化工原理課程設(shè)計(jì) 列管式換熱器的工藝設(shè)計(jì)

1、成績(jī)?nèi)A吐科技學(xué)浣課程設(shè)計(jì)報(bào)告題 目列管式換熱器的工藝設(shè)計(jì)課 程名稱化工原理課程設(shè)計(jì)專業(yè)化學(xué)工程與工藝班級(jí)學(xué)生姓名學(xué)號(hào)設(shè)計(jì)地點(diǎn)指導(dǎo)教師設(shè)計(jì)起止時(shí)間：2011年5月2日至2011年5月13日4化工設(shè)備機(jī)械基礎(chǔ)董大勤主編化學(xué)工藝出版社（八）附錄ChemCAD運(yùn)行結(jié)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課程設(shè)計(jì)任務(wù)書(shū)設(shè)計(jì)題目：列管式換熱器的工藝設(shè)計(jì)和選用物料密度Kg/m3粘度Pas比熱容 kJ/(kg. )入導(dǎo)熱系數(shù)W/(m. )原油8153 X IO32.20.128柴油7150.64X

10、10 32.480.133設(shè)計(jì)題目4、煉油廠用原油將柴油從1750c冷卻至130。，柴油流量為12500 kg/h；原油初溫為70,經(jīng)換熱后升溫到HOC。換熱器的熱損失可忽略。60kPao管、殼程阻力壓降均不大于30kPao污垢熱阻均取0. 0003 m2./W一、確定設(shè)計(jì)方案1、選擇換熱器類型倆流體溫度變化情況：柴油進(jìn)口溫度175C,出口溫度110。原油進(jìn)口溫度70,出口溫度110從兩流體的溫度來(lái)看，估計(jì)換熱器的管壁溫度和殼體壁溫之差不會(huì)很大，因此初步確定選用 固定管板式換熱器。2、流程安排該任務(wù)的熱流體為柴油，冷流體為原油，由于原油的黏度大，因此使原油走殼程，柴油走管程。二、工藝結(jié)構(gòu)設(shè)計(jì)(

11、-)估算傳熱面積1 .換熱器的熱流量(忽略熱損失)Q =兀）=x 2.48 x103x（175-30） = 3875000W2.冷卻劑原油用量（忽略熱損失）387500qi2 G2l 力)2200 x(110-70)=4.40 依 / s2 .平均傳熱溫差、_ Ktx -At2 _ (175-110)-(130-70) 八。 一= 62.5。加23.估K值130-70K估=220W/G/。4,由K值估算傳熱面積4 _ Q387500 re。 ,Av.= 28.2m“K估屋 220 x62.5（二）工藝結(jié)構(gòu)尺寸.管徑、管長(zhǎng)、管數(shù)。管徑選擇 選用例9義2加傳熱管（碳鋼）估算管內(nèi)流速 取管內(nèi)流速估=

12、0.6根/s12500計(jì)算管數(shù)= 3x715 =45.446（根）-x0.0152x0.6計(jì)算管長(zhǎng) L = =10.28m 7idn x0.019x46Cz 3而確定管程 按單管程設(shè)計(jì)，傳熱管稍長(zhǎng)，宜采用多管程結(jié)構(gòu)?，F(xiàn)取傳熱管長(zhǎng)/=2.5m,那么該傳喚器管程數(shù)為：N = = U4（管程），那么傳熱管總根數(shù)N=46 p I 2.5X4=184 （根）.管子的排列方法采用組合排列法，即每程內(nèi)按正三角形排列，隔板兩側(cè)采用矩形排列，管子和管板采用焊接結(jié)構(gòu)計(jì)算管心距 t = l.25d。= 1.25 x 19 = 23.75 x 24mm隔板中心到離其最近一排管中心距離S=t/2+6=24/2+6=l

13、8mm各程相鄰管心距為36mm各程各有傳熱管46根.殼體內(nèi)徑的計(jì)算采用多管程結(jié)構(gòu)，取管板利用率n=0.7計(jì)算 D = 1 .05“N/ = L05 x 24x 7184/0.7 = 408(mm)圓整 D=450mm.折流板 圓缺高度的計(jì)算 H = 25%，= 0.25x325 = 81.25/加折流板間距 h 3OO/W7?/9折流板數(shù)量Nh = 1 =1 = 6 nh0.3.計(jì)算殼程流通面積及流速計(jì)算流通面積n =1.19777 = 1.19a/64 =9.5210A = h(D - nd) = 0.3(0.325-10 x 0.025) = 0.0225(m2)V 1/計(jì)算殼程流體流速U

14、o2xl040.0225 x 3600 x 1.09547 x：=0.225 m/s6 .計(jì)算實(shí)際傳熱面積= N/cdJ = 10.05m2.傳熱溫差報(bào)正系數(shù)確實(shí)定TX。r_TT2 A 40 20r_TT2 A 40 20= 1.5查表：cp - 0.92.管程與殼程傳熱系數(shù)確實(shí)定殼程外表傳熱系數(shù) a。=0.363Re：Pr%(風(fēng))4當(dāng)量直徑，由正方形排列得：24(a2-do) 4(0.031252-x 0.0252)de =一 = 0.0247md。萬(wàn) x 0.025殼程流通截面積：A = /zD(l-) = 0.3 x 0.325(1 -= o.0195nra0.03125殼程流體流速:U

15、o200003600 x 1.09547 xl03x 0.0195=Q 26mls雷諾數(shù)： duop() 0.0247 x 0.26 x 1.09547 x 103 一 也)5.68981X10-4普蘭特準(zhǔn)數(shù)：Pr _CpM _ 1.77029x1()3 x5 6898 lx ICT4V 2.1.34945 xW1粘度校正先嚴(yán)=0.36 x1 2364.4$5 x 7.46% = 684.495W 人m1 )0.0247管程外表傳熱系數(shù)az. =0.023Re,0 8 PrlJ IIdi管程流體流速：一 _ 匕Ll-冗,2 a. n4 ；3.54509 x 10-3 2 =4V _4x3.54

16、509x1()-3mi? V 7rxi .8=0.05m12、換熱器流體流動(dòng)阻力管程流體阻力=(M + M)CMNpN$=l,Np=4,Ft=1.4由Re=17609.615 ,傳熱管對(duì)粗糙度 =更=0.005,查莫狄圖得= 0.0314 20而1 1口 吉 Asv pr 枕ac 勺 I u：p20.7052 x995.78/.母程直官壓降 AP = A x- = 0.031x X= 76714Rz420.022每程回彎壓降 AQ. = 3空=3x 0.705- x 995.78 = 742.39&總壓降 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折流板缺口壓降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總壓降= (453.62 + 367.42)x1.15 = 944.196P。工 0.94kPa 35kP

18、a(五)結(jié)果概要換熱器主要結(jié)構(gòu)尺寸和計(jì)算結(jié)果見(jiàn)下表:參數(shù)管程殼程流率(kg/h)12708.46820000進(jìn)口溫度/20140出口溫度/40110壓力/Mpa0.40.3物性參數(shù)定性溫度/30125密度/ (kg/m3)995. 781. 09547 X103定壓比熱容/kj/(kg)4. 17901. 77029粘度/ (mPa*s)0. 797325. 68981 X 10-1熱導(dǎo)率(W/m)0. 615641. 34945 X10-1普朗特?cái)?shù)5.417. 46設(shè)備結(jié)構(gòu)參數(shù)形式浮頭式殼程數(shù)1殼體內(nèi)徑/mm325臺(tái)數(shù)1管徑/mm。25 x 2.5管心距mm31.25管長(zhǎng)/mm2000管子排列正方形管數(shù)/根64折流板數(shù)/個(gè)6傳熱面積/ni?10. 05折