化工原理课程设计 列管式换热器的工艺设计

1、成绩华吐科技学浣课程设计报告题 目列管式换热器的工艺设计课 程名称化工原理课程设计专业化学工程与工艺班级学生姓名学号设计地点指导教师设计起止时间：2011年5月2日至2011年5月13日4化工设备机械基础董大勤主编化学工艺出版社（八）附录ChemCAD运行结果TABULATED ANALYSISOverall Data:Area Totalm210.05% ExcessArea Requiredm25.16U Calc.W/m2-KArea Effectivem29.48U Service W/m2-KArea Per Shellm29.48Heat Duty MJ/h1Weight LMTD

2、 C94.91LMTD CORRFactor 0.9888 CORR LMTD C83.74590.49321.37.03E+00393.85Shellside Data:Crossflow Vel. m/sec9.2E-002 EndZone Vel. 8.0E-002Window1.6E-001Film Coef. W/m2-K Allow Press . Drop MPa Inlet Nozzle Size m Outlet Nozzle Size mRho V2 IN kg/m-sec22158.05 Reynold* s No.0.03 Calc. Press . Drop MPa0

3、.15 Press . Drop/In Nozzle MPa0.15 Press . Drop/Out Nozzle MPaMean Temperature C35.16 Press . Drop (Dirty) MPaVel.2669-0.010.000.000.00-0.01Stream Analysis: SA Factors: A 7.74B 70.23 C 16.27 E 5.76Ideal Cross Vel. m/sec0.13 Ideal Window Vel. m/sec.000.19Tubeside Data:Film Coef. W/m2-K Allow Press. D

4、rop MPa Inlet Nozzle Size m Outlet Nozzle Size m Interm. Nozzle Size m Velocitym/secClearance Data:BafflemTube HolemBundle Top Space m Bundle Btm Space m1603.99 Reynold1s No.0.03 Calc. Press . Drop MPa0.15 Press . Drop/In Nozzle MPa0.15 Press . Drop/Out Nozzle MPa0.00 Mean Temperature C1.01 Mean Met

5、al Temperature C0.0032 Outer Tube Limit m0.0008 Outer Tube Clear. m0.0000 Pass Part Clear. m0.0000386860.010.000.00125.0067.470.29000.03500.0000Baffle Parameters:Number of BafflesBaffle TypeSingle Segmental0.3420.3000.34225.0000.050HorizontalDiameter00.003Tubes:NumberLengthmTube O.D.mTube I.D.mTube

6、Wall Thk. m64Tube TypeBare2.00Free Int. Fl Aream20.000.025Fin Efficiency0.0000.020Tube PatternSQUAR0.003Tube Pitchm0.032No. Tube PassInner Roughness m40.0000560Resistances: Shellside Film Shellside Fouling Tube Wall Tubeside Fouling Tubeside Filmm2-K/Wm2-K/Wm2-K/Wm2-K/Wm2-K/W0.000460.000180.000050.0

7、00180.00062 TOC o 1-5 h z Inlet SpacemCenter SpacemOutlet SpacemBaffle CutpercentBaffle OverlapmBaffle Cut DirectionBaffle Cut BasisNumber of Int. BafflesBaffle ThicknessmShell:Shell O.D.m0.35OrientationHShell I.D.m0.33Shell in Series1Bonnet I.D.m0.33Shell in Parallel1TypeAEWMax. Heat Flux Btu/ft2-h

8、r0.00Imping. PlateImpingement Plate Sealing StripReference Factor (Total outside area/inside area based on tube ID) 1.250Pressure Drop Distribution:Tube SideShell SideInlet NozzleMPa0.0000Inlet NozzleMPa0.0000Tube EntranceMPa0.0008ImpingementMPa0.0000TubeMPa0.0065BundleMPa0.0002Tube ExitMPa0.0022Out

9、let Nozzle MPa0.0000EndMPa0.0020Total Fric.MPa0.0003Outlet NozzleMPa0.0000Total Grav.MPa-0.0061Total Fric.MPa0.0115Total Mome.MPa0.0000Total Grav.MPa0.0000TotalMPa-0.0059Total Mome.MPa-0.0000TotalMPa0.0115课程设计任务书设计题目：列管式换热器的工艺设计和选用物料密度Kg/m3粘度Pas比热容 kJ/(kg. )入导热系数W/(m. )原油8153 X IO32.20.128柴油7150.64X

10、10 32.480.133设计题目4、炼油厂用原油将柴油从1750c冷却至130。，柴油流量为12500 kg/h；原油初温为70,经换热后升温到HOC。换热器的热损失可忽略。60kPao管、壳程阻力压降均不大于30kPao污垢热阻均取0. 0003 m2./W一、确定设计方案1、选择换热器类型俩流体温度变化情况：柴油进口温度175C,出口温度110。原油进口温度70,出口温度110从两流体的温度来看，估计换热器的管壁温度和壳体壁温之差不会很大，因此初步确定选用 固定管板式换热器。2、流程安排该任务的热流体为柴油，冷流体为原油，由于原油的黏度大，因此使原油走壳程，柴油走管程。二、工艺结构设计(

11、-)估算传热面积1 .换热器的热流量(忽略热损失)Q =兀）=x 2.48 x103x（175-30） = 3875000W2.冷却剂原油用量（忽略热损失）387500qi2 G2l 力)2200 x(110-70)=4.40 依 / s2 .平均传热温差、_ Ktx -At2 _ (175-110)-(130-70) 八。 一= 62.5。加23.估K值130-70K估=220W/G/。4,由K值估算传热面积4 _ Q387500 re。 ,Av.= 28.2m“K估屋 220 x62.5（二）工艺结构尺寸.管径、管长、管数。管径选择 选用例9义2加传热管（碳钢）估算管内流速 取管内流速估=

12、0.6根/s12500计算管数= 3x715 =45.446（根）-x0.0152x0.6计算管长 L = =10.28m 7idn x0.019x46Cz 3而确定管程 按单管程设计，传热管稍长，宜采用多管程结构。现取传热管长/=2.5m,那么该传唤器管程数为：N = = U4（管程），那么传热管总根数N=46 p I 2.5X4=184 （根）.管子的排列方法采用组合排列法，即每程内按正三角形排列，隔板两侧采用矩形排列，管子和管板采用焊接结构计算管心距 t = l.25d。= 1.25 x 19 = 23.75 x 24mm隔板中心到离其最近一排管中心距离S=t/2+6=24/2+6=l

13、8mm各程相邻管心距为36mm各程各有传热管46根.壳体内径的计算采用多管程结构，取管板利用率n=0.7计算 D = 1 .05“N/ = L05 x 24x 7184/0.7 = 408(mm)圆整 D=450mm.折流板 圆缺高度的计算 H = 25%，= 0.25x325 = 81.25/加折流板间距 h 3OO/W7?/9折流板数量Nh = 1 =1 = 6 nh0.3.计算壳程流通面积及流速计算流通面积n =1.19777 = 1.19a/64 =9.5210A = h(D - nd) = 0.3(0.325-10 x 0.025) = 0.0225(m2)V 1/计算壳程流体流速U

14、o2xl040.0225 x 3600 x 1.09547 x：=0.225 m/s6 .计算实际传热面积= N/cdJ = 10.05m2.传热温差报正系数确实定TX。r_TT2 A 40 20r_TT2 A 40 20= 1.5查表：cp - 0.92.管程与壳程传热系数确实定壳程外表传热系数 a。=0.363Re：Pr%(风)4当量直径，由正方形排列得：24(a2-do) 4(0.031252-x 0.0252)de =一 = 0.0247md。万 x 0.025壳程流通截面积：A = /zD(l-) = 0.3 x 0.325(1 -= o.0195nra0.03125壳程流体流速:U

15、o200003600 x 1.09547 xl03x 0.0195=Q 26mls雷诺数： duop() 0.0247 x 0.26 x 1.09547 x 103 一 也)5.68981X10-4普兰特准数：Pr _CpM _ 1.77029x1()3 x5 6898 lx ICT4V 2.1.34945 xW1粘度校正先严=0.36 x1 2364.4$5 x 7.46% = 684.495W 人m1 )0.0247管程外表传热系数az. =0.023Re,0 8 PrlJ IIdi管程流体流速：一 _ 匕Ll-冗,2 a. n4 ；3.54509 x 10-3 2 =4V _4x3.54

16、509x1()-3mi? V 7rxi .8=0.05m12、换热器流体流动阻力管程流体阻力=(M + M)CMNpN$=l,Np=4,Ft=1.4由Re=17609.615 ,传热管对粗糙度 =更=0.005,查莫狄图得= 0.0314 20而1 1口 吉 Asv pr 枕ac 勺 I u：p20.7052 x995.78/.母程直官压降 AP = A x- = 0.031x X= 76714Rz420.022每程回弯压降 AQ. = 3空=3x 0.705- x 995.78 = 742.39&总压降 Pt = (767.14 + 742.39)x1x4x1.4 = 8453.368P。x

17、 SA5kPa 500, = 5.0 Re/0228 =5xl2364.4-0-228 =0.583Ntc=1A 9(%) 5 =1.19x 64 5 =9.52=10n xi 09547xin3AP = 0.3 x 0.583 xl0 x(6 + l)x = 453.62Pa折流板缺口压降2 u 2 p Mp = N3.5-7)告 h 0.3m, D - 0.325mAg=6x(3.5 Ag=6x(3.5 =367.4242x0.3、0.262x 1.09547 xlO3)x 0.325总压降= (453.62 + 367.42)x1.15 = 944.196P。工 0.94kPa 35kP

18、a(五)结果概要换热器主要结构尺寸和计算结果见下表:参数管程壳程流率(kg/h)12708.46820000进口温度/20140出口温度/40110压力/Mpa0.40.3物性参数定性温度/30125密度/ (kg/m3)995. 781. 09547 X103定压比热容/kj/(kg)4. 17901. 77029粘度/ (mPa*s)0. 797325. 68981 X 10-1热导率(W/m)0. 615641. 34945 X10-1普朗特数5.417. 46设备结构参数形式浮头式壳程数1壳体内径/mm325台数1管径/mm。25 x 2.5管心距mm31.25管长/mm2000管子排列正方形管数/根64折流板数/个6传热面积/ni?10. 05折