换热器计算excel表

,盐度,进口温度(℃),出口温度(℃),处理量（Kg/s）,定性温度(℃),定压比热(J/Kg/K),定压比热(J/Kmol/K),热传导系数（W/m/K）,粘度（Pa*s）,密度（Kg/m3）,饱和蒸气压（Pa）,分子量,操作压强pa,流量m3/h

CaCl2,,-11,-4,,-7.5,2771,,0.465,0.006391,1228,1927.2,,,

乙炔,气相,32,11,24.66720864,21.5,1676.316062,43647.75,0.020916745,0.00000969,1.889403215,,26.0379,176470,47000

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π,3.1415926,换热器效率,0.98,,,,,,,,,,,

P,0.162790698,,,初选传热系数K'(W/m2/K),580,,管,,,,初选结构,换热器原理的计算,,计算公式来自续表5-19《换热器原理及计算》

R,3,Φ,,初选管程流速（m/s）,1.6,,管径d（m）,0.025,,,管间距s（m）,0.03125,,

总换热量Q(J/s),850983.7832,0.938,,初选壳程流速（m/s）,-,,内径di（m）,0.02,,,管束中心处一排数管ne,13.56171081,14,三角形排列

海水流量qsw(Kg/s),43.87192778,,,初估传热面积A'（m2）,55.02346235,,单程管数Ns,71.07526759,72,,管束外沿与壳体间距,0.05,,

热端温差deltaT1,36,,,,,,管长l(m),6,,,壳体内径Ds（m）,0.50625,0.5,

冷端温差deltaT2,22,,,取壳程流速m/s,15,,单程管长L（m）,9.730284632,,,长径比l/Ds,12,4~25横放,

对数平均温差deltaTm(℃）,28.42775325,,,,,,管程,1.621714105,2,,弓形折流板弓高h（m）,0.1,,

平均传热温度差(℃）,26.66523255,,,,,,总管数N,144,152,,折流板间距B(m),0.166666667,0.45,

,,,,,,,,,,,折流板数nB,12.33333333,13,

管程对流传热系数hi,,,,壳程传热系数ho,,,总传热系数K,,,,,,,

管程流通截面积(m2),0.022619467,,,壳程流通面积ao（m2）,0.045,,Rsi,0.000086,《换热器原理及计算》附录13-2,,,,,

海水流速ui(m/s),1.579450391,1.6,,壳程流速uo（m/s),290.1234568,,Rso,0.00017197,,,,,,

Rei,6069.676358,2100<Re<6000不用校正,,当量直径de（m）,0.040789474,,K,673.5481592,,,,,,

Pri,38.08486237,,,reo,2307447.443,,K/K',1.16128993,1.1~1.25,,,,,

（μ/μw)^(-0.14),1,μw按照-7.5℃取,,pro,0.776578895,,换热器的实际传热面积,71.62831128,,,,,,

校正系数Φ,0.907006351,2300<Re<10000,,ho,61053.69075,,依Qi＝Si△tm,47.38133084,Φ,0.338511128,足够大,,,

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hi,1051.45766,,,壳程压降,计算公式来自P205《化工原理》,,压强校核,计算公式来自续表5-19《换热器原理及计算》,,,,,,

管壁温度,计算公式来自续表5-19《换热器原理及计算》,,,F,0.5,,管程允许压降（pa）,35000,表5-2,均满足,,,,

管外壁热流密度q1（W/m/℃）,267.3123906,,,fo,0.177082624,,壳程允许压降（pa）,35000,表5-2,,,,,

管外壁温度tw1（℃）,-7.527367182,,,Ao,0.0675,,,,,,,,,

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误差校核△tw（℃）,-0.027367182,误差很小不再重算,,uo(m/s),193.4156379,,,,,,,,,

管程压降,计算公式来自续表5-19《换热器原理及计算》,,,△P1’,3170.941751,,,,,,,,,

壁温下水的粘度μwpas,0.006391,,,△P2',4038.113414,,,,,,,,,

管程黏度修正系数Φ,1,,,△Po,14418.11033,,,,,,,,,

管程摩擦系数ξi,0.045,《换热器原理及计算》图1-19,,,,,,,,,,,,

管子沿程压降△Pi（pa）,8563.926808,,,,,,,,,,,,,

回弯压降△Pr（pa）,12253.7873,,,,,,,,,,,,,

进出口管处质量流量Wn2（kg/m2s),1500,ρw2<3300,,,,,,,,,,,,

进出口管处压降△Pn2（pa）,1374.185668,,,,,,,,,,,,,

管程结垢校正系数Φd2,1.2,<1.4,,,,,,,,,,,,

管程压降△p2,26355.44259,,,,,,,,,,,,,

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尺寸计算,,