燃料油換熱器計算

1、燃料油換熱器計算燃料油換熱器計算一、物性參數(shù)M100燃料油物性參數(shù)根據(jù)油品儲運設(shè)計手冊油品容重修正系數(shù) 油品密度油品導(dǎo)熱系數(shù)：油品粘度 油品的質(zhì)量熱容：T-55導(dǎo)熱油性質(zhì)：140下密度為845kg/m3140下比熱為2.05kJ/kgK149下粘度為1.311mPas149下導(dǎo)熱系數(shù)：= 0.1134 W/mK二、計算天津大學(xué)版化工原理（一）1500m3/h1、試算和初選冷卻器的規(guī)格（1）計算熱負荷燃料油入口溫度50，經(jīng)換熱器加熱至70裝船。裝船泵額定流量：1500m3/h熱負荷 Q = =15009801.8920/3600 = 15435 kW（2）導(dǎo)熱油的量 導(dǎo)熱油入口160，出口：14

2、0，則需要導(dǎo)熱油的量 m= = =376.46kg/s需要的導(dǎo)熱油量：376.463600/845 = 1603.85m3/h（2）平均溫度差燃料油： 50 70 導(dǎo)熱油： 160 140 110 70 tm = 88.50R = = = 1P = = = 0.3333由R和P值，查圖 6-15a，t=0.96tm = ttm = 0.9688.50 =84.96 （3）初選換熱器規(guī)格根據(jù)兩流體情況，取K選 = 400 W/ m故 =454m2選擇浮頭式換熱器（JB/T4717-92）：DN1200 2管程，計算傳熱面積 504.3m2管長L = 6 m管徑 192換熱管數(shù)：1452折流擋板間

3、距 B = 300 mm若采用這臺換熱器，要求過程的總傳系數(shù)為： = 360W/ m2、 核算壓降（1） 管程壓強降管程平均通道面積 Ai = 0.1290 m2ui = = = 3.23m/sRei = = = 573857.87以管壁粗糙度為0.25mm，則 /d = = 0.0167 = 0.046 所以 P1 = = =94063PaP2 = = = 13928PaFt = 1.5 Ns = 1 Np =2所以 Pi = (94063+13928)1.512 = 326973 Pa（2） 殼程阻力降P1= 管子為正三角排列，取F=0.5 nc = 1.1 (n) 1/2 = 1.1 (

4、1452) 1/2 =41.92取折流擋板間距 h=0.3 mNB = = =19=0.3(1.2-41.920.019)=0.1210 m2 = 3.68 m/sReo = = = 45067 500fo = 5Reo-0.228 = 0.43所以 P1= 0.50.4341.9219 = 979796 Pa P2 = = = 326135 Pa = (979796+326135)1.151 =1501820.65Pa3、 核算總傳熱系數(shù)（1） 管程對流傳熱系數(shù) iRei = 573857.87故 i = = = 68598.59（2） 殼程對流傳熱系數(shù)oAo= = 0.0864m2uo =

5、 = 5.16 m/sReo = =63191.30故 o = 0.36 *(/do)*Re0.55 * Pr(1/3) *0.95 = =2561.24（3） 確定污垢熱阻Rso = 0.00018Rsi =0.0009（4）計算總傳熱系數(shù)經(jīng)計算 = = Ko= 576.84K計/K選 = 576.84/360= 1.60滿足要求，但導(dǎo)熱油殼程壓降太大。（二）800m3/h1、試算和初選冷卻器的規(guī)格（1）計算熱負荷燃料油入口溫度50，經(jīng)換熱器加熱至70裝船。裝船泵額定流量：800m3/h熱負荷 Q = =8009801.8920/3600 = 8232 kW（2）導(dǎo)熱油的量 導(dǎo)熱油入口160

6、，出口：140，則需要導(dǎo)熱油的量 m= = =200.78kg/s需要的導(dǎo)熱油量：200.783600/845 = 855m3/h（2）平均溫度差燃料油： 50 70 導(dǎo)熱油： 160 140 110 70 tm = 88.50R = = = 1P = = = 0.3333由R和P值，查圖 6-15a，t=0.96tm = ttm = 0.9688.50 =84.96 （3）初選換熱器規(guī)格根據(jù)兩流體情況，取K選 = 400 W/ m故 =242m2選擇浮頭式換熱器（JB/T4717-92）：DN900 2管程，計算傳熱面積 279.2m2管長L = 6 m管徑 192換熱管數(shù)：800折流擋板間

7、距 B = 300 mm若采用這臺換熱器，要求過程的總傳系數(shù)為： = 385.57W/ m4、 核算壓降（3） 管程壓強降管程平均通道面積 Ai = 0.0707 m2ui = = = 3.14m/sRei = = = 557868以管壁粗糙度為0.25mm，則 /d = = 0.0167 = 0.046 所以 P1 = = =88894PaP2 = = = 14494PaFt = 1.5 Ns = 1 Np =2所以 Pi = (88894+14494)1.512 = 310164 Pa（4） 殼程阻力降P1= 管子為正三角排列，取F=0.5 nc = 1.1 (n) 1/2 = 1.1 (

8、800) 1/2 =31.11取折流擋板間距 h=0.3 mNB = = =19=0.3(0.9-31.110.019)=0.0927 m2 = 2.56 m/sReo = = = 31351 500fo = 5Reo-0.228 = 0.47所以 P1= 0.50.4731.1119 = 384617 Pa P2 = = = 157827 Pa = (384617+157827)1.151 =623810.6Pa5、 核算總傳熱系數(shù)（4） 管程對流傳熱系數(shù) iRei = 557868故 i = = = 67065.15（5） 殼程對流傳熱系數(shù)oAo= = 0.0648m2uo = = 3.6

9、65 m/sReo = =44882.97故 o = 0.36 *(/do)*Re0.55 * Pr(1/3) *0.95 = =2122（6） 確定污垢熱阻Rso = 0.00018Rsi =0.0009（4）計算總傳熱系數(shù)經(jīng)計算 = = Ko= 551K計/K選 = 551/385.57= 1.43滿足要求。（三）800m3/h，因殼程導(dǎo)熱油壓降大，放大一級1、試算和初選冷卻器的規(guī)格（1）計算熱負荷燃料油入口溫度50，經(jīng)換熱器加熱至70裝船。裝船泵額定流量：800m3/h熱負荷 Q = =8009801.8920/3600 = 8232 kW（2）導(dǎo)熱油的量 導(dǎo)熱油入口160，出口：140

10、，則需要導(dǎo)熱油的量 m= = =200.78kg/s需要的導(dǎo)熱油量：200.783600/845 = 855m3/h（2）平均溫度差燃料油： 50 70 導(dǎo)熱油： 160 140 110 70 tm = 88.50R = = = 1P = = = 0.3333由R和P值，查圖 6-15a，t=0.96tm = ttm = 0.9688.50 =84.96 （3）初選換熱器規(guī)格根據(jù)兩流體情況，取K選 = 400 W/ m故 =242m2選擇浮頭式換熱器（JB/T4717-92）：DN900 2管程，計算傳熱面積 260.6m2管長L = 4.5 m管徑 192換熱管數(shù)：1006折流擋板間距 B

11、= 300 mm若采用這臺換熱器，要求過程的總傳系數(shù)為： = 371.81W/ m6、 核算壓降（5） 管程壓強降管程平均通道面積 Ai = 0.089m2ui = = = 2.50m/sRei = = = 444162以管壁粗糙度為0.25mm，則 /d = = 0.0167 = 0.046 所以 P1 = = =56350PaP2 = = = 9187.5PaFt = 1.5 Ns = 1 Np =2所以 Pi = (56350+9187.5)1.512 = 196612.5Pa（6） 殼程阻力降P1= 管子為正三角排列，取F=0.5 nc = 1.1 (n) 1/2 = 1.1 (1006) 1/2 =34.89取折流擋板間距 h=0.3 mNB = = =14=0.3(1.0-34.890.019)=0.1011 m2 = 2.35 m/sReo = = = 28779 500fo = 5Reo-0.228 = 0.48所以 P1= 0.50.4834.8919 = 37122Pa P2 = = = 97997 Pa = (37122+97997)1.151 =155387Pa7、 核算總傳熱系數(shù)（7） 管程對流傳熱系數(shù) iRei = 444162故 i = = =55886（8） 殼程對流傳