wdi精餾塔設(shè)計(jì)說(shuō)明書-附錄五

附錄目 附錄目 塔體計(jì) 1.3.6筒 1.3.7封 1.3.8裙座的相關(guān)尺寸計(jì) 配體計(jì) 原料 管件計(jì) 液流 1.1物料衡算及塔板計(jì)1.1.1全塔物料衡原料液、塔頂及塔底產(chǎn)品的摩爾分表1- 乙醇-水相關(guān)物性參數(shù)MMwD1 1.1物料衡算及塔板計(jì)1.1.1全塔物料衡原料液、塔頂及塔底產(chǎn)品的摩爾分表1- 乙醇-水相關(guān)物性參數(shù)MMwD1 0.881x0.951DM Mww-1- 0.020x0.051wM M 0.443xwF1 0.671FM 乙醇 水 原料液、塔頂及塔底產(chǎn)品的平均摩爾質(zhì)MDxDMA1原料液、塔頂及塔底產(chǎn)品的平均摩爾質(zhì)MDxDMA1xDMBMFxFMA1xFMBMwxwMA1xwMB1.1.1.3物料衡算進(jìn)料處理F1.1.1.4總物料衡算(間接蒸汽加熱FWFxFWxw1.1.2實(shí)際回流1-xyxy00最小回流比及實(shí)際回流比3.2最小回流比及實(shí)際回流比3.2R=(1.1-1-1.1.2.2R（1）精餾段操作線方程： xDRnRRF xn xw1.2735xn0.2735xwRR1.1.2.3氣、液相熱負(fù)荷計(jì)1.1.3理論塔板數(shù)確0.021812塊理論板1-xy12345671.1.3理論塔板數(shù)確0.021812塊理論板1-xy123456789--實(shí)際塔板數(shù)確E)0TLL——塔頂與塔底平均溫度下的液相粘度表1- sααtdt78.1782.56122x1=0.4380；y1數(shù)據(jù)手冊(cè)中內(nèi)插得該溫度下乙醇的黏度A10.42mpas，水的粘度B10.3546mpatdt78.1782.56122x1=0.4380；y1數(shù)據(jù)手冊(cè)中內(nèi)插得該溫度下乙醇的黏度A10.42mpas，水的粘度B10.3546mpas11- 1lgμL10.4380lg0.42ET10.49(1L1 0NEtwt95.582.56提餾段平均溫度222x20.37mpas0.3201mpas1y1x222lgL2x2lgA2(1x2)lgμL2L2)02 1(7-NtPEtNpNp1L2)02 1(7-NtPEtNpNp1Np225+16=4126ENT-1180.439TNP精餾塔的工藝條件及有關(guān)物性數(shù)據(jù)計(jì)1.1.5.1操作壓力計(jì)Pm1105.32Pm2124.921.1.5.2操作溫度計(jì)塔頂溫tD78.17CtF82.56CtD2tF21.1.5.3平均摩爾質(zhì)量計(jì)MLDmxDMA(1xD)MB0.825246(10.8252)1841.1056kg/MVDmy1.1.5.3平均摩爾質(zhì)量計(jì)MLDmxDMA(1xD)MB0.825246(10.8252)1841.1056kg/MVDmyDMA(1yD)MA0.838746(10.8387)1841.4836kg/MLFmxFMA(1xF)MB0.670146(10.6701)1836.7628kg/MVFmyFMA(1yF)MB0.735846(10.7358)1838.6024kg/MLWmxWMA(1xW)MB0.012046(10.0120)1818.336kg/（1）MLDm38.9342kg/M2MVDm40.043kg/M2MLFm27.5494kg/M2 MVFmMVWm29.8636kg/21.1.5.4平均密度計(jì)氣相平均密度計(jì)算：由理想氣體狀態(tài)方程，即Pmm1/ 注：iA3B972.832kg/30.8252D0.825246(10.8252)1753.8kg//(1)/ 進(jìn)料板平均密度計(jì)算：由進(jìn)料溫度tF82.56C732.3535kg/，A3B0.8252D0.825246(10.8252)1753.8kg//(1)/ 進(jìn)料板平均密度計(jì)算：由進(jìn)料溫度tF82.56C732.3535kg/，A3B970.136kg/mF1762.54kg//(1)/ A722.3555kg/mtw95.5CB961.505kg/m，w1952.02kg//(1)/ Lm1(LDmLFmPm1MVm11.5686kg/Lm2(LFmLWm)127.729.86361.2671kg/Pm28.31液體平均表面張力計(jì)1/m1/1/sWsO并用下列關(guān)聯(lián)式求出sWBq sOA液體平均表面張力計(jì)1/m1/1/sWsO并用下列關(guān)聯(lián)式求出sWBq sOABAqV2/ QWO2/TWq(xWVWxOVOO(xWVWxOVOVW——表示水的摩爾體積；VO——有機(jī)物的摩爾體積(1）o17.5mN/w62.2mN/tm1=80.365℃，qx1y11000M62.6cm3/V0ρ01000M18.5cm3/VwρwφwxwVw/xwVwx0V0φ01φwB㏒/φ0q22σοVοQ0.411qσV3wTqABQqA㏒sw2φ22σοVοQ0.411qσV3wTqABQqA㏒sw2φsOφsw0.138;φso1/m1/1/ 21.39mN/w60.6mN/o16.7mN/qx2y21000M62.77cm3/V0ρ01000M18.6cm3/VwρwφwxwVw/xwVwx0V0φ01φwB㏒/φ0q22Q0.411qσ T3w qABQ-qA㏒sw2φABQ-qA㏒sw2φsOφsw0.545;φso1/m1/1/ 35.47mN/1.1.5.6液體平均黏度計(jì)lgLmxilg塔頂平均黏度計(jì)算：由tD78.17C，查手冊(cè)得進(jìn)料板平均黏度計(jì)算：由tF82.56C，查手冊(cè)得μA0.395，μB0.3454塔底平均黏度計(jì)算：由tw95.5C，查手冊(cè)得μA0.335，μB0.2978μ0.335001200.2978（1-00120）22精餾塔的塔體工藝尺寸計(jì)1.1.6.13.5268.4840.0431.7287m3/V1M 36002.5268.4838.93420.002462m3/L2M 3600s1(精餾塔的塔體工藝尺寸計(jì)1.1.6.13.5268.4840.0431.7287m3/V1M 36002.5268.4838.93420.002462m3/L2M 3600s1(lm1)1/0.029，取 0.4m，板上清液高度0.05m,則hTLTLV 'C(L0778.515 1.16m/u0.7umax0.811m/4D按標(biāo)準(zhǔn)塔徑圓整后為：AD22.54m2T4u1.7090.673m/ VMvm240.74×29.86361.5761m3/ S3600424.3727.54940.00379m3/LMLm S36000.0551，取 0.4mS2 lM2)1/h0.05m板上清液高度VTLS vM0.0551，取 0.4mS2 lM2)1/h0.05m板上清液高度VTLS vMHThL'C(L0876.55 0.1002.44m/u0.7umax1.71m/D按標(biāo)準(zhǔn)塔徑圓整后為：AD22.54m2T4uVS1.57610.62m/ 1.1.6.2精餾塔高度計(jì)1.1.6.2精餾塔高度計(jì)Z1(NP11)HT270.4Z2(NP21)HT70.4ZZ1Z20.51.2精餾塔工藝計(jì)精餾段塔板工藝尺寸的計(jì)1.2.1.1溢流裝置計(jì)因塔徑1.2.1.1.1堰長(zhǎng)取lw0.6D1.2.1.1.2溢流堰高度2.841(0.0021773600)2/30.01061.2.1.1.1堰長(zhǎng)取lw0.6D1.2.1.1.2溢流堰高度2.841(0.0021773600)2/30.0106m2.84E(Lh)2/3 o w所以選用平直堰,取板上清液層高度hL50mm，故hwhLhow1.2.1.1.3弓形降液管寬度Wd和截面積D0.60Af0.055由wADTAf0.055AT0.0552.54wd0.12D0.121.83600AfHT36000.13970.425.67s1.2.1.1.4降液管底隙高度h0lw取u0.07ms，則h001.08'故降液管底隙高度設(shè)計(jì)合理，選用凹形受液盤，深度hw80mm1.2.1.21.2.1.2.1塔板分1.2.1.2.2邊緣區(qū)寬度確取W'，W c1.2.1.2.3鼓泡區(qū)面積的計(jì)鼓泡區(qū)面積Aa計(jì)算xD/2(wdws1.2.1.21.2.1.2.1塔板分1.2.1.2.2邊緣區(qū)寬度確取W'，W c1.2.1.2.3鼓泡區(qū)面積的計(jì)鼓泡區(qū)面積Aa計(jì)算xD/2(wdws)0.9(0.2040.216)rD/2wc0.90.04A2(xr2x2r2sin1x)2(0.6240.8620.62420.862sin10.624)1.94mar1.2.1.2.4篩孔計(jì)算及其排d0F1F0u0ρV 3.140.0392t A0開孔率為：0D提餾段塔板工藝尺寸設(shè)1.2.2.1溢流裝置計(jì)1.2.2.1.1堰長(zhǎng)取lw0.6D1.2.2.1.2溢流堰高度由hwh提餾段塔板工藝尺寸設(shè)1.2.2.1溢流裝置計(jì)1.2.2.1.1堰長(zhǎng)取lw0.6D1.2.2.1.2溢流堰高度由hwhLhow2.84E(Lh)2/32.841(0.00323)2/3 o w取板上清液層高度hL50mm，故hwhLhow1.2.2.1.3弓形降液管寬度Wd和截面積D0.60Af0.055由wADTAf0.055AT0.0552.54故wd0.12D0.121.83600AfHT36000.13970.417.3s0.003231.2.2.1.4降液管底隙高度LSh0ulw3600取u0.07ms，則h0.043m.(0.02-0036001.08'故降液管底隙高度設(shè)計(jì)合理，選用凹形受液盤，深度hw80mm1.2.2.21.2.2.2.1邊緣區(qū)寬度確取W' W， c1.2.2.2.2鼓泡區(qū)面積的計(jì)3600取u0.07ms，則h0.043m.(0.02-0036001.08'故降液管底隙高度設(shè)計(jì)合理，選用凹形受液盤，深度hw80mm1.2.2.21.2.2.2.1邊緣區(qū)寬度確取W' W， c1.2.2.2.2鼓泡區(qū)面積的計(jì)鼓泡區(qū)面Aa的計(jì)xD/2(wdws)0.9(0.060.216)rD/2wc0.90.04A2(xr2x2r2sin1x)2(0.6240.8620.62420.862sin10.624)1.94mar1.2.2.2.3篩孔計(jì)算及其排F0u0ρV4 3.140.0392t A0開孔率為：0D1.2.3.1精餾1.2.3.1.1塔板壓降核(1）干板阻力hc計(jì)算u09.783m/u1.2.3.1精餾1.2.3.1.1塔板壓降核(1）干板阻力hc計(jì)算u09.783m/u10.37m/00u9.7830hc01.990.0381m(2）氣體通過(guò)液層的阻力(ε00.45h1(hwhow0.450.050.0225m(3）液體表面張力阻力計(jì)hphchlPhpLg462.8Pa(260pa530pa(設(shè)計(jì)允許1.2.3.1.20.5 1.080.029hlHdhphdhlHtHw0.50.441HtHw液體降液管里停留時(shí)間核0.13970.435.7SτAf1.2.3.1.4液體降液管里停留時(shí)間核0.13970.435.7SτAf1.2.3.1.4過(guò)量霧沫夾帶核查泛點(diǎn)負(fù)荷因數(shù)cf1.2.3.1.5嚴(yán)重漏液核F0121.2.3.2提餾1.2.3.2.1塔板壓降核(2）干板阻力hc計(jì)算u010.892m/u00u12.850hc01.990.03448m0.45(4）氣體通過(guò)液層的阻h1(hwhow0.450.50.0225m(5）液體表面張h1(hwhow0.450.50.0225m(5）液體表面張力阻力計(jì)hphchlPhpLg490Pa(260pa530pa(設(shè)計(jì)允許1.2.3.2.20.5 1.080.043hlHdhphdhlHtHw液體降液管里停留時(shí)間核0.13970.417.3SτAf1.2.3.2.4過(guò)量霧沫夾帶核AA2A2.2720.125 f查泛點(diǎn)負(fù)荷因數(shù)1.2.3.2.5嚴(yán)重漏液核F0121.2.4塔板的負(fù)荷性能1.2.4.1精餾1.2.4.1.1漏液線55π0.039242NVo1.2.3.2.5嚴(yán)重漏液核F0121.2.4塔板的負(fù)荷性能1.2.4.1精餾1.2.4.1.1漏液線55π0.039242NVoρv1.2.4.1.2液沫夾帶1.36LVSS0.11Vs4.1091.2.4.1.3液相負(fù)荷下how0.006m作最小液體負(fù)荷2.84E(3600Ls)2/ lwLS,min1.2.4.1.4液相負(fù)荷上限作液體在降液管中停留時(shí)限Af0.13970.40.0112m3/ S5液泛aNLbH液泛aNLbHT(ε1)hw0.50.4(0.50.451)0.0394c0.153/(lwh0)0.153/(1.080.029) 2/dE(1ε)(0.667)lw圖1- 精餾段負(fù)荷性能1由圖得到VS,max3.418m3s，VS0.7158m3/V操作彈性為：S,max 1.2.4.2提餾1.2.4.2.1漏液線55π0.039242NVoρv1.2.4.2.2液沫夾帶1.36LVSS0.111.2.4.2提餾1.2.4.2.1漏液線55π0.039242NVoρv1.2.4.2.2液沫夾帶1.36LVSS0.11Vs4.861.2.4.2.3液相負(fù)荷下how0.006m作最小液體負(fù)荷2.84E(3600Ls)2/ lw0.00092m3/LS1.2.4.2.4液相負(fù)荷上限作液體在降液管中停留時(shí)限Af0.13970.40.0112m3/ S51.2.4.2.5液泛aNLbHT(ε1)hwc0.153/(lwh0)0.153/(1.080.043) 2/c0.153/(lwh0)0.153/(1.080.043) 2/dE(1ε)(0.667)lw9.33 222/VSS圖1- 由圖得到VS,max2.7m3s，VS,min0.6614m3V2.71.3塔體計(jì)塔體結(jié)構(gòu)塔的頂部空間高HD1200mm1.3.2塔的底部空間高5minHB(L2t60)/AT0.61.3.3進(jìn)料板空間高度1.3.3進(jìn)料板空間高度1.3.41.3.5總體HHDNP2SHTSHPHF式中：HD--HP--開有人孔的塔板HF--HB--塔底空間高度N—實(shí)際塔板數(shù)S—人孔數(shù)目（不包括塔頂空間和塔底空間人孔1.3.6壁厚選6mm,選用材質(zhì)為A31.3.7本設(shè)計(jì)采用橢圓形封頭，由于直徑1800mm，查的曲面高度h1450mm,h140mm,選用封頭D1800g1.3.8裙座的相關(guān)尺寸1.4配體計(jì)1.4.1回流冷凝1.3.8裙座的相關(guān)尺寸1.4配體計(jì)1.4.1回流冷凝塔頂氣體：冷凝水20℃---36℃MDxAMA1xAMB0.82524610.82521841.11kg/rArbxArxArA1xArB1235.78kj/qmVMDR1DMD9894.98kg/Qrqm1.22107kj/Δt1-Δt258.2842.28mΔt㏑㏑QA1.4.2原料預(yù)熱120°C2CPA2.8kJ/kg4.2kJ/kgxFCpxFCpA120°C2CPA2.8kJ/kg4.2kJ/kgxFCpxFCpA1xFCpB3.86kJcqFVMF251.1129.61727466.79kg/=t1t210039.9mlnt80.120qFCPt1.4.3原料H。由于存H=(1.05~1.2）He(1.05~1.2)(zp/(g)u2/(2g)Hf12pu z1.2H1.21.31.2z1.87m,u=2m/s,d=0.029m,p=5duρ0.0292803.23Reμ（湍流取管壁絕對(duì)粗糙度d0.250.0290.006查表：摩擦系數(shù)λRe及相對(duì)粗糙度ξ/d的關(guān)系圖知：λ=0.032Re及相對(duì)粗糙度ξ/d的關(guān)系圖知：λ=0.032Hf12