3.5=459mm 取折流板的间距为：h=300mm,最小厚度6 mm 折流板的档板数
NB? =
28 1
传热管长折流板间隙?1 (2-12)
6000300?1
=19 所以 折流板的实际间隙为：
h?5900/?NB?1? =197mm
折流板和支持板管孔直径为?25.8?0.40mm
换热器支持板名义直径为Dy?6?500?6?494mm
2.4.3 接管规格
A 管程 d?4Vs4?12615/?3600?994?u????1.5?54.7mmmm (2-13)
B 壳程 di?4V4?30500/?3600?32.63??u??1?57.5mm (2-14)
C 接管规格
（1）管程：?50?4： （2）壳程：?50?4
2.5 换热器核算
核算总传热系数[6]
2.5.1 管程对流传热系数?i：
Rui?ie?di??0.02?0.5?994i0.000626?15879?104 (2-15)
为湍流
29
1
Pri?Cp? (2-16)
?4.174?103?0.626?10?3 =
0.6338
=4.32J/kg?K 因为 ??0.626mpa.s?2mpa.s
ld?600025?240?60
所以 ???du??0.8ii?0.023?d????P0.4r (2-17)
i??? =0.023?0.6338.80.40.02?15879?0??4.32? =3002.6w/?m2?0C?
2.5.2 壳程对流传热系数?0：
?0.140?0.036?(deu0?)0.5(cpu/3
??)1(??)w (2-18)
取换热器列管的中心距t=32mm 流体通过管间最大截面积为：
A?hD??1?d0??t?? (2-19) =0.3?0.5???1?0.025??0.032?? 30 1
=0.033m2 u0?? (2-20)
A =
305000.033?3600?32.63
=7.87m/s
4(t2??20)de?4d?d04?(0.0322??40.0252)?3.14?0.025
?0.027m Rdeu0?丙烷e0?? (2-21)
丙烷 =
0.027?7.87?32.630.0118?10?3
=5.9?105
Pr0?Cp??
?1.125 ?103?0.0118?10?30.025
=0.531
0.14壳程中丙烷被冷却，取?????1
???w??0.551/30.14 ??0.36??0?d?eu0????Cpu????????????????????w?31
1
(2-22)
=0.36??5.9?105?0.55??0.531?1/3?1
=435w/?m2?0C?
2.5.3 总传热系数k0
管壁热阻可忽略管内，外侧污垢热阻分别为：
?4
Rsi?0.86?10k/w
Rso?0.86?10?4k/w总传热系数k0为：
K0?11?Rd0d0bd0?so?Rsid?0i??idi?di?11435?0.86?10?4?0.86?10?4?0.025.025.0025?0.0250.02?03002.6?0.02?045?0.02=336ω/m2 k
计算传热面积
3
S1?Q?285.9?10 =267.4 Kt?39.6m2 (2-23)0?m336?21.5实际传热面积
S?Nt?d0L?132???0.025?5.99?62m2 (2-24)
2.5.4 计算流体阻力
核算管程和壳程的压强降
32 1
A 管程压力降公式： ????水ul????3F0Np (2-25) ?pi=??d?2i??2 式中 ： F0=1.4 ， Np = 6, di(内径)=20mm 管程流通面积： A?2ni?4diN (2-26)
p =
??0.022?2246
=0.0014m2 水的流速： uVi?A (2-27)
i =
3.5994?0.0014
=2.4m/s
Rdiui?水e?? (2-28)
=
0.02?2.4?9940.626?10?3 =76217?104
所以为湍流。
管壁的粗糙度：?= 0.1
?d?0.105mm (2-29)