.140.69)Umax0.048(732.51.755)/1.7550.98m/su0.7Umax0.70.980.69m/s1.54m圓整D1=2m,橫截面積AT1d2/43.14m2,那么空塔氣速u1'1870.41m/s3.143 .提福段3橫坐標(biāo)數(shù)值：LS2(上)0.56.0910(728-0)0.50.086Vs2V21.332.0

19、5同樣,取Ht0.45m,hL0.07m,那么HthL0.38m,查得C20=0.033umax0.033(728.02.05)/2.050.62m/su0.7umax0.70.620.435m/sD14VS2,(41.33)/(3.140.435)1.97m212.一.21.33圓整D2=2m,橫截面積At2d2/43.14m,那么空塔氣速u2'0.42m/s3.14六、溢流裝置1 .堰長(zhǎng)1w:由塔板結(jié)構(gòu)參數(shù)系列化標(biāo)準(zhǔn)(單溢流型)查得：塔徑D=2m時(shí),1w=1308mm對(duì)于單溢流1w=(0.60.8)D)284L,皿出口堰局：本實(shí)驗(yàn)米用平直堰,堰上披圖度：hOWE(),Lh為塔內(nèi)液體

20、流量,E近似取1.10001w32.8436002.66210x2/3(1)精微段：hOW()0.010m10001.3堰高：hWhLhOW0.070.0100.060m3提福段：hOW'"4(36006.0910)2/30.019m10001.3堰高：hW'hLhOW0.070.0190.051m2.弓形降液管的寬度和橫截面弓形降液管的寬度用Wd表示,截面積用Af表示,設(shè)計(jì)中可根據(jù)堰長(zhǎng)與塔徑之比1w/D由圖查得lw/D=1.38/2=0.654m,查圖得：Af/At0.0700,Wd/D0.124Wd0.12420.248m貝UAfAt0.07003.140.219

21、8m2精福段:Af?HtLS10.21980.4532.6621037.16s提福段:Af?Ht'LS20.21980.456.0910316.24s停留時(shí)間>5s,故降液管可用.3.降液管底隙高度(降液管下端與塔板間的距離)Ln3600U0Lw(1)精儲(chǔ)段：取降液管底隙流速u00.13m/s,那么hoLSIlWu02.6621031.3080.130.016m,取h0為0.02m(2)提福段:h.'LS2lwU0'6.091031.3080.130.036m,取h.'為0.04m七、塔板分布、浮閥數(shù)目與排列1 .塔板分布：此設(shè)計(jì)塔徑D=2.0m,采用分缺

22、式塔板,以便通過人孔拆裝塔板2 .浮閥數(shù)目排列(1)精福段取閥孔能動(dòng)因子F0=12,那么孔速：u01-F0-12/1.7559.06m/sM每層塔板上浮閥數(shù)目：NVs1d0u0141.2870.7859.060.0392119個(gè)取邊緣區(qū)的寬度WC=0.06m,破沫區(qū)的寬度Ws=0.10m.計(jì)算塔板上的鼓泡區(qū)面積,即Aa2(x1R2x2R2arcsin)180RD2D2其中RWc0.060.94m,xWsWd0.010.2480.652m2222所以Aa2(0.652.0.9420.6522一0.942arcsin-052)2.24m21800.94浮閥排列方式采用等腰三角形叉排列,取同一橫排的

23、孔心距t=75mm,那么A.224u041排間距：t'-250mm,塔板開孔率：100%4.52%Nt1190.075U019.06(2)提福段取閥孔能動(dòng)因子F0=12,那么孔速u02012/-2.058.38m/sV2每層塔板上浮閥數(shù)目：N'同樣,取同一個(gè)橫排的孔心距,224排間距：t'一224-1330.075133個(gè)VS21.332,20.7858.380.0392d°u024t=75mm那么224mm,塔板開孔率：0.42100%5.01%u028.38塔板流體力學(xué)計(jì)算一、氣相通過浮閥塔板的壓降可根據(jù)hp=hc+hi+h,PphpLg計(jì)算其中：hc：與

24、氣體通過浮閥塔板的干板壓降相當(dāng)?shù)囊褐叨?m液柱hL：與氣體通過板上液層的壓降相當(dāng)?shù)囊褐叨?m液柱h:與克服液體外表張力的壓降相當(dāng)?shù)囊褐叨?m液柱1 .精福段(1) 干板阻力：hc15.34-V1u015.341.7559.060.054m2 L1g2732.59.8板上充氣液層阻力：取(充氣系數(shù))=0.5,hl1hL0.50.070.035m(3)液體外表張力所造成的阻力,此阻力很小,可以忽略不計(jì),因此與氣體流經(jīng)塔板的壓降相當(dāng)?shù)囊褐叨葹閔p1=0.054+0.035=0.089mp1hp1L1g0.89X9.8X732.5638.89pa2.提福段22(1) 干板阻力：hc25.34u

25、025.342.058.380.054m2L2g2728.09.8(2) 板上充氣液層阻力：取=0.5,hl2hL0.50.070.035m(3) 液體外表張力所造成的阻力,此阻力很小,可以忽略不計(jì),因此與氣體流經(jīng)塔板的壓降相當(dāng)?shù)囊褐叨葹閔p2=0.054+0.035=0.089mp2hp2L2g0.89X9.8X728.0634.96pa二、淹塔為了預(yù)防淹塔現(xiàn)象的發(fā)生,要求限制降液管中清液高度Hd<(HThW),即Hd=hp+hL+hdHd：降液管中清液層高度,m液柱hL：板上清液層高度hd與液體流過降液管的壓降相當(dāng)?shù)囊褐叨?m液柱hp：塔板壓降HT：板間距hw:出口堰高:平安系數(shù)

26、(對(duì)易揮發(fā)泡系,為0.30.5;對(duì)不易揮發(fā)泡系,為0.60.7)1,精福段(1) 單層氣體通過塔板的壓降相當(dāng)?shù)囊褐叨萮p1=0,089mpJo2,662X10-3o(2) 披體通過降放管的壓頭損失hd10.153(51)0.153X-)0.0025mlw?h01.308X0.016(3) 板上液層高度hL=0.07m,貝UHd1=0.089+0.025+0.07=0.1615m取=0.5,已選定HT=0.45m,hw=0.060m,那么(HThw)=0.5X(0.060+0.45)=0.255,可見Hdw(HThw),所以符合預(yù)防淹塔的要求.2.提福段(1)單板壓降所相當(dāng)?shù)囊褐叨龋篽D2=

27、0,089mp4Lccc609X10-3c液體通過降液管的壓頭損失hd20.153(-LS)20.153X(6.0910)20.0026mlw?h.1.308X0.036(3)板上液層高度hL=0.07m,貝UHd2=0.089+0.026+0.07=0.1616m取=0.5,已選定HT'=0.45m,hw'=0.051m,貝U(HThw)=0.5X(0.051+0.45)=0.2505,可見Hdw(HThw),所以符合預(yù)防淹塔的要求.三、物沫夾帶1,精福段KCfA泛點(diǎn)率：VS1-V1/(L1V1)1.36Ls1ZLX100%板上液體流經(jīng)長(zhǎng)度：Zl=D-2Wd=2-2X0.24

28、8=1.504m板上液體流經(jīng)面積：Ab=AT-2AF=3.14-2X0.2198=2.700m2取物性系數(shù)K=1.0,泛點(diǎn)負(fù)荷系數(shù)CF=0.103,那么、一1.287Jl.755/(732.51.755)1.36X1.504X2.662X10-3n/泛點(diǎn)率為*X100%24.64%1.0X0.103X2.7002.提福段取物性系數(shù)K=1.0,泛點(diǎn)負(fù)荷系數(shù)CF=0.101,那么_r-一_-3、一上生,1.33工,205/(7282.05)1.36XS.09X1.504X10、“八八"0coec/.,/人而工泛點(diǎn)率為、X100%30.80%<80%符合要求1.0X0.101X2.7

29、00四、塔板負(fù)荷性能圖1.物沫夾帶線泛點(diǎn)率VSVL一v1.36,乙X100%,據(jù)此可作出負(fù)荷性能圖的物沫夾帶線,按泛點(diǎn)率80%十算.KCFA(1)精儲(chǔ)a：0.832.51.755)36*1.5041.0X0.103X2.700,整理得VS'=4.113-38.585LS'精偶段提偶段LS/(m3/s)Vs/(m3/s)Ls/(m3/s)Vs,/(m3/s)0.0024.460.0024.040.014.120.013.73在操作范圍內(nèi),任取假設(shè)干個(gè)LS'值,計(jì)算如表所示:2.液泛線(HThW)=hp+hL+hd=hc+hl+h+hL+hd,由此確定液泛線,忽略式中h,2

30、2(HThW)=5.34-u+0.153()2+(H0)hW+"84E(3600LS)2LglW?h01000IwHVS而u0S(d0為浮閥孔直徑,標(biāo)準(zhǔn)孔徑為0.039m)-d°N4(1)精福段：221.755VS21LS22.843600LS10.2555.34X22S40.153X(S)21.5X(0.060X1(S1)30.7852X1192X732.5X0.0394X2X9.81.308X0.0210001.308整理得：V：5.166986.56LS77.44L2S/3(2)提福段:0.25055.34X2.05VS20.7852X332728.00.039429

31、.80.153X(L)21.5M0.0511.308X0.0422843600Ls2rW4X1X(S2)310001.308整理得:V.225.81863LS18.6LS/3精偶段提偶段Ls1/(m3/s)Vs1/(m3/s)LS2/(m3/s)Vs2/(m3/s)0.0012.090.0012.370.0031.870.0032.320.0041.760.0042.300.0071.980.0072.24計(jì)算如表所示:3.液相負(fù)荷上限AFHT液體的最大流量應(yīng)保證降液管中停留時(shí)間不低于35s,停留時(shí)間LS以.=5s作為液體在降液管內(nèi)停留時(shí)間的下限,那么(LS)maxAfHt50.2198X0.

32、450.0198m3/s4.漏液線對(duì)于Fi型重閥,依F0=5作為規(guī)定氣體最小負(fù)荷的標(biāo)準(zhǔn),那么Vs沙.(1)精福段:(VS1)min-X0.0392X119X5/J1.75540.536m3/s(2)提福段:(VS2)min2-X0.039X133X5/V2.054_30.55m/s直線,取E=1.0,那么(Ls)min(0.019X1000)32.84X15.液相負(fù)荷下限線取堰上層液高度hOW=0.019m作為液相負(fù)荷下線條件,作出液相負(fù)荷下限線,該線為與氣相流量無關(guān)的豎x1080.001m3/s,由以上15作出塔板性能復(fù)合線.3600浮閥塔工藝設(shè)計(jì)計(jì)算結(jié)果工程符號(hào)單位計(jì)算數(shù)據(jù)備注精儲(chǔ)段提儲(chǔ)段

33、塔徑Dm22板間距Htm0.450.45塔板類型單溢流弓形降液管分塊式塔板空塔氣速um/s0.69*0.435堰長(zhǎng)lwm1.3081.308堰高h(yuǎn)wm0.0600.051板上層液高度hLm0.070.089降液管底隙高h(yuǎn)om0.0160.036浮閥數(shù)N119133等腰三角形排列閥孔氣速U0m/s9.068.38浮閥動(dòng)能因子F01212孔心距tm0.0750.075同一橫排孔心距排間距Vm0.250.224相鄰橫排中央距離單板壓降A(chǔ)ppPa638.89634.96降液管內(nèi)清液層高度Hdm0.16150.1616泛點(diǎn)率%24.6430.80氣相負(fù)荷上限(VS)max3,m/s5.857.62氣相負(fù)

34、荷下限(VS)min3m/s1.92.0霧沫夾帶限制操作彈性1.61.8漏液限制塔附件設(shè)計(jì)一、接管4Vs仃3DJ,MuF=1.6m/s,lL=731kg/m3V九F-332.64X10m/s1.進(jìn)料管采用直管進(jìn)料管,管徑計(jì)算如下:5X1073600X24X300X731D/4X2.64X10-333.14M.645.85mm,查標(biāo)準(zhǔn)系列選取e54x42.回流管1.95024X采用直管回流管,取uR=1.6m/s,dR?73446.00mm,查標(biāo)準(zhǔn)系列選取454x433.14X1.63 .塔底出料管取uw=1.6m/s,直管出料,dW0.22X7414X7253.14X1.642.28mm,查標(biāo)準(zhǔn)系列選取巾54x44 .塔頂蒸汽出料管一一)4X1.287.直管出氣,取出口氣速u