【化工原理课程设计】甲醇和水筛板精馏塔分离

设计计算＜一＞设计方案的确定本设计任务为分离甲醇-水混合物。对于二元混合物的分离，应采用连续精储流程。设计中采用泡点进料，将原料液通过预加热器至泡点后送入精储塔内。塔顶上升蒸汽采用全凝器冷凝，冷凝液在泡点下一部分回流至塔内，其余部分经产品冷却器冷却后送至储罐。该物系属易分离系，最小回流比，故操作回流比取最小回流比的2倍。塔釜采用间接蒸汽加热，塔底产品经冷却后送至储罐。＜二＞精储塔的物料衡算1、原料液及塔顶、甲醇的摩尔质量塔底产品的摩尔分率M1、原料液及塔顶、甲醇的摩尔质量塔底产品的摩尔分率M甲醇=32.04kg/kmol水的摩尔质量M水=18.02kg/kmol0.40.99970.40.9997_32.04Xf=0.4_32.04Xf=0.40.6+32.0418.02=0.273Xd=32.040.99970.0003+—32.0418.02=0.99470.005Xw=32.04=0.002818Xw=0.0050.995+32.0418.022、原料液及塔顶、塔底产品的平均摩尔质量MF=0.273X32.04+(1—0.273)X18.02=21.85kg/kmolMd=0.9947X32.04+(1—0.9947)X18.02=31.96kg/kmolMW=0.002818X32.04+(1—0.002818)M8.02=18.06kg/kmol3、物料衡算原料处理量:210000000=115.57kmol/h总物料衡算：甲醇物料衡算:F=原料处理量:210000000=115.57kmol/h总物料衡算：甲醇物料衡算:F=――-〜―F3302421.85F=D+W115.57=D+Wfxf=dxd+wxw115.57X0.273=DX0.9947+W0.002818w=84.09kmol/h联立解得D=31.48kmol/hw=84.09kmol/h＜三＞塔板数的确定①由y=1①由y=温度液相气相a温度液相气相a92.90.05310.28347.0581.60.20830.62736.490.30.07670.40018.0380.20.23190.64856.1188.90.09260.43537.55780.28180.67755.3586.60.12570.48316.577.80.29090.68015.18850.13150.54557.9376.70.33330.69184.4983.20.16740.55866.2976.20.35130.73475.1182.30.18180.57756.1573.80.4620.77564.0272.70.52920.79713.49680.77010.89622.5771.30.59370.81833.0866.90.87410.91941.64、三x一、..一_..——x一及甲醇一水在不同温度下的汽一液平衡组成1+（：-1）x

700.68490.8492700.68490.84922.59am=19a1.a2.a3a19=4.83得到相平衡方程:x_4.83xy=1+(:-1)x-1+3.83x得到相平衡方程因为泡点进料，所以q=1且Xq=XF=0.273且q点过相平衡线贝Uyq=463xq=0.645=0.645且q点过相平衡线q1+3.83xqRmin=xD-yq=0.94取操作回流比R=2.Rmi=1.88yq小2、求精储塔的气液相负荷L=RD=1.88X31.48=59.18kmol/hV=(R+1)D=2.88X31.48=90.66kmol/hL=L+F=59.18+115.57=174.75kmol/hV=V=90.66kmol/h3、求操作线方程精储段操作线方程yn产—+=0.6528Xn+0.3454R1R1提储段操作线方程yn书=VL2-等=1.927Xn-2.614X10-35、逐板计算法求理论板数因为塔顶为全凝器y1=Xd=0.9947通过相平衡方程求X1=y——=0.97494.83-3.83y1再通过精微段操作线方程y2=0.6528X1+0.3454=0.9818,如此反复得y1=0.99947xi=0.9749y2=0.9818x2=0.9179y3=0.9446x3=0.7793y4=0.8541x4=0.5482y5=0.7032x5=0.3291y6=0.5603x6=0.2087<0.273当X6<Xq后，改用相平衡方程与提储段操作方程yn+1=1.927Xn-12.614X10-3计算.如此反复得y7=0.3995x7=0.1211y8=0.2308x8=0.0585y9=0.1101x9=0.025y10=0.0455xio=0.1474

yii=0.02578xii=5.45X10-3yi2=7.88X10-3X12=1.64X10-3<0.002818可得到进料板位置NF=6总理论板数Nt=12＜包括再沸器＞2、实际板层数的求取，一一、一，一一5精微段实际板层数：N精=言=8.3=9提福段实际板层数：N提=包=10（不包括再沸器）0.6＜四＞精储塔工艺条件及有关物性数据的计算1、操作压力计算塔顶操作压力PD=101.3+4=105.3KPa每层塔板压力降.F=0.7KPa进料板压力P进料板压力Pf=105.3+0.7X9=111.6KPa塔底压力Pw=PF+0.7x10=118.6KPa精微段平均压力Pm=105.3+111.62=108.45KPa提福段平均压力Pm'精微段平均压力Pm=105.3+111.62=108.45KPa提福段平均压力Pm'111.6+1202=115.1KPa2、操作温度计算（内插法得）根据甲醇-水的气-液平衡组成表，再通过内插法得:塔顶温度td=64.79C进料板温度tF=78.3C塔釜温度tw=99.6C精微段平均温度tm=tD+tF=64.79+783=71.54C22提储段平均温度tm="W=78.3+99.6=88.95。223、平均摩尔质量的计算塔顶平均摩尔质量计算由XD=yi=0.9947通过相平衡方程求得Xi=0.9749MVd解y1M甲+(1-y1)M水=0.9947X32.04+(1-0.9947)X18.02=31.97Kg/KmolMLOM=XiM甲+(1-Xi)M水=0.9749X32.04+(1-0.9749)X18.02=31.69Kg/Kmol进料板平均摩尔质量计算通过逐板计算得进料板yF=0.5603,再通过相平衡方程得Xf=0.2087M/FMryFM甲+(1-yF)M水=0.5603X32.04+(1-0.5603)X18.02=25.87Kg/Kmol

MF^XFM甲+(1-XF)M水=0.2087X32.04+(1-0.2087X18.02)=20.95Kg/Kmol塔釜平均摩尔质量的计算由Xw=0.002818查平衡曲线得yw=0.01346M/WMyw/M甲+(1-yw)M水=0.01346X32.04+(1-0.01346)X18.02=18.21Kg/KmolMLW=X/X甲+(1-XwM水=0.002818X32.04+(1-0.002818)X18.02=18.06Kg/Kmol精福段平均摩尔质量M/M=(MVDM+MVFM)2M/M=(MVDM+MVFM)231.97+25.87=28.92Kg/KmolMLM=(MLDM+MLFM)231.69+20.952=26.32Kg/Kmol提福段平均摩尔质量M/M=(MVDM+MVFM)M/M=(MVDM+MVFM)225.87+18.212=22.04Kg/KmolMm'=(MLFM+MLWM)220.95+18.062=19.50Kg/Kmol4、平均密度计算⑴气相平均密度计算由理想气体状态方程计算即精福段PVM=PmMvm108.4528.92精福段PVM=PmMvm108.4528.92RTm8.314(71.54+273.15)=1.094Kg/mPmMvm提储段：:vm，=~~-RTm115.122.048.314(88.95+273.15)=0.8427⑵液相平均密度计算液相平均密度按下式计算即，二液相平均密度按下式计算即，二pLmpi塔顶液相平均密度的计算由tD=64.79C查手册得P甲=747.168Kg/m*以=980.613Kg/msTOC\o"1-5"\h\z一1.1：LPM=3D3w=^"9970W=747.7Kg/m++P甲P水746.168980.613进料板液相平均密度计算由tF=78.3C查手册得P甲=735.53Kg/m5P水=972.82Kg/m5进料板液相的质量分率xfM甲0.2087M32.04…”aA===0.3192aA=xfM甲+(1-xf)M水0.2087M32.04+0.7913父18.02

「LFM=~~0cA——+P甲「LFM=~~0cA——+P甲11-OCA提储段液相平均密度计算由tw=99.6C查手册得p甲=716.36Kg/m*跺=958.176Kg/m,TOC\o"1-5"\h\z、11;LWI===957.06Kg/mww1-3w0.0050.995—++。甲p水716.36958.676»Cldm:lfm747788191精微段液相平均密度为：LM==8=814.8Kg/m22提微段液相平均密度：iM'=三皿J81.9"。6=919.48Kg/m225、液体平均表面张力的计算液相平均表面张力依下式计算即0M=£Xj◎塔顶液相平均表面张力的计算由tD=64.79C查手册得&甲=18.31mN/m&水=65.29Mn/m&0M=%辨+(1-XD)外=0.9947X18.31+0.0053X65.29=18.56mN/m进料板液相平均表面张力的计算由tF=78.3C查手册得和=17.0647mN/m&K=62.889mN/m配FM=XF湃+(1-XF)M=0.2087X17.0647+0.7913X62.889=53.32mN/m塔釜液相平均表面张力的计算由tw=99.6C查手册得每甲=14.93mN/m3水=58.9mN/m配W=Xw标+(1-Xw)%=0.002818X14.93+(1-0.2087)X62.889=53.32mN/m精储段液相平均表面张力为提储段液相平均表面张力为6、液体平均粘度计算、lQ：.|、lfm18.5653.32”〜LM==、lQ：.|、lfm18.5653.32”〜LM===35.94mN/m22OLFM•1.LWM53.3258.78==56.05mN/m塔顶液相平均粘度计算由tD=64.79C查手册得N甲=0.3289mpa.sN水=0.4479mpa.slgNLDM=XD|g坳+(1-XD)lg蹂=0.9947g(0.3289)+(1-0.9947)lg(0.4479)=-0.4825-ldm=0.3292mpa.s进料板液相平均粘度计算由tF=78.3C查手册得N甲=0.28193mpa.sN水=0.37084mpa.slg^lfm=XFlg/甲+(1-XF)lg限=0.2087lg(0.28193)+(1-0.2087)lg(0.37084)=-0.4557-LFM=0.35mpa.s由tw=99.6C查手册得用=0.226mpa.sN水=0.289mpa.s

1g-Lw而Xwlg□甲+(1-Xw)lg%=0.0028181g(0.226)+(1-0.002818)lg(0.289)=-0.5394JL丽0.2888mpa.s精微段液相平均黏度为」LM="LDM”皿=0.32920.35=0.3397mpa.s22,-LFMJlw.[02888035提储段液相平均黏度为」lm'=0.28880.35=0.3194mpa.s22<五>精微塔的塔体工艺尺寸计算1、塔径的计算精微段的气液相体积流率为Vs=VMvm_3600pvm-90.6628.92Vs=VMvm_3600pvm-90.6628.9236001.094=0.6657m/sLs=LMlm3600plm591826.323600814.8=0.000531m/s提储段的气液相体积流率为VMvmVs3600pvmVMvmVs3600pvm90.6622.0436000.8427=0.6586m/sLMlm174.7519.503Ls'===1.029*10Ls3600pm3600919.48LV精微段Umax=cJ-^式中C由C20求取，C20可通过查图(P129页)筛板塔的泛点关联图的横坐标功能参数Ls不=0.000531I8141.Vs:：V0.6657V1.094取板间距H=0.35m（通过筛板塔的的泛点关联图）（书P129图10-42）得到C20=0.068C=Q0(dL)°2=0.068X(3594)0.2=0.076462020l-：v814.8-1.094取大仝塔气速UmaX=c<=0.0746.=2.085m/s\:v11.094取安全系数为0.8,则空塔气速u=0.8umax=0.8X2.085=1.668m/s4Vs40.6657D==.1=0.713m，二u3.141.668按标准塔径圆整后D=0.8m（据书P129表10-1）

D23.140.82-塔截面积为AT===0.5024m244实际空塔气速u=Vs=0^65Z=i.325m/sAt0.5024ut="至=0.63（安全系数在允许范围内，符合设计要求）Umax2.085919.48=0.051610.8427提福段同理查阅得919.48=0.051610.8427Ls：l1.02910-3.=VsvDv0.6586查表得H=0.35mC20'=0.07C=C20，(景0.2=0.07(5605)0.2=0.08602UmaX=C919.48-0.8427:0.8427UmaX=C919.48-0.8427:0.8427=2.84m/s同上取安全系数同上取安全系数0.8u'=0.8Umax'=0.8x2.84=2.272m/sD'40.65863.142.272=0.6076mD'40.65863.142.272=0.6076m圆整取D'=0.8m同上圆整取D'=0.8m同上AT'=0.5024m2实际空塔气速u'="=0.6586=1.313At0.5024u1313…—u—=313=046（符合安全系数范围，设计合理）Umax2.842、精微塔有效高度的计算精微段有效高度为Z精=（N精-1）Ht=（9-1）X0.35=2.8m提福段有效高度为Z提=（N提-1）Ht=（10-1）X0.35=3.15m在加料板上设一人孔，其高度为0.7m故精微塔的有效高度为Z=Z精+Z提+0.7=2.8+3.15+0.7=6.65m<六>塔板主要工艺尺寸的计算1、溢流装置计算因塔径D=0.8,可选用单溢流弓形降液管，采用凹形受液盘⑴堰长lw取lw=0.6D=0.48m⑵溢流堰图度hw由hw=hL—how284Lh选用平直堰，堰上液层高度how=E(L)2/3ow1000lw取E=1.03how=^^41.03(ow取E=1.03how=^^41.03(ow10000.00053136000.48)2/3=7.35mm2.840.0010293600how'=1.03()2/3=11.31mm10000.48取板上清液高度为hL=60mmhw=60-7,35=0.05265mh2.840.0010293600how'=1.03()2/3=11.31mm10000.48取板上清液高度为hL=60mmhw=60-7,35=0.05265mhw=60-11.31=0.04869m⑶弓形降液管宽度wd和截面积Af,lwAf…-Wd…由=0.6查图(P127页弓形降液管的宽度与面积图)得=0.052=0.1DAtD所以Af=0.052AT=0.052X0.5024=0.02612m2Wd=0.1D=0.1X0.8=0.08m所以依式计算液体在降液管中的停留时间精福段：声3600AfHT36000.026120.35,==17.217s>3~5s(故设计合理)Lh0.00053136003600AfHt36000.026120.35Lh-0.0010293600=8.884s>3~5s（故设计合理）⑷降液管低隙高度Lhhoho.=3600lwu。u。=0.08m/s精微：ho=提储：h。’精微：ho=提储：h。’36000.480.0836000.001029==0.02679m>0.006m36000.480.08故降液管设计合理，选用凹形受液盘hw=52.65mmhw'=48.69mm2、塔板布置⑴塔板的分块因D>800mm故塔板采用分块式，塔板查表可知分为3块⑵边缘区宽度确定取Ws=Ws'=0.04mwc=0.03m⑶开孔区面积计算AaAa=2(x标谓sin点x=T—(wd+ws)=^.p-0.08-0.04=0.28mr=D-wP=0.8-0.03=0.37m2c2故A0t=2(0.2840.372-0.282+3.14父0.372sin—簪)=0.3703m21800.37

⑷筛孔计算及其排列选用小3mm碳钢板，取筛孔直径do=4.5mm筛孔按正三角形排列，取孔中心距t为t=3.1d。=3,1x4.5=13.95mm1.155A-.1.1550.3703筛孔数目n为n=-==2198个t2（13.95x10—四开孔率80.907（上）2=0.907X（工）2=9.44%t3.1气体通过阀孔的气速精微段uo=-Vs-=O6657=19.04m/sA：.0.09440.3703提储段u。'上=0.6586=18.84m/sA；0.09440.3703（七）塔板的流体力学验算1、塔板压降⑴干板阻力hc计算：（由生=竺=1.5查资料附表图3-14干筛孔的流量系数有Co=0.82）c3①hc=0.051（比）2—=0.051x（19^4）2x1^94=0.0369m液柱c6PL0.82814.8u。。Pv18.84。0.8427②hc，=0.051(-)2一=0.051M()2父=0.0242m放枉c。pl'0.82919.48⑵气体通过液层的阻力hlMhlVsAtVsAt-Af0.66570.5024-0.02612=1.3977m/sF。=ua#=1.3977^1?094=1.4619Kg?/(sm)?查资料附表图3-15充气系数关联图，由F。=1.4619得P=0.59hC=PhL=P(hw+how)=0.59X(0.05265+0.00735)=0.0354m液柱At-Af0.65270.5024-0.02612=1.371m/sF。'=ua'Jpv'=1.371M，0.8427=1.258Kg?/(sm)?查资料附表图3-15充气系数关联图，由F0'=1.258得P'=0.62hc，=P'hL'=P'(hw，+h0w')=0.62M(0.04869+0.01131)=0.0372n®柱

⑶液体表面张力的阻力h瓷hj计算h=4QL=-4-3594_1°__L=3.99m10-m=0.00399m液柱-：Lgd。814.89.810.0045h^=-^L-=4'56.0"10=5.51父10-m=0.00551m液柱pL'gdo919.48父9.81父0.0045气体通过每层塔板的液柱高度hp及hp'计算h=hc+hi+h产0.0369+0.0354+0.00399=0.07629m液柱ph。'=hcf+hi+h/=0.0242+0.0372+0.00551=0.0669m液柱p气体通过每层塔板的压降APp及APp'计算△Pp=hppeg=0.07629x814.8x9.81=609Pa<0.7KPa（设计允许值）△Pp'=hp'p-g=0.0669m919.48父9.81=603.44Pa<0.7KPa（设计允许值）2、液面落差对于筛板塔，液面落差很小，且本方案的塔径和液流量均不大，故可忽略页面落差影响。3、液沫夹带液沫夹带量ev及％'计算5.76106,ev=（（TL5.76106,ev=（（TL」^）3.2=5.76106（1.3977）3.2Ht-hf35.941030.35-0.15，5.76106ev=JL?=0.07986Kg液/Kg，5.76106ev=JL?父（ua?）3.2=5.76父106/（1.371）3.2‘Ht—hf，56.05^103'0.35-0.15，=0.0489Kg液/Kg气<0.1Kg液/Kg气故在本设计中液沫夹带量ev及在允许范围内4、漏液对筛板塔，漏液气速U0,min（U「,min）由下式计算①u。,min=4.4C°jE+0五=4.4"81.陛瓯0垣叵0匹1^=9.435W'pv'001.094实际孔速Uo=19.04m/S>U,min

u。19.04,稳te系数K===2.02>1.5u。,min9.435②u，，min"4C。件0056+0.13廿h”L=4.4,0.82,八0.0056+01艺0.06-0.00551)乱^转由隗的,\pv，V0.8427实际孔速U。’=18.73>U。：min稳定系数K'=-^=曳臾=1.8>1.5U；min10.555、液泛为防止塔内发生液泛，降液管内液层高Hd及Hd'应服从下式Hd<5(叫+%)[中取0.5];Hd'w邛(片，+hw，)邛(Hr+hw)=0.5X(0.35+0.03882)=0.19441m液柱邛(Ht'+hw')=0.5X(0.35+0.04869)=0.199m液柱而Hd=hp+h|_+hd；Hd=hp'+hj+hd'板上不设进口堰hd=0.153(u。)2=0.1530.082=0.001m液柱hd=hd=0.001m液柱Hd=hp+hL+hd=0.07629+0.06+0.001=0.13729m液柱<0.19441m液柱HT=hp'+hL'+hd'=0.0669+0.06+0.001=0.1279m液柱<0.199m液柱故在本设计中不会出现液泛现象（八）塔板负荷性能图1.漏液线由U0,min=4.4C0J(0.0056+0.13hL—K)Pl//U0,min-U0,min-A0hL=hw-h0w,2.84匚how-E1000八、2/3Lh<lw」Lh工Vs,min=4.4/4“0.0056+0.13%+裳E(M)2/3Lh——Pl/Pv11:1000lw_2/3I2.84f3600Ls)1814.8=4.4x0.82x0.0944x0.37030.0056+0.130.05265+父1.03sI1—0.00399》11000I0.48)j1.094Vs,min=3.44110.0088545+0.1457Ls2/3「..,2/3।同理可得Vsmin'=4.4c0A0jd0.0056+0.13hw'+理E』—h八-P「/TML1000JwJj=4.4S82，0.0944M0.370310.0056+0.130.04869召VI1000M1.03,2门一0.0055：00.48[j0.8427VS,min=4.1540.00642+0.1457LS在操作范围内，任取几个LS(Ls')值，依上式计算出VS(VS')值，计算结果列于下表:3Ls(Ls),m/s0.00050.00100.00150.0020Vs,m3/s0.3400.3490.3570.364VW,m3/s0.3340.3360.3380.340由上表数字即可作出漏液线①2、液沫夹带线以ev=0.1kg液/kg气为限，求Vs-Ls关系如下3.25.7父10上iUa或lHT-hf/—―=S=2.0997VSAT-Af0.5024-0.02612how2.84〜i/3600LS⑵3

父1.03.Y1000I0.48J=1.1208Ls2/3%=2.5、=2.5hwhow=2.50.038821.1208LS2/3=0.090752.802LS2/3Ht-hf=0.259-2.802LS2/35.710-35.9410，2.0997Vs2/30.2592-2.802LS、3.2=0.1整理得VS=0.9245-9.994Ls2/3同理可计算出小矗噜2.0997Vs0.2592-2.802L同理可计算出小矗噜2.0997Vs0.2592-2.802LS2/332=0.12/3整理得VS=0.9368-11.50LS在操作范围内，任取几个Ls）值，依上式计算出Vs值,计算结果列于下表:0.00050.00100.00150.0020Vs,mVs,m3/s0.8620.8250.7930.766Vs',m3Vs',m3/s0.8640.8220.7860.754由上表得出液沫夹带线②3、液相负荷下限线对于平直堰，取液上液层高度how=0.006m,作为最小液体负荷标准，由下式得2.84howE1000取E=1,则3600LS

lw2/3=0.006,0.00610000.4843,LSmin4.09410m3/s2.843600同理，Ls,mi「=4.094M10“m3/s据此作出气体流量无关的垂直液相负荷下限图③4、液相负荷上限图以。=4s作为液体在降液管中停留时间的下线，由下式得「3=4LSLs,maxAfHT0.026120.3533,=2.285510m/s故LSmax=2.285510”m3/sS,max据此可以作出与气体流量无关的垂直液相负荷上限图④5、液泛线令Hd=(Hthw)Hd=hph|hd,hpzhch|h,1^hw%由联立得由Ht+(邛—P—1)hw=(P+1)how+hc+hd+h6忽略hg将how与Ls，hd「Ls，hc与v初关系式带入上式，并整理得：Vs2=b-cLs2-dLs2/3a'=叨5L(U)=(AoC。)2「0.0512(10.09440.37030.82)21.094=0.0833814.8b'hq：'：HT(：---1)hw=0.50.35(0.5-0.59-1)0.03882-0.1327式中，.0.1530.1533c=22=3.47210(lwho)(0.480.01383)3-36002/3336002/3d=2.8410E(1-)()=2.84101.03(10.59)()=1.782lw0.48故0.0833/S2=0.1327-3.472103LS2-1.782LS2/3222/3VS2=1.59-41680.67LS2-14.14LS同理得0.057Vs2=0.1204-925.26Ls2-1.82L”3Vs2=2.11-16232.6LS2-31.93Ls2/3LS(Ls),m30.00050.00100.00150.0020VS,m3/s1.2211.1861.1451.095-3Vs,m/s1.3801.3321.2861.240在操作范围内，任取几个LS(Ls')值，依上式计算出VS(VS')值，计算结果列于下表＜九＞换热器的设计1、冷凝器的选择有机物蒸气冷凝器设计选用的总体传热系数一般范围为500-1500kcal/(m2.h.C)本设计取k=600w/（m2.C）出料温度：64.6C（饱和气）一（饱和液）64.6C冷却水温度：30c—40c逆流操彳:At1=34.6C拉2=24.6C△ti-At234.6C-24.6C4m=-At；1n瓦,34.6ln24.6=28.97C传热面积：A=-Q—在此温度下，查化工原理＜第三版＞附录得学甲=1200KJ/Kg,7水=2378KAtmKJ/KgQ而?=pvVs[xD,+(1-xd)yk]=1.094X0.6657X[0.9947X1220+(1-0.9947)X2378]=0.7303X1226=895.35KJ/s八895.35103「A==51.5m260028.97设备号型公称直径公称压力管程数管子根数中心排管数管程流通面积换热管长度计算换热面积啦52.5X600mm1.6MPa2232160.0364m23000mm52.8m22、再沸器的选择选用120c饱和水蒸气加热，传热系数取K=600w/（m2.C）料液温度：99.6C—100c热流体温度：120c—120c逆流操彳:=20C&2=20.4C△t1-At2?_20-20.4_r==20.2,At/,20InInAt2‘20.4=0.8427X0.6586=0.555Kg/s*+（1-xw）京查表知此温度下丁甲=1100KJ/Kg京=2400KJ/Kg=0.002818X1100+(1-0.002818)X2400=2396KJ/Kg8'=s'7=2396X0.555=1329.8KJ/sA，Q'1329.8^103.cc”OA===109.72m2KAtmz60020.2设备型号公称直径公称压力管程数管子根数中心排管数管程流通面积换热管长度计算换热面积蚣X2.5700mm4.00MPa4322210.0253m24500mm111.2m2（十）福塔接管尺寸计算1、接管①进料管的结构类型很多，本设计采用直管进料管，管径计算如下:取U取Uf=1.6m/s25c进料，此温度下锌=786.9Kg/m3你=996.95Kg/m325c进料，此温度下锌=786.9Kg/m3你=996.95Kg/m3（查化工原理（上）附录）11ce^XF=0.20871-0.2087=944-34Kg/m3—++。甲P水786.9996.95F11557.Vs===0.000743m3/s3600Plp3600944.34D=4Vs40.000743M==0.024m=24mm二uf.3.141.6查标准系列取卷2X3②回流管采用直管回流管取UR=1.6m/s4Ls40.000531人=；=0.065m二ur.3.141.6③塔釜出料管取uw=1.6m/s4Ls'Uw4-1.029—③塔釜出料管取uw=1.6m/s4Ls'Uw4-1.029—1033.141.6=0.029m=29mm查表取查表取38x3④塔顶蒸气出料筒直管出气，取出口气速u=20m/sD=40.66573.14D=40.66573.1420=0.206m=206mm查表取查表取4273X8⑤塔釜进气管采用直管取气速u=23m/s