323028262422201614121086420.0000.005液泛线液相负荷下限线Vs(m3/s)18漏液线雾沫夹带线0.0100.0150.0200.025Ls(m3/s)液相负荷上限线
8.2提馏段：
8.2.1漏液线
由
?0,min?V0,min/A0?4.4C0(0.0056?0.13(hw?how)?hc)?L/?V ，
hOW?LA?2.84/1000*E??l?WVs,min?4.4C0A0??? ?2?2/3???lh??2.84??E???0.0056?0.13?hw??l????hl?l/?V1000??w???????4.4?0.772?0.101?0.377??2.84?Ls?3600??0.0056?0.13?0.031??????1000?1.92??????4.690.8971.31?13.28Ls2/32/3???790?0.002??3.34????
表9漏液线
Ls /(m3/s) Vs /(m3/s)
0.00164 4.88
0.0235 6.61
0.0485 7.56
0.0656 8.12
8.2.2雾沫夹带线
3.25.7?10??uaev??H?h?Lf?T?6????3.2?????6Vs5.7?10???
19.19?10?3?4.52?0.656????H?H?Tf???a?VsVs??0.259Vs
AT?Af4.52?0.6562/3?2.84?3600Ls??HT?hf?0.4?2.5?hw?how??0.4?2.5?0.031??1?????1000?1.92?????
0.3225?1.08Ls2/33.2?0.259Vs5.7?10?6???ev??3?2/3?19.19?10?0.3225?1.08Ls??0.1
Vs?7.67?25.68Ls2/3
表10雾沫夹带线
Ls /(m3/s) Vs /(m3/s)
0.00164 0.0235 0.0485 0.0656
7.31 5.56 4.25 3.49
8.2.3液相负荷下限线
对于平直堰，取堰上液层高度how?0.006mm作为最小液体负荷标准
how2.84?3600Ls?E?1000??Lw????2/3取 E=1
Lsmin?0.006?1000????2.84??3/2?1.92?0.00164 36008.2.4液相负荷上限线
以??4s作为液体在降液管中停留时间的下限
??AfHT LsLs?max0.656?0.4?0.0656
48.2.5液泛线
令HD?由Hd?K?HT?hw?
hp?hl?hd hp?hc?hl?h?
hl??hL
hL?hw?how
联立得KHT??K???1?hw????1?how?hc?hd?h?
忽略ho，将how与Ls，LC与Vs的关系代入上式
a?Vs?b??c?Ls2?d?Ls2/3
a??0.051??V?2??Aolo???L?0.051?3.34?? ???0.101?3.77?1.92?2?790??0.000403???2b??KHT??K???1?hw?0.23?0.4??0.23?0.702?1?0.038?0.04922
22c??0.153/?loho??0.153/?1.92?0.023??78.46
?3600?d??2.84?10?3E?1?????L???w?22/3?3600??2.83?10?1??1?0.702???1.92???32/3?0.73
代数得0.000403Vs?0.04922?78.46Ls2?0.73Ls2/3
Vs?122.13?195000Ls2?1811.4Ls2/3
表11 液泛线
Ls /(m3/s)
0.00164
0.0235
0.0485
0.0656
2Vs /(m3/s)
19.56 18.47 16.13 14.11
做出筛板负荷性能图
图2筛板负荷性能图
20液泛线1816141210液相负荷下限线Vs(m3/s)8642漏液线雾沫夹带线0.000.010.020.030.040.050.060.07Ls(m3/s)
9 设备设计
9.1塔顶全凝器的计算与选型
9.1.1全凝器的传热面积和冷却水的消耗量
tD?80.92℃
冷凝蒸汽用量：G1?Mv?V80.64?425.86??9.54kg/s 36003600查得苯的潜热r?394kj/kg 甲苯的潜热r?362kj/kg
r?0.983?394?0.017?362?393.5kj/kg
液相负荷上限线