脂肪醇聚氧乙烯醚車間工藝設(shè)計(jì)

TOC\o"1-5"\h\z\o"CurrentDocument"第1章物料及熱量衡算 1\o"CurrentDocument"L1物料衡算基準(zhǔn) 1\o"CurrentDocument"L2管道物料衡算及有關(guān)反應(yīng)時(shí)間計(jì)算 2\o"CurrentDocument"預(yù)反應(yīng)、反應(yīng)及熟化階段的物料衡算 6\o"CurrentDocument"階段數(shù)據(jù)表格 7\o"CurrentDocument"第2章設(shè)備計(jì)算 7\o"CurrentDocument"反應(yīng)回路換熱器E0101的選型計(jì)算 7\o"CurrentDocument"反應(yīng)回路換熱器E0102的選型計(jì)算 12\o"CurrentDocument"反應(yīng)回路換熱器E0104的選型計(jì)算 18\o"CurrentDocument"導(dǎo)熱油加熱器E0103的選型計(jì)算 23\o"CurrentDocument"第3章泵的選擇 27\o"CurrentDocument"PC-0101反應(yīng)回路循環(huán)泵揚(yáng)程計(jì)算 27\o"CurrentDocument"PC-0101反應(yīng)回路循環(huán)泵的選型 29\o"CurrentDocument"第4章中和釜體積及攪拌器功率計(jì)算 30\o"CurrentDocument"中和釜體積計(jì)算 30\o"CurrentDocument"攪拌器的功率計(jì)算 30附表 31第1章物料及熱量衡算物料衡算基準(zhǔn)說明：硬脂酸(C15H24O)+10EO,年產(chǎn)量60000噸,日產(chǎn)量(按300天計(jì))200噸，每批10噸=10000kg,每天20批鏈起始劑分子量Mst=284.48最終產(chǎn)品分子量Mfp=284.48+10x44.05=724.98每批起始劑的量：Wst=x\0000=28448x10000=3923.97依Mfp 724.98環(huán)氧乙烷EO的量：Wox=Wstxnx44/Mst=3923.97xl0x44/284.486076.03依故：3923.97+6076.03=10000.00kg催化劑的量：NaOH10000x0.1%/42%=23.81kg中和齊IJ：CH3COOH10000X0.1%xMHAc/(MNaOH)=10000x0.1%x60/(40x98%)=15.31kg管道物料衡算及有關(guān)反應(yīng)時(shí)間計(jì)算管線(2)111附錄已知EO液體流速GzzlOOOOkg.h-1EO最快加料時(shí)間：t=Wox/G=6076.03/10000=36.5min實(shí)際操作中管道內(nèi)流體流速不能達(dá)到最大值對(duì)加料時(shí)間進(jìn)行取整：r=40min此時(shí)管線內(nèi)質(zhì)量流速：G,=Wox/t=3923.97/30000=7.85min管線(3)已知鏈起始劑的流速G=30000kg.h-1起始劑最快加料時(shí)間：r=3923.97/30000=7.85min對(duì)加料時(shí)間取整為：r'=10min1.2.41.2.4管線(6)、(9)、(10)此時(shí)管內(nèi)實(shí)際質(zhì)量流速：G'=WstlT'=3923.977(10/60)=23543.82依//?管線(5)、(7)、(8)催化劑的質(zhì)量流速860kg.h1其中：58%水質(zhì)量流速860x58%=498.80kg.h-142%NaOH質(zhì)量流速860x42%=361.20kg.lr142%NaOH最快加料時(shí)間：t=Wnuoh/Gnuoh=23.81/361.20=0.066h=3.95min取整為x'=5min則此時(shí)42%NaOH溶液在管道中實(shí)際質(zhì)量流速：GNaOH'=23.81/(5/60)=285.72kg.h-1催化劑在管道內(nèi)實(shí)際質(zhì)量流速：GNaOH'/42%=285.72/42%=680.29kg.h"因?yàn)椋阂訮D101為衡算范圍，輸入二輸出所以：(7)、(8)號(hào)管線質(zhì)量流速相等。管線(5)中催化劑NaOH的最大質(zhì)量流速為2860kg/h則經(jīng)驗(yàn)系數(shù)：＜7=2860/860=3.33由《技術(shù)文件及裝置操作手冊(cè)》知，加料時(shí)間定為5min則(5)中流速：G=axG'NaOH=3.33x680.29=2265.37kg-h-142%的NaOH2265.37x42%=951.46kg.h"2%的H2O2265.37x58%=1313.91kg.h-,管(9)中和劑的質(zhì)量流速為600kg.h-1其中：98%CH3coOH質(zhì)量流速：98%x600=588kg.h-12%的比0的質(zhì)量流速：2%x600=12kg.h/98%CH3COOH最快加料時(shí)間：r=Wch3cooh/G=15.31/588=0.026h=1.56min取整為T'=5min則此時(shí)98%CH3COOH的實(shí)際質(zhì)量流速：Gcu3cooh,=15.31/(5/60)=183.72kg.h'1其中：98%CH3COOH183.72x98%=180.05kg.h-12%的H2O183.72x2%=3.67kg.h-1以中和計(jì)量泵為衡算范圍：輸入二輸出所以：(9)、(10)號(hào)管線質(zhì)量流速相等。管(6)中和劑最大質(zhì)量流速2000kg.h」經(jīng)驗(yàn)系數(shù)：a=2000/600=3.33由《技術(shù)文件及裝置操作手冊(cè)》知，加料時(shí)間定為5min則(6)中流速：G=axCxh3cwh,=3.33x183.72=611.79kg.h-198%CH3coOH611.79x98%=599.55kg.lr12%的H2O611.79x2%=12.24kg.h」管線(11)、(12)、(13)反應(yīng)回路小循環(huán)泵PC-103每次循環(huán)量為10000kg,每小時(shí)循環(huán)次數(shù)為6.5次，每小時(shí)質(zhì)量流速G=6,5x10000=65000kg.h/流經(jīng)管線(11)的物料通過反應(yīng)循環(huán)泵PC-103之后，流經(jīng)管線(12),最后經(jīng)反應(yīng)換熱器E-102,流經(jīng)管線(13)的連續(xù)過程中，泵和換熱器內(nèi)部都沒有積累，即對(duì)每一個(gè)設(shè)備來(lái)說，輸入二輸出，故管線(11)、(12)、(13)的質(zhì)量流速均為G=65000kg.h-1管線(17)、(18)、(19)反應(yīng)回路小循環(huán)泵PC-103每次循環(huán)量為10000kg,循環(huán)次數(shù)為36次/h,每小時(shí)質(zhì)量流速為360000kg.M,在連續(xù)操作過程中，PC-101和換熱器E-101中不可有積累。所以管線(17)、(18)、(19)中質(zhì)量流速都相等360000kg.hL管線(16)、(22)、(23)管線(16)是小循環(huán)產(chǎn)品出料管線流速已知為40000kg.hL管線(22)是大循環(huán)產(chǎn)品出料管線流速已知為150000kg.hL若卸料只靠小循環(huán)回路泵，即只從管線(16)卸料，則10噸產(chǎn)品出料時(shí)間T=10000/40000=0.25h=15min若卸料只靠大循環(huán)回路泵，即只從管線(22)出料時(shí)，則10噸產(chǎn)品出料時(shí)間t=10000/150000=0.067h=4mino而實(shí)際生產(chǎn)中卸料應(yīng)先是大小循環(huán)回路同時(shí)卸料，即(22)、(16)同時(shí)卸料，達(dá)到一定程度，液位不再滿足大循環(huán)回路時(shí)，就只能從(16)管線卸料?？紤]上述原因，每批醇酸產(chǎn)品出料時(shí)間取工=10min,則管線平均每小時(shí)卸料G=10000x60/10=60000kg.h/，卸料只靠小循環(huán)泵時(shí)，(23)的實(shí)際流速G=40000kg.h'o卸料前期管線(23)的流速G>60000kg.h-1o取:150000kg.hL中和部分管線(13)、(14)管線(13)的流速為35000kg.h1卸料1：=10000/35000=0.29h=17min,取整t=25min此時(shí),實(shí)際流速G=10000/(25/60)=24000kg.h1因?yàn)橐訮V-104A/B為衡算范圍，輸入=輸出所以管線(13)、(14)流速相等。6428.6X6428.6X95%X5% y預(yù)反應(yīng)、反應(yīng)及熟化階段的物料衡算預(yù)反應(yīng)EO總量為4050kg.lr1在預(yù)反應(yīng)階段加入5%CisHiyOH+9EO—>CisHa12cHiO\)H220 396 616x6428.6X5% yJx=220x6428.6x5%/396=178.57攵gy=616x6428.6x5%/396=500.00心所以，在預(yù)反應(yīng)階段反應(yīng)鏈起始劑用量178.57kg,得500.00kg產(chǎn)品。反應(yīng)階段加入剩余的EO,但只有95%參加反應(yīng)，故Cl3H230H+9EO-Cl3H23O(CH￡H?O)9H220 396 616x6428.6X95%X95%yx=220x6428.6x95%x95%/396=3223.23kgy=616x6428.6x95%x95%/396=9025.04Ag熟化階段Ci3H230H+9EOfCi3H"(CH2cH?O)9H220 396 616x=220x6428.6x95%x5%/396=l69.644y=616x6428.6x95%x5%/396=475.00依因?yàn)樵现杏?.1%的水，所以實(shí)際投料量：(178.57+3223.23)x(1+0.1%)=3405.20kg其中預(yù)反應(yīng)起始劑量：178.57x(l+0.1%)=l78.75kg反應(yīng)起始劑量：3223.53x(1+0.1%)=3226.45小階段數(shù)據(jù)表格反應(yīng)時(shí)間/minEO投料量/kg起始劑投量/kgCat用量/kg反應(yīng)率/%產(chǎn)品量/kg預(yù)反應(yīng)5321.43178.751.191100500.00反應(yīng)305801.83226.4522.62959025.04熟化20///5475第2章設(shè)備計(jì)算反應(yīng)回路換熱器E0101的選型計(jì)算根據(jù)工藝條件選擇u型管式換熱器，因反應(yīng)產(chǎn)品的黏度較大且需要冷卻，所以水走殼程，導(dǎo)熱油走管程，設(shè)管程數(shù)為NP=2。計(jì)算定性溫度，確定物理常數(shù)管程（導(dǎo)熱油） 殼程（產(chǎn)品）定性溫度 t=（60+86.2%=73,10℃t=+1"SO）/?=172,40℃p2=3mpa.s=10.8kg/(m'h)pl=lOmpa.s=136kg/(m?h)物理常數(shù) Cp2=2.01kj/(kg*℃)Cpl=2.72k]/(kg*℃)(定性溫度下) 入=O.lOkcal/(h-nv℃)pl=1000kg/m3p2=960kg/m3初設(shè)總傳熱系數(shù)%=321.43kcal/(m2h?℃)=1350kJ/(n?-h?℃)2.L3計(jì)算對(duì)數(shù)平均溫度T1=18O℃ T2=164.8CCt2=86.2O℃ tl=60℃△tl=Tl-t2=180-86.2=93.8℃△t2=T2-tl=164.8-60=104.80℃(At-At)/ 104.80-93.80/；空=]而8。=9-，nAtl-93go計(jì)算溫度校正系數(shù)(T1-T2)/ _180-164.80_R- 86.20-60-0-58(t2-tl)/ _86,20-60_S=/'(Tl-tl)=180-60=0,22根據(jù)R、S值由P2-54圖8-12(a)查得溫度校正系數(shù)Ft=0.99△tm=Ft,Atm=0.99x99.20=97.20熱負(fù)荷Q及導(dǎo)熱油量W2Q=Wl-Cpl-Atl=360000X2.72X(180-164.80)=1.49X10?kI/h川Q/ 1-49X10/ ku.lw2=(Cp2,At2)= [2.01x(86.2-60)]=282629.6kg,h

計(jì)算所需的傳熱面積Flq, 1.49X107F1=(K-Atm)=1350X97.20=112170m2選定換熱器的參數(shù)由P4-358表23-41選取換熱器的面積119.40m2.管外徑do=0.025,管內(nèi)徑di=O.O2,管心距pt=O.O32,折流板缺口為25%,管子為正方形45°排列，管長(zhǎng)=6m,管子數(shù)Nt二Fl/(n?do?1)=233.54根,考慮到管子的排列問題，管子數(shù)取250根(Ds-do)/由P2-69圖8-28查得/Pt-1815,Ds-do=592mm, Ds=617mm根據(jù)加工原則取Ds=700mm計(jì)算給熱系數(shù)管程：管內(nèi)質(zhì)量流速4-W2?Nd.1 4X2X282629.6 ?Gi= ZNt?干3.14x(0。1)2x25。、7200754.14kg/(m,h),w,Rei雷諾準(zhǔn)數(shù),w,Rei雷諾準(zhǔn)數(shù)=13334.733= 10.80IIIP2-58圖8-13查得柯爾因子Jh=0.00452由公式Jh=[%3脾%)出口f[l\X014(pH=— =1.05因液體被加熱，黏度校正系數(shù)Id

管內(nèi)給熱系數(shù)hi=Jh.CpG（Cp,m入2尸（%卬-0.14/ 10.80\-3-0.14=0.0045x2.01x7200754.14x2.01x—=6353.69kj/(m-h?℃)殼程相鄰管間隙C=Pt-do=0.032-0.025=0.007m假定折流板間距B=0.30m質(zhì)量流速Gs=Ws//as360000/0046=7826086.96kg/(m2■h)橫過管束的流動(dòng)截面積as=Ds?C,B/Pt=0.70X質(zhì)量流速Gs=Ws//as360000/0046=7826086.96kg/(m2■h)當(dāng)量直徑29一荻%.呵=4x(0.0322-3.14 /29一荻%.呵=4x(0.0322-3.14 /4x0.0252,/(3.14X0.025)=0.02715md_d_Des,Gs/雷諾準(zhǔn)數(shù)R"= /|/10,8=19673-90由P2-59圖8-14查得管子為正方形排列，折流板缺口為25%,管外膜給熱系數(shù)Js=45.80.14液體被冷卻:pw=0.95h。6%爛"）明0.1445.8X液體被冷卻:pw=0.95h。6%爛"）明0.1445.8X0.42//0.02715X2.72X36/1//30.42X0.95=4142.61kJ/(m2?h?℃)2.L8計(jì)算總傳熱系數(shù)K1由P2-86附表8-18查得管內(nèi)污垢系數(shù)欽=0.0002m-h-℃/kcal=0.0000478mh℃/kj管外污垢系數(shù)丫。=0.0002n9.h?℃/kcal=0.0000478n??h?℃/kJ材質(zhì)采用不銹鋼，查得導(dǎo)熱系數(shù)入w=167.50kj/(m.h.℃)Iw/ 0.0025/ 廠uop\s管壁熱阻2=，入w= 167.50=149x10-5(m2?h?C)/kjKI=總傳熱系數(shù)1/ 1do/ , ,(yi,do)/,(yw-do)/ho+J(hi?di)+Y°+di+ dam_rl/,0.025/ ,nnnnn47Q(0.0000478x0.025)/=[4142.61+ /(6353.69x0,02)+0-0000478+ /q.02「/c“r0.025/ -1+1.4Jx10-5x/0.02251=1747.17儲(chǔ)備系數(shù)"=(1747.17-1350)/i35Q=02942=2942%(10%<乙<30%)K計(jì)/K選=1—1.30時(shí)，，可認(rèn)為初選合適，Kl/K0=L29所以選型合理2.1.9壓力降的計(jì)算管程Rei=13334.73由P2-63圖8-21查得摩擦因子段=0,0。5Gi/_7200754,14/ _OAom，管內(nèi)流體流速：UI=1(3600pi)= /(3600x960)=2-08m，sAPI=Np按公式0.816時(shí)/祖)(%認(rèn),卜】+0.255pui〃式中m-黏度系數(shù):m=0.14(Rei>2100,m=0.14)取(%W廠°"=%。5△Pi=2x0.816x/(0020x1.05)+0.255x960x2.08/2=4348.77kg/m2允許壓降=(25。-138)x1000/9.8=11428.57kg/m2(4348.77<11428.57)殼程由P2-63圖8-22查得當(dāng)Res=8277.4時(shí)殼程壓降摩擦因子餌=。?。52,TT_Gs/ _10975609.76/殼內(nèi)流體流速”!(3600pl)= /(3600x1000)=APs=0.816Jfs(D7Des)(7B)pUS/2(7RW)=0.816x0,052x(°-5/o,O2715)(7o,3O)x1000'允許壓降=(950-865)X1000=85000Pa2.1.10列出計(jì)算結(jié)果如下3.0鏟/1/“X.0.95=76519.08Pa(76519.08<85000)選單管程U型管式換熱器,管程數(shù)NP=2殼徑Dsmm700公稱壓力Pgatm16傳熱面積Flnr119.40管程數(shù)NP2管根數(shù)Nt250管長(zhǎng)1in6管徑dmm025x2.5板間距Bm0.3管子排列：正方形旋轉(zhuǎn)45。2.2反應(yīng)回路換熱器E0102的選型計(jì)算根據(jù)工藝條件選擇u型管式換熱器，因反應(yīng)產(chǎn)品的黏度較大且需要冷卻，所以水走光程，導(dǎo)熱油走管程，設(shè)管程數(shù)為NP=20計(jì)算定性溫度，確定物理常數(shù)

殼程（產(chǎn)品）管程（導(dǎo)熱油）殼程（產(chǎn)品）定性溫度 t=(60+80%=70OCt=(180+16580)/⑺皿物理常數(shù)（定性溫度下）[i2物理常數(shù)（定性溫度下）[i2=3mpa.s=10.8kg/(m?h)Cp2=2.01kj/(kg*℃)A=0.10kcal/(h-m-℃)p2=960kg/m3pl=5pa,s=18kg/(m?h)Cpl=2.72kJ/(kg?℃)pl=1000kg/m3初設(shè)總傳熱系數(shù)Ko=1200kJ/(n?JT℃)計(jì)算對(duì)數(shù)平均溫度T1=180℃ T2=165.8℃t2=8O℃tl=60℃△tl=Tl-t2=180-80=100^C△t2=T2-tl=165.8-60=105.80C⑷2-%)/ 105.80-100△2 1加2= 10/0 =102￡7K*Me計(jì)算溫度校正系數(shù)rri一12)/ 180—165.80R=( )/(t2Tl)=F^=0,71(t2-tl)/ 80-60_根據(jù)R、S值由P2-54圖8-12(a)查得溫度校正系數(shù)Ft=0.99Atm'=Ft?Atm=0.99x102.87=101.84

W?=108529.38kg/h熱負(fù)荷QW?=108529.38kg/hQ=2.51xIO6M/h計(jì)算所需的傳熱面積Flqt 2.51xIO6 2"=(K-Atm)=1200x101.84=20,5m226選定換熱器的參數(shù)lilP4-358表23-41選取換熱器的面積26.1nr.管外徑do=0.025,管內(nèi)徑di=0.02,管心距pt=0.032,折流板缺口為25%,管子為正方形排列，管長(zhǎng)=3m,管子數(shù)Nt=Fl/(ir-do-1)=87.05考慮到管子的排列問題,管子數(shù)取100根。=11.8(Ds-do)=11.8由P2.69圖8-28查得/Pt,Ds-do=352mm,Ds=403mm根據(jù)加工原則取Ds=500mm計(jì)算給熱系數(shù)管程：管內(nèi)質(zhì)量流速4x2x108529.38=6912699kg/(m3.14x(0.02/x1003.14x(0.02/x100雷諾準(zhǔn)數(shù)為:G.di.. 6912699x0.020Rei= 十:一io^b—=1280129由P2-58圖8-13查得柯爾因子Jh=0.0058

2由公式2由公式Jh=[%…(%J0.14(niX0-14(pji=— =1.00因液體被加熱，黏度校正系數(shù)2管內(nèi)給熱系數(shù)M=Jh.Cp?Gi?(Cp?W入2尸,(%)2/ 10.80\-3=0.0058x2.01x6912699x2.01x x1.00\ 0.43)=5809.8kl/(m-h?℃)2.2.7.2殼程相鄰管間隙C=Pt-do=0.032-0.025=0.007m假定折流板間距B=O.3Om橫過管束的流動(dòng)截面積as=DsCB/Pt=0.50x0.007x0.30/0.032=0.033m2質(zhì)量流速Gs=Ws/質(zhì)量流速Gs=Ws/360000/0033=1981707.32k&(m2.h)當(dāng)量直徑雷諾準(zhǔn)數(shù)以,2 3.144x(0.032--4x0.025/(3.14X0,025)=0-02715mDesGs/0.02715x1980952.32//18=雷諾準(zhǔn)數(shù)以,2 3.144x(0.032--4x0.025/(3.14X0,025)=0-02715mDesGs/0.02715x1980952.32//18=2987.44由P2-59圖8-14查得管子為正方形排列，折流板缺口為25%,管外膜給熱系數(shù)Js=2OJ\0.14液體被冷卻:=0.95his.(%/4)看「20x0.42/ Z10.8x2.01/ \hnnr= /0.02715X( 『042)X0.95=2574.65kJ/(m2?h℃)2.2.8計(jì)算總傳熱系數(shù)KlIIIP2-86附表8-18查得管內(nèi)污垢系數(shù)yi=0.0002m2-h?℃/kcal=0.0000478m2-h?℃/kJ管外污垢系數(shù)丫°=°?00°2m2-h-℃/kcal=0.0000478m2?h-℃/kJ材質(zhì)采用不銹鋼，查得導(dǎo)熱系數(shù)入w=167.50kj/(m,h.℃)管壁熱阻'入w=0002^167.50=149X10J(m2-h-℃)/kJ總傳熱系數(shù)9=1/ ,do/.? ?(yi?血)/-do)//ho+/(hi,di)+)'°+di+ /dami.of=[/257，l+' /(5809x0.02)+°，°°°°478+(0,0000478x0.025)//0.02..A-50.025/ 】i+L4Jx10X,0,02251=1374.56M/(m?h?℃)_(1374.56-1200)/ _八 匚。/儲(chǔ)備系數(shù)n= ；1200=02942=14.54(10%<”30%)K計(jì)/K選二1一1.30時(shí)，可認(rèn)為初選合適,K1/K0T.145所以選型合理2.2.9壓力降的計(jì)算管程Rei=12801.29IIIP2-63圖8-21查得摩擦因子用=0,0。6Gi/_6912699/ _om<管內(nèi)流體流速：U1= (3600pi)= (3600X960)=2"按公式API=Np0.816Jftf/dJ%w)m+0.255Pui/2式中m-黏度系數(shù):m=0.14(Rei>2100,m=0.14)%w)-014=1APi=2xF0.816X0.0006x3/ ,nnrrl… 、,(0020)+0,255x960x42=3799.29kg/m允許壓降=(250-210)x1000/9.8=4081.60k^m2(3799.29<4081.6)殼程IIIP2-63圖8-22查得當(dāng)Res=1756.44時(shí)殼程壓降摩擦因子餌=0,055,TIGs/_1980952.32/ ncr殼內(nèi)流體流速加="(3600pl)= /(3600x1000)=655sAPs=O.816Jfs(D7Des)(7B)PU72(VMW)-014si\/3； \ o55/=0.816x0.07x(/o.O2715)(/o.3O)x1000*,/2又1=1919.8kg/m2允許壓降=(950-890)x1000/9.8=6122.45kg/m2(1919.8<6122.45)2.2.10列出計(jì)算結(jié)果如下選單管程U型管式換熱器，管程數(shù)NP=2殼徑Ds mm 500公稱壓力Pg atm 16傳熱面積Fl m2 26.1管程數(shù)NP 2管根數(shù)Nt100管長(zhǎng)1管徑dmm025x2.5板間距B0.3管子排列正方形旋轉(zhuǎn)45。管子排列2.3反應(yīng)回路換熱器E0104的選型計(jì)算根據(jù)工藝條件選擇浮頭式換熱器，因反應(yīng)產(chǎn)品的黏度較大且需要冷卻，所以水走管程,導(dǎo)熱油走殼程，設(shè)管程數(shù)為NP=20計(jì)算定性溫度，確定物理常數(shù)殼程（產(chǎn)品）管程（導(dǎo)熱油）殼程（產(chǎn)品）定性溫度t=(3°^°)/2=350Ct=(84+6。)/[12=3.6kg/(m?h)pl=16.2kg/(m?h)物理常數(shù)Cp2=4.2kJ/(kg.℃)Cpl=1.98kJ/(kg-℃)（定性溫度下）A2=0.538kcal/(h-nr℃)pl=1000kg/m3p2=1000kg/m3XI=0.1kcaI/(h-m?℃)初設(shè)總傳熱系數(shù)^=1300^/(111?!!?℃)233計(jì)算對(duì)數(shù)平均溫度Tl=60℃T2=84℃Tl=60℃T2=84℃t2=40℃tl=3O℃t2=40℃tl=3O℃△tl=Tl-t2=60-30=30℃△t2=T2-tl=84-40=44℃2.3.7.12.3.7.1管程:z44-30Atm= ad= TT~=36.55℃/aiz 44m而哧計(jì)算溫度校正系數(shù)D_(T1-T2), _84-60_R= ，(t2—tl)=和面=24化2-tl) 40-307(Tl-tl)=ra=0.185根據(jù)R、S值由P2-54圖8-12(a)查得溫度校正系數(shù)Ft=0.98Atm=Ft?Atm=0.98x36.55=35.5℃熱負(fù)荷Q及導(dǎo)熱油量W2Q=1.59x107Q=1.59x107W/hWz=380031.3^計(jì)算所需的傳熱面積Flq.. 1.59xlO7Fl=/(K-Atm)=1300x35.5=34L8m2236選定換熱器的參數(shù)由P4-358表23-41選取換熱器的面積350m2.管外徑do=0.025,管內(nèi)徑di=0.02,管心距pt=0.032,折流板缺口為25%,管子為正方形45。排列，管長(zhǎng)=6m,管子數(shù)Nt=Fl/C-do?1)=743根，考慮到管子的排列問題，管子數(shù)取750根。(Ds-do)/由P2.69圖8-28查得 PL”,Ds-do=928mm,Ds=953.6mm根據(jù)加工原則取Ds=1000mm計(jì)算給熱系數(shù)管內(nèi)質(zhì)量流速c4?W2?Np/Gi=x/c4?W2?Np/Gi=x/區(qū)=/n-Nt-dj4x2X380031.33.14x(0.02)x750=3227442.03kg/(m2?h)G,dl/雷諾準(zhǔn)數(shù)Re1= /="930.23IIIP2-58圖8-13查得柯爾因子Jh=0.00612由公式(力2由公式(力0.14(pH因液體被加熱，黏度校正系數(shù)管內(nèi)給熱系數(shù)hi=hCpG(CpW入2戶(%w)■,2=0.0061X4.2X3227442.03xC，2.25)x1=23249.7kJ/(m-h?℃)殼程：相鄰管間隙C=Pt-do=0.032-0.025=0.007m假定折流板間距B=0.60m橫過管束的流動(dòng)截面積as=Ds?C?B/Pt=1x0.007x0.60/0.032=0.13m2質(zhì)量流速Gs=Ws/as=36。。。％13=2400000kg-(m2-h)、與量直徑:TOC\o"1-5"\h\zTT 2 3.144g/ 4X(0.032J1 )/n八24do2,/ _ 4x0,025/ nnnr7.rDes一 ，(n,do)一 /(3.14x0,025)=°-02715mDrcDes-Gs/0.02715x2400000/ 3八””雷諾準(zhǔn)數(shù)儂= m2= '16.2=4022.22由P2-59圖8-14查得管子為正方形排列，折流板缺口為25%,管外膜給熱系數(shù)Js=29液體被冷卻:<PM=pw0.14=10.14液體被冷卻:<PM=pw0.14=10.1429x0.42/ fl.974X16.2/ 一= 0.02715 /0.42)'I=3234.5kl/(m2?h?℃)算總傳熱系數(shù)KI由P2-86附表8-18查得管內(nèi)污垢系數(shù)yi=0.0002m-h?℃/kcal=0.0000478m-h?℃/kJ管外污垢系數(shù)丫°=0.0002m2?h?℃/kcal=0.0000478n??h?℃/kJ材質(zhì)采用不銹鋼，查得導(dǎo)熱系數(shù)入w=167.50kJ/（m.h"C）Iw/ 0.002S/ —5Uo「、h,管壁熱阻2='入w= 167.50=L49x10(m2?h?C)/kJ總傳熱系數(shù)Kl=1/ .do/tt(yi-do)/,(yw-do)/Kl=ho+/(hi,di)+Y°+di+dam1/ 0.025/ nnnnA7Q工(0.0000478x0.025)/；23249+ /(32345x0.02)+°*0000478+ 0.02n-50.025/J+L4JX1Ux/0.02251=1516.7k]/(m-h-℃)(10%<??<30%)(1516.7-1300)/(10%<??<30%)儲(chǔ)備系數(shù)11= /1300=16.6%K計(jì)/K選=1—1.30時(shí),可認(rèn)為初選合適，Kl/K0=1.16所以選型合理力降的計(jì)算

管程Rei=17930由P26圖8-21查得摩擦因子1=0008Gj/ 3227442/管內(nèi)流體流速：Ui=/(3600pi)= ，(3600xl000)=0?89m，s按公式APi=Np0,816Jftf/di)%w)m+0-255Pui/2按公式6,APi6,APi=2x0.816X0.008X+0.255]x1000X0嗎2=1729.72kg}1允許壓降=(400-274)x1000/9,8=12857.14kg/m2(1729.72<12857.14)殼程由P2-63圖8-22查得當(dāng)Res=2364時(shí)殼程壓降摩擦因子作=。。52,.._Gs/_2400000/ _n,Qm/殼內(nèi)流體流速出=(3600pl)= '(3600x1000)=668/sAPs=O.816Jfs(D7Des)(7B)pU72(%w)-0,142=0.816x0.076x(1/o.O2715)(6/o,6O)x1000x0，684=8804.65Pa允許壓降=(385-290)x1000=9693.87Pa (8804.65<9693.87)列出計(jì)算結(jié)果如下選浮頭式列管換熱器，管程數(shù)NP=2殼徑Dsmm1000公稱壓力Pgatm16傳熱面積Fl7nr350管程數(shù)NP

管長(zhǎng)1m6管徑dmm025x2.5板間距Bin0.6管子排列：正方形2.4導(dǎo)熱油加熱器E0103的選型計(jì)算根據(jù)工藝條件選擇浮頭式換熱器，導(dǎo)熱油走殼程，水走管程，設(shè)管程數(shù)為NP=2。計(jì)算定性溫度，確定物理常數(shù)殼程（產(chǎn)品）管程（導(dǎo)熱油）殼程（產(chǎn)品）定性溫度 t=203℃定性溫度 t=203℃t=(150+16。)/久物理常數(shù)（定性溫度下）卜物理常數(shù)（定性溫度下）卜i2=0.4824kg/(m?h)Cpg=0.58kcal/(m-h?℃)Cpl=1.07kcal/(mJv℃)Al=0.568kcal/QTnr℃)pg=840kg/m3pl=860kg/m3y=460.62kcal/kgpl=1.8kg/(m'h)Cpl=0.55k]/(kg*℃)

pl=900kg/m3XI=0.1kcal/(h-ni?℃)初設(shè)總傳熱系數(shù)^=2000^/(11?-h?℃)計(jì)算對(duì)數(shù)平均溫度T1=203℃ T2=2O3℃t2=160℃ tl=15O℃△tl=Tl-t2=203-160=43℃

△t2=T2-tl=203-150=53℃(At2-At)/ 53-43Atm= ' 1/At2=—―=47.8℃'瓦ln43計(jì)算溫度校正系數(shù)由于T1=T2,所以R=0,Ft=l不需要校正，所以Atm=47.80CW2=720kg/h熱負(fù)荷Q及蒸汽量W2W2=720kg/hQ=1.4xIO6kJ計(jì)算所需的傳熱面積Fl,q, 1.4xIO6 2Fl=(K?Atm)=2000x47.8=14,6m246選定換熱器的參數(shù)illP4-358表23-41選取換熱器的面積25.30m2.管外徑do=0.025,管內(nèi)徑di=0.02,管心距pt=0.032,折流板缺口為25%,管子為正方形排列，管長(zhǎng)=4.5m,管子數(shù)Nt=Fl/(n-do?1)=70.7根，考慮到管子的排列問題，管子數(shù)取75根。(Ds-do)/由P2.69圖8-28查得 Pt-JbJDs-do=313.6mm,Ds=338.6mm根據(jù)加工原則取Ds=400mm計(jì)算給熱系數(shù)管程管內(nèi)質(zhì)量流速4x2X7203.14x(0.02)2x75=611464x2X7203.14x(0.02)2x75=61146kg/(m2?h)G「di/雷諾準(zhǔn)數(shù)：Rei=U=2537IllP”8圖8-13查得柯爾因子Jh=0.0031/2GE=G)+Gg(PL/pG)=1.42X105+1.42x105X(860/814)2=287957kg/hD.GEdi/0.02x287957/11QQQr9Re】=/川= /04824=11938.52查圖8-16得<P=140/humdi/\zCpl-ul/.3140x2.38/ 4,494x0,4824；甲=(R(/A)= /0.02x( .2.38)=126890.02kg/(m2-h)殼程相鄰管間隙C=Pt-do=0.032-0.025=0.007m假定折流板間距B=O.3Om橫過管束的流動(dòng)截面積as=Ds?C,B/pt=0.40x0.007x0.30/0.032=0.02625m2質(zhì)量流速Gs=WS/as=360000/0.02625=1108x10?k^'(m2,h)當(dāng)量直徑TT4岫一破"TT4岫一破"4X(0,0322-Des= /(n-do)=3.14 /4x0,02521,(3.14x0,025)=0*02713mnDes-Gs/0.02715x1.05x10/雷諾準(zhǔn)數(shù)Res= ,42= /L8=106400由P2-59圖8-14查得管子為正方形排列，折流板缺口為25%,管外膜給熱系數(shù)Js=90液體被冷卻:<PM=|IW0.14=1液體被冷卻:<PM=|IW0.14=1ho=ho=Js-_90x0.42/ (2.72x36/ 「3.0.02715xI -0.42Jx1=5078.lM/(m2-h-℃)計(jì)算總傳熱系數(shù)KI由P2-86附表8-18查得管內(nèi)污垢系數(shù)yi=0.0002m2-h?℃/kcal=0.0000478m2-h?℃/kJ管外污垢系數(shù)Y°=0.0002m2?h?℃/kcal=0.0000478m2?h?℃/kJ材質(zhì)采用不銹鋼，查得導(dǎo)熱系數(shù)入w=167.50kj/(m?h?。0管壁熱阻e入w=0002J/167.50=149x101(m"-h-℃)/kJlz1 4.do/、工、小Jyi'do)/(yw-do)/y1總傳熱系數(shù)KI一( +(hi,di)+)。+di+dam]_rl/x0,025/ 工0nnnn47Q,(0-0000478X0.025)/=[,5078.6+ /(126890.2x0.02)+°-0000478+ ,0.02A-50.025/ii+L4JX10x/0.02251=2383.57M/(m-h?℃)(2383.512。。。)/2ooo=o2o=2o%K計(jì)/K選=1—1.30時(shí),可認(rèn)為初選合適,Kl/K0=L20所以選型合理。壓力降的計(jì)算殼程Rei=106400,由P?6圖8-21查得摩擦因子母=。?。57管內(nèi)流體流速：Ui=G1(3600pi)=L08xWZ(3600x960)=3ms.=0.816Jfs(Ds/Des)(7B)(7RW)pUi/2式中m-黏度系數(shù):m=0.14(Rei>2100,m=0.14),取=APi=(0.816X0,05X4%3x°-4/o,O2715]x(%()**%=6428.57kg/m2允許壓降=(385-315)x1。。。/9.8=7142.86kg/m2(6428.57<7142.86)列出計(jì)算結(jié)果如下選浮頭式列管換熱器，管程數(shù)NP=2殼徑Dsmm400公稱壓力Pgatm16傳熱面積F1in225.6管程數(shù)NP2管長(zhǎng)1m4.5管徑dmm025x2.5板間距Bm0.3管子排列：正方形第3章泵的選擇PC-0101反應(yīng)回路循環(huán)泵揚(yáng)程計(jì)算用途：把(17)號(hào)管線的液體輸送到SA-0101管路上有三個(gè)90彎頭，三個(gè)閥門，一個(gè)換熱器E0101,二個(gè)三通，PC-0101液體流速360000,密度1000,溫度180,人口壓力450,排出壓力855,轉(zhuǎn)速1450,黏度10。流體形態(tài)”?算ms/Vs=pTOC\o"1-5"\h\z360000/ —3ms/Vs=pd=200mm/1000=360m/hd=200mmVQ/ 36。(u=7a= / 2=3.18m/s'A/(3600x0.785x0.2z)ndup/(0.2x3.18x1000).. -in4Re=7“=' ，/ -3=6.4x10>40003 /(lOx10)???湍流流動(dòng)3.L2摩擦因數(shù)07543/入=0.01227+. /o38=0,0235/Re3.1.3泵的揚(yáng)程2II=Az+ ，2g+P/pg+A叫由于M=8m(巳知)忽略動(dòng)能變化，即%=。叫g(shù)=四-5。）x】。。。/we28mAhf=Ahfl+Ahf2名稱阻力系數(shù) 數(shù)量管出口甲。二1管入口(Pj=0.590彎頭(P=0.75 三個(gè)三角落<P=1 二個(gè)管通長(zhǎng) 5m=3.27m中途經(jīng)過E0101換熱器，此處局部阻力為酊行E0101 Ds=1.0mNt=404 di=0.017 1=6mV1=V2 Alul=A2u2A1U1/fdi/V0.22x3.18/ Imu7= 'a= " ，U]= 9 =1.09m,s2A2Id2/ 1 /(0.017"x404)屬于湍流區(qū)，取入=0.022,貝產(chǎn)以=制+聞'U/zg2/0.022x6/1c一八1.09/ nrrm<=( /0.017+°5+l)x ,(2x9,81)=0156sAhf=Ahfl+Ahf2=3.27+0.56=3.83mH=Az+加/2g+即/pg+Ahf=8+41.28+3.83=53.11m3.2PC-0101反應(yīng)回路循環(huán)泵的選型查得泵型號(hào)200YG75流量Q360m3/h揚(yáng)程H75m轉(zhuǎn)數(shù)1450r/min效率n75%軸功率98kw配電機(jī)功率132kw允許氣蝕余量Ah4.5m泵殼許用壓力16kgf/cm2第4章中和釜體積及攪拌器功率計(jì)算4.1中和釜體積計(jì)算年產(chǎn)量W1=60000噸，一年工作日Tl=300天，物料比重(：P=lOOOkg/n/取裝料系數(shù)S=0.8(反應(yīng)物料為液相取0.75-0.8),日產(chǎn)量%=*=答=20批每日生產(chǎn)批數(shù)C=Wox/r'=6076.03/(40/60)=9114.05依/h貝IJ每小時(shí)的工作量明=K，2X10Q0=2000x1000=8333.4kg/h,T2=24hTOC\o"1-5"\h\zT? 24工作周期7；=馬=*=12?3卬3 20每小時(shí)物料體積匕=-J-= =8.333W/hL1000 1000設(shè)備總?cè)莘eMv=SG=8333-4*L2=已⑤/S0.83實(shí)際設(shè)備總體積Va=13m4.2攪拌器的功率計(jì)算因?yàn)橐后w黏度不大，對(duì)溶介速度無(wú)要求可用漿式攪拌器，所以選漿式攪拌器d/取 /p=0.5D=2.4m所以 d=2.4x0.5=1.2m 取u=3m/sN=u'TTd=3/(3.14X1.2)=01796r，sDnpNd2/1000x0.796x1.22/ QRe=3= /(H)5=22924.8d/ 1/取 /B=5 B=1,2x,5=0,24m

C=10EXI^1.3-4x(B/d-O.s2)-1，14d/D=10,94A=14+C=10EXI^1.3-4x(B/d-O.s2)-1，14d/D=10,94A=14+%)卜70x%-0.6)2+1850.24=14+”xfl.2\2670xk^-06+185=33.17413,d/p=l.l+/d-2.5-</d-0.5)=1.5A[1000+L2Re°”]P/H\(0?35十b/d)Np_Re+C1000+3,2Re0-^W(sin0)1,2(取H/d=ih=90°),33.1722924.8+10.94X1000+1.2x22924.80661L5*十。.1)1000+3.2X22924.80,66xl1,2=4.56所以，p=NppN3d5=4.56x1000x0.7963x1.25=5722.8W設(shè)備一覽表序號(hào)位號(hào)設(shè)備名稱技術(shù)規(guī)格介質(zhì)數(shù)量單位材料Mft(kg)備注總1R0101反應(yīng)氣液接觸！器臥式①1200X10X7000：V=8/54M3外半管4>73/60.3X3：保溫層厚度120mm