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要求部分进料量F=进料浓度：进料状态：馏出液乙醇浓度≥94%釜液乙醇浓度≤0.5%冷却水进口温度≤25°C冷却水出口温度≤45°C加热蒸汽压力0.4MPa操作压力：加热方式：进料F=摩尔分数xf摩尔分数xd摩尔分数xw平均摩尔质量平均摩尔质量平均摩尔质量转化为摩尔流量F=摩尔流量D摩尔流量W上升蒸汽量S=塔顶D釜液WS=作图得Rm=倍数R=R/(R+1)=xd/（R+1）=精馏段曲线L=RD=L'=W=L+F=V'=V=S=L'/V'=(W/V)*xw=提馏段曲线理论板实际板N塔顶D和进料F汽相的平均摩尔质量塔顶D和进料F液相的平均摩尔质量尺寸计算部分精馏段平均蒸汽流量ρv=精馏段平均液相流量ρl=精馏段上升蒸汽量Vv=精馏段下降液体量Ll=取塔板间距HT=板上液层高度HL=分离空间HT-HL=功能参数（Ll/Vv)*(ρl/ρv)^0.5=查史密斯关联图可得C20=表面张力σ2=C=C20(σ2/20)^0.2=Umas=C√(ρl-ρv)/ρv=安全系数0.6~0.8，取空塔气速u=塔径D=√4V/πu=所以取塔径D=塔横截面积AT=πD2/4=空塔气速u=塔高H塔=HD+(N-2-S)HT+SHT+HF+HW=手孔数目S=N/8-1=约为设塔底停留时间为10min取塔底空间Hw=储蓄液高度ΔZ=L*60*5/A截=进料板空间高度Hf=手孔两板间距Ht=塔顶空间Hd=取溢流堰堰长（0.6~0.8DT)取则lw收缩系数E=1How=（2.84/1000）*E*（L/lw）^2/3=出口堰高Hw=降液管宽度与降液管面积取溢流堰堰长（0.6~0.8DT)取则Wd/D=Af/At=Wd=Af=0.05*π*D^2/4=取停留时间τ=Af*Ht/L=因为Hw-H0=6~12mm所以底隙高度H0=边缘区宽度Wc=安定区Ws=开孔区面积r=D/2-Wc=x=D/2-(Wd+Ws)=x/r=sin-1=则开孔区面积Ap=2{x√(x2-r2)+r2sin(x/r)}=浮阀数目N孔径d0=气体通过阀孔速度（取F=11）u0=F/√ρv=N=4V/π(d0)^2*u0=约为N阀孔排列A0=π*d0^2*N/4=孔间距t=d0√0.907*Ap/A0=等边三角形排列，取孔间距为（75、125、150）浮法数目n取阀孔速u0‘动能因素F（8~12）开孔率Φ=N（d0）^2/D2=流体力学验算部分全开转为全部全开的临界速度uoc=则hc=5.34*u0^2*ρv/2gρl=板上层充气液层阻力hl则hl=εhL=0.5*0.05=表面张力引起的压力hσ忽略单板压降hp=hc+hl+hσ=压降漏液验算取动能因数F0=则uom=F0/√ρv=稳定性系数K=u0/uom=液泛验算hd=0.153(L/lw*h0)^2=则溢流管内清液层高度Hd=hp+hd+hL+hσ=Φ(Ht+Hw)=要求HdΦ(Ht+Hw)雾沫夹带验算查得物性系数K=泛点负荷系数Gf=Zl=D-2Wd=Ab=A截-2Af=Gv=V√ρv/(ρl-ρv)=则F1=(100Gv+136*L*Z)/(Ab*K*Gf)=F1'=100Gv/0.78*A截*k*Gf=均小于80%操作性能负荷图1、气相负荷下限线（漏液线），线1Vs=πd0^2N5/4√ρv=2、过量雾沫夹带线（气相负荷上限线）线2√ρv/(ρl-ρv)=则80=100Gv/0.78*A截*k*Gf80=100V*√ρv/(ρl-ρv)+136*L*Z/Ab*k*Gfa=b=c=方程为aV+bL=c3、液相负荷下限线，线3由0.006=(2.84/1000)*E*((3600Ls/lw)^(2/3))L=4、液相负荷上限线，线4L=Af*Ht/5=5、液泛线，线5a=1.91*10^5*ρv/(ρl*N2)=b=ΦHt+(Φ-1-ε0)hw=c=0.153/(lw^2*h0^2)=d=(1+ε0)E(0.667)*(1/lw^2/3)=方程如下aV^2=b-cL^2-dL^2/3工作线气相负荷下限气相负荷上限液相负荷下限液相负荷上限液泛线1060kg/h30%泡点进料q=1（绝对压）常压直接蒸汽加热1480kg/h0.1434983530.859639680.00196060522.0365637942.1314894218.0650145867.16110614kmol/h10.95988437kmol/h110.1479646kmol/h53.94674283kmol/h461.7562522kg/h1989.824586kg/h971.5808383kg/h2.1791.83.92220.7968388120.17464541942.98685846110.147964653.946742832.0417908260.004003145203837.0332.081.287kg/m3815.6kg/m30.431159433m3/s0.000469667m3/s0.3m0.05m0.25m0.0274221680.05229.32dym/cm0.056134536m/s1.41200602m/s0.81.129604816m/s0.697301903m0.7m0.38465m21.12m/s26.1m3.75个4个2.5m0.366307548m0.5m0.6m1.5m0.60.42m0.007186996m0.042813004m0.6倍0.10.050.07m0.0192325m212.284759165s符合0.036813004m0.055m0.07m0.295m0.21m0.7118644070.7921493020.224890653m20.039m9.696241231m/s37.24222418个38个0.04537143m20.082691852m75mm46.2477.6831827598.71626523414.6%9.140201879m/su00.025352799m取板上充气程度因素ε=0.50.025m0.050352799m402.8745566Pa54.407382378m/s1.7432530471.5~2.00.000141179m0.100493978m0.171406502小于，符合要求10.0840.56m0.346185m20.01714081660.1746595868.01298822符合要求0.247330377m3/s按泛点率80%来算0.0397551683.97551676676.162.32636320.0003582580.00115395m3/s0.2087216520.107186996640.01525381.783956387LV000.0004696670.4311594330.0007625190.7LV00.2473303770.00120.247330377LV00.5851725290.00030.5794253520.00050.57559390.00070.5717624480.00090.5679309970.0010.5660152710.00120.5621838190.50.60.70.8漏液线液沫夹带LV0.00035825800.0003582580.7LV0.0011539500.001153950.7LV00.7166173150.00030.6891745570.00050.677444230.00070.6668246440.00080.6617564360.00090.6567979310.0010.6519228650.00120.64234549000.10.20.30.400.00010.00020.00030.0004气速V0.4311594330.7性能负荷图液沫夹带液负荷下限液负荷上限液泛工作线0.4311594330.00040.00050.00060.00070.00080.00090.0010.00110.00120.0013液速L