化工原理课程设计

目录1、前 2、塔的工艺计 2.1浮阀塔的物料衡 2.2理论实际塔板的计 目录1、前 2、塔的工艺计 2.1浮阀塔的物料衡 2.2理论实际塔板的计 2.3精馏塔内各物性参数的计 2.4塔径的初步设 2.5溢流装置的设计计 2.6塔板布置及浮阀排 3、流体力学验 3.1气相通过浮阀塔板的压力 3.2淹 3.3.雾沫夹带验 3.4塔板负荷性能 4、浮阀塔工艺设计结 5、精馏塔的辅助设备设计的设计与选 5.1接管尺寸的确 5.2冷凝器的选 5.3再沸器的选 5.4除沫器的选 6、主体设备机械设 6.1塔体强度校 6.26.1塔体强度校 6.2裙 6.3吊 6.4人 6.5塔的总体高度设 7、课程设计心 8、参考文 摘要摘要:1.94827.3块，计算出全塔效率为AbstractAbstract:Afloatvalvedistillationtowerisdesignedtoseparateethanolandwater.Thedesignincludesdeterminationofthedistillationprocess,optimalrefluxratiothrougheconomicaccounting,calculationofthedistillationcolumnsizeandselectionofauxiliaryequipment.Theethanol-watersolutionisanon-idealphysicalsystem.Theminimumrefluxratiowas1.848bymappingmethod.Theoptimalrefluxratiois4.74byprogrammingthedistillationcostmodel.Thetheoreticalplatenumberwas27.3,theefficiencyofthewholetoweris52.94%,sotheactualplatenumberwas51,ofwhichtherectifyingsection43andthestrippingsection8,thefeedinglocationisthe44thplate.Thediameterofdistillationtoweris1.2meters,thetotalheightoftoweris23.865meters;Theaperturerationofplateis8.67%,theoperatingflexibilityoftherectifyingsectionis5.014andofthestrippingsectionis4.89.Throughcalculatingthefluidmechanicsofthefloatvalvetowereverytargetanddataisuptostandard.Thematerialofthetowerbodythethicknessofthewallis12mm,Strengthcheckingshowsthatthedistillationtowermeetsthestrength,stiffnessandstabilityKeywords:ethanol-water，distillation，floatvalvetower，optimalreflux乙醇-水溶液连续精馏乙醇-水溶液连续精馏塔优化设1精馏问题进行分析选取计算核算绘图等是较完整的精馏设计过程20.343/M乙醇M水xF=20.343/M乙醇M水xF=0.343/46+0.6750.94/0.94/46+0.06==0.0005/0.0005/46+0.9995MF==1-=46·0.169634025+18·(1-=22.74975kg/F=512.8261kmol/300·24·F=DFxF=DxF+Wx得1 512.8261 101.0893 0.e=e000X????2根据Rmin=(x0.e=e000X????2根据Rmin=(xD-ye)/(ye-xe 算出最小回流比Rmin=根据经验得R1.4RminRxR R提馏段操作线：y2.10x2.143·10-Y????0.....000X???Y??0.....000X???Y???? 用内插法求出tFtDtW83.85-83.75=tF-t=F16.77- 16.96-78.2-78.17=tD-t=D85.97- 85.98用内插法求出tFtDtW83.85-83.75=tF-t=F16.77- 16.96-78.2-78.17=tD-t=D85.97- 85.98-99.9-99.8=tW- =W0.004- 0.0195-t1=(tF+tD)/2=提馏段平均温度=(tF+tD)/2=1=aB（质量分率混合气密度rv t1=81.01-81.1= x=1x- 36.02-181.01-81.1= y=1y- 59.84-1ML1=46·0.3684+18·(1-0.3684)=28.32kg/MV1=46·0.6025+18·(1-0.6025)=34.87kg/ t2=91.9-91.3=91.88-91.9=2 x2-91.9-91.3=91.88-91.9=2 y2-ML2=46·0.0374+18·(1-t2=91.9-91.3=91.88-91.9=2 x2-91.9-91.3=91.88-91.9=2 y2-ML2=46·0.0374+18·(1-0.0374)=19.05kg/MV2=46·0.2813+18·(1-0.2813)=25.88kg/85- =r乙醇733.99kg=730 r乙醇11 85- =81.01-85r=971.15kg/968.6- r-t2=91.88℃，同理得 =722.50kg/乙醇3r水964.0kg21=0.3684·46/0.3684·46+18·(1-0.3684)]+1-=1.2055·10-31= 精馏段气相密度：1=0.0374·46/0.0374·46+18·(1-0.0374)]+1-=1.0687·10-rL= =0.86kg/m3提馏段气相密度：精馏段挥发度：由xA10.3684yA10.6025=0.6316，yB1==0.6025·0.6316=a1提馏段挥发度：由xA20.0374yA20.2813=0.6316，yB1==0.6025·0.6316=a1提馏段挥发度：由xA20.0374yA20.2813xB=0.9626，yB= =a20.7187查得s乙醇s提馏段平均温度：t2 查得s乙醇ssm(精x乙醇sx水s水0.6316·0.01490.0625·0.36840.0324Nsm(提x乙醇sx水s水0.9626·0.01360.0605·0.03740.0154Nn水1 =1.04642·10-5Pa乙醇提馏段平均温度t291.88m乙醇=1.07969·10-5Pa2m水3.07769·10Pa2mLm乙醇x1m水(1x10.0105·0.36840.3499·(10.3684)0.2249mPa111mLm乙醇x2m水(1x20.0108·0.03740.3078·(10.03740.2967mPa2222.3.6V=mLm乙醇x2m水(1x20.0108·0.03740.3078·(10.03740.2967mPa2222.3.6V=(R+1)D=(2.73+1)·101.09=377.07kmol/=275.98·28.32=9.42m3/V=377.07·34.87=10957.03m3/V'=V+(q-1)F=V=377.07koml/=788.81·19.05=15.58m3/V=377.07·25.88=11347.18m3/2.3.7全塔效率ET和实际塔板ET0.49(amL)-0.2450.49·(2.6·0.2249)-0.24543(圆整1ET0.49(amL)-0.2450.49·(10.07·0.2267)-0.245=4-=82= 43+PrL-2.4.1u(0.6~0.8)uumax=LS1·(rL1)1/)1/== rV 取板间距H0.4mh0.06mHh C200.071CC1==0.078m/2020 829.50-u==2.05m/操作孔塔气速u1LS1·(rL1)1/)1/== rV 取板间距H0.4mh0.06mHh C200.071CC1==0.078m/2020 829.50-u==2.05m/操作孔塔气速u10.8umax=1.435m4·10957.03=1.53m,圆整D=111p·36001p22横截面积AT4D1V'空塔气速u S=1.513m/1 TrL-2.4.2u(0.6~0.8)uumax=LS2·(rL2)1/2=)1/= rV 取板间距H0.4mh0.06mH'' TT15.4C=C202==0.069m/20 935.76-==2.28m/u2= =1.824m/' 4·11347.18=1.48m，圆整DD2=23600p2 =p·1.62=T4空塔气速=1.567m/=22A'ThN-1)Ho.4·(51-1)TE0堰长lw=(0.6~0.8)D=0.7D采用平直堰，堰上高度lA2/h· owlw空塔气速=1.567m/=22A'ThN-1)Ho.4·(51-1)TE0堰长lw=(0.6~0.8)D=0.7D采用平直堰，堰上高度lA2/h· owlw 9.422/ =0.017m>ow·1 hw=h- =0.055-0.0117= 15.582/h=0.0164m>=·ow hw=hL-how=0.06-0.0164= 2D=0.7,查图 =0.09,Wd=DAf0.09·2.011Wd=0.15·1.6=AfHT=3600·0.181·0.4=28s>验算：精馏段在降液管内停留时间q3600=17s>提馏段= T精馏段：取液体通过降液管底隙时的流速u00.1mLh=23mm>则h0= =3600·1.12提馏段：取液体通过降液管底隙时的流速u'=0.1m0则= ==39mm>3600·1.12 Lh=23mm>则h0= =3600·1.12提馏段：取液体通过降液管底隙时的流速u'=0.1m0则= ==39mm>3600·1.12 塔，重量为33g，孔径39mm。取板厚d4mm,孔径d039mm，边缘区宽度Wc0.06mWS=取阀孔动能因子F0=12,则孔速=10.95m/==1=237(块1p3600·0.0392404R2arcsinx+R-xRR=D-Wc=1.6-0.06=22x=D-(Wd+Ws)=0.8-(0.24+0.1)=2Aa20.460.742+0.742arcsin0.46浮阀排列方式采用等腰三角形叉排，取同一横排孔心距t=则排间距 = 222取阀孔动能因子F0=12,则孔速 =12.94m/'203(块'3600t·0.03924浮阀排列则排间距 = 222取阀孔动能因子F0=12,则孔速 =12.94m/'203(块'3600t·0.03924浮阀排列方式采用等腰三角形叉排，取同一横排孔心距t=75mm。则排间=== 33.1气相通过浮阀塔板的压可根据hphchL=1.825u0c1==9.50m/rVr因为u01u0c1，故hc15.340=5.34=2rL12取e00.5hL1e0hL0.5·0.055度hp1=0.0275+0.047=DPp=hpPLg=0.0745·829.5·9.8= u0c=11.41m/==ru0.86·5.34rv2=因为u02u0c2，故hc25.34=5.342rL2u0c=11.41m/==ru0.86·5.34rv2=因为u02u0c2，故hc25.34=5.342rL2·935.762取e00.5hLe0hL0.5·0.062度hp2=0.0419+0.03=DPP=hpPLg=0.0719·935.76·9.8= 3.2为防止淹塔现象，要求控制降液管中清液高度Hd£F(HThW),即Hd=hp+hl+hd，hp1=hL1=L=0.153·( )=h=S1lh1.2wHd＝0.0745+0.00158+0.055=1取F0.5（H+h=0.5·(0.0433+0.4)=FW1\Hd1=0.156<，hL=2hp=2)2=h=0.1531.12·0.039Hd＝0.0719+0.06+0.0015=2取F0.5 +hFTW22V+1.36LSSr-F取F0.5 +hFTW22V+1.36LSSr-F ZLD2Wd=1.62·0.24·829.50-F=71%<·935.76-F=62%<3.43.4.1V+1.36LSSr-由F rV +1.36LZSSr- 0.8KCFV+1.36LSS829.50-=代入数据得：Vs3.58-同理得：Vs4.44-F(HT+hw)=hp+hl+hd=hc+h1+ rV +1.36LZSSr- 0.8KCFV+1.36LSS829.50-=代入数据得：Vs3.58-同理得：Vs4.44-F(HT+hw)=hp+hl+hd=hc+h1+hs+hl+忽略其中的 rvu0+)2/3F(HT+hw)=5.34+(1+e0)hwlwh0其中u0pd22)140.22165=5.34· p · +0.153(L)S11.12829.50·2·9.81)2S 222V=31.87-46890.5L-3SSS2SSSAf==（Lssq5p2F=5V=dS04p5=p·0.0392·2275=1.292精馏段：Vs=d2s014r4vp5=p·0.0392·5=1.3072=dss044rv取堰上液层高度how=0.006m作为液相负荷下限条件作出液相2.84E(360p2F=5V=dS04p5=p·0.0392·2275=1.292精馏段：Vs=d2s014r4vp5=p·0.0392·5=1.3072=dss044rv取堰上液层高度how=0.006m作为液相负荷下限条件作出液相2.84E(360LSmin =lWE=1.0,（L）9.55·10-4ss8642002468Ls?4 418642002468Ls?5置按固定的液气比，由图查出精馏段的气相负荷上限(VS)max=5.30,气相负下限(V8642002468Ls?5置按固定的液气比，由图查出精馏段的气相负荷上限(VS)max=5.30,气相负下限(Vs)min=3.53。提馏段塔板的气相负荷上限(VS)max=5.78，气相负荷下限(Vs Vmin=5.30 Vmin=5.78 4143精馏段hL提馏段hL精馏塔u/(m.s-提馏塔u/(m.s-43精馏段hL提馏段hL精馏塔u/(m.s-提馏塔u/(m.s-溢流堰长度lwAf降液管高度Wd精馏段h0提馏段h0精馏段u0m.s提馏段u0m.s孔阀中心距t精馏段t/提馏段t/3取uf2.0msrf829.50kgV=22.75·513=0.00391m3/f4·0.00391=则管径==f3取uf2.0msrf829.50kgV=22.75·513=0.00391m3/f4·0.00391=则管径==fpfm3V -=·Ss829.504p=取 =2.0m/s,则d精馏段q/提馏段q/Lm3sLm3s=WMW=(788.81-=0.0022m3/rW =WMW=(788.81-=0.0022m3/rW =38mm取UW2.0msdw=PN6DN50，4·11347.18=D= PN6DN250l43600pD==PN6DN500H0=0.4·6+3+323H=H-q·0.01=8.4-0.01·(3.672·10)=- q=hqrg=7.8·3.672·10-3·9.81·882.63= 塔顶温度tD78.20rA=850kJ/rB=2313kJ/平均r850·0.8598·462314·(10.8598)·1839455.2668kJQC=Vr塔顶温度tD78.20rA=850kJ/rB=2313kJ/平均r850·0.8598·462314·(10.8598)·1839455.2668kJQC=Vr=(R+1)Dr=3