甲醇制氫裝置冷凝器(E0103)設(shè)計(jì)

JINJING本科畢業(yè)設(shè)計(jì)甲醇制氫裝置冷凝器(E0103)設(shè)計(jì)學(xué)院化工與藥學(xué)院專業(yè)過(guò)程裝備與控制工程年級(jí)班別學(xué)號(hào)學(xué)生姓名指導(dǎo)教師2015年05月10日荊楚理工學(xué)院畢業(yè)設(shè)計(jì)②用鋼管作圓筒時(shí)，其尺寸允許偏差應(yīng)符合GB/T8163和GB/T14976的規(guī)定。（2）圓筒同一斷面上，最大直徑與最小直徑之差為，且：當(dāng)時(shí)，其值不大于；當(dāng)時(shí)，其值不大于；在本設(shè)計(jì)中其值不大于。（3）圓筒直線度允許偏差為（為圓筒總長(zhǎng)），且：當(dāng)時(shí)，其值不大于；當(dāng)當(dāng)時(shí)，其值不大于。在本設(shè)計(jì)中其值不大于。（4）直線度檢查，應(yīng)通過(guò)中心線的水平和垂直面，即沿圓周四個(gè)部位測(cè)量。（5）殼體內(nèi)壁凡有礙管束順利裝入或抽出的焊縫均應(yīng)磨至與母材表面齊平。（6）在殼體上設(shè)置接管或其他附件而導(dǎo)致殼體變形較大，影響管束順利安裝時(shí)應(yīng)采取防止變形措施。（7）插入式接管、管接頭等，除圖樣另有規(guī)定外，不應(yīng)伸出管箱、殼體和頭蓋的內(nèi)表面。11.2管箱管箱短節(jié)與接管和管箱法蘭組焊時(shí)，應(yīng)以法蘭端面為基準(zhǔn)。且螺孔應(yīng)與設(shè)備主軸中心線跨中。管箱隔板組裝前，須將管箱內(nèi)和隔板結(jié)合的環(huán)焊縫部位鏟磨齊平，并把隔板和管箱經(jīng)測(cè)量、劃線、調(diào)整好間隙后再裝焊。組裝、焊接管箱隔板，靠近密封面區(qū)域需焊透，防應(yīng)力集中而開(kāi)裂。11.3換熱管換熱管管端外表面應(yīng)除銹。用于焊接時(shí)，管端清理長(zhǎng)度應(yīng)不小于管外徑，且不小于。11.4管板（1）管板孔直徑及允許偏差按GB151-1999《管殼式換熱器》規(guī)定。（2）孔橋?qū)挾绕罟馨迳嫌泻芏喙芸?，其孔心距尺寸偏差的大小直接影響焊管和脹管的施工質(zhì)量，所以限制鉆孔背面的孔橋?qū)挾绕?，以便于檢查。終鉆（出鉆）一側(cè)管板表面，相鄰兩管孔之間的孔橋?qū)挾劝碐B151-1999規(guī)定。終鉆后應(yīng)抽查不小于管板中心角區(qū)域內(nèi)的孔橋?qū)挾?，值得合格率?yīng)不小于，允許的最小寬度的數(shù)量應(yīng)控制在之內(nèi)，超過(guò)上述合格率時(shí)，應(yīng)全管板檢查。（3）本設(shè)計(jì)中換熱管與管板焊接連接，管孔表面粗糙度值不大于。11.5換熱管與管板的連接換熱管與管板的連接是管殼式換熱器中最主要的問(wèn)題，因?yàn)閮烧咧g的連接處通常是換熱器容易滲透的地方，若連接質(zhì)量不好，則直接影響工藝操作的正常進(jìn)行。（1）連接部位的換熱管和管板孔表面應(yīng)清理干凈，不應(yīng)留有影響焊接連接質(zhì)量的毛刺、鐵屑、銹斑、油污等。（2）焊渣及凸出于換熱管內(nèi)壁的焊瘤均應(yīng)清除。焊縫缺陷的返修，應(yīng)清除缺陷后焊補(bǔ)。（3）換熱管與管板的強(qiáng)度焊焊接接頭，接施焊前應(yīng)按GB151-1999《管殼式換熱器》中附B作焊接工藝評(píng)定。11.6折流板（1）折流板的管孔直徑及允許偏差按GB151-1999《管殼式換熱器》規(guī)定，但允許超差的管孔數(shù)不得超過(guò)。（2）折流板外圓表面粗糙度值不大于，外圓面兩側(cè)的尖角應(yīng)倒鈍。（3）應(yīng)去除折流板上的任何毛刺。到此，換熱器結(jié)構(gòu)設(shè)計(jì)及強(qiáng)度計(jì)算已經(jīng)基本結(jié)束?？梢哉f(shuō)，換熱器的主要設(shè)計(jì)計(jì)算已經(jīng)完成，其計(jì)算結(jié)果將通過(guò)裝配圖、部件圖以及零件圖表現(xiàn)出來(lái)。主要參考文獻(xiàn)[1]賈紹義,柴誠(chéng)敬主編.化工原理課程設(shè)計(jì)[M].天津大學(xué)出版社.2003.[2]王志魁,劉麗英，劉偉編.化工原理.第四版[M].北京化學(xué)工業(yè)出版社.2010.[3]方書(shū)起主編.化工設(shè)備課程設(shè)計(jì)指導(dǎo)[M].北京.化學(xué)工業(yè)出版社.2010.[4]國(guó)家醫(yī)藥管理局上海醫(yī)藥設(shè)計(jì)院編[M].化工工藝設(shè)計(jì)手冊(cè).化學(xué)工業(yè)出版社.[5]錢(qián)頌文.換熱器設(shè)計(jì)手冊(cè)[M].北京.化學(xué)工業(yè)出版社.2002.[6]中華人民共和國(guó)國(guó)家標(biāo)準(zhǔn)GB151-1999《鋼制管殼式換熱器》.[7]中華人民共和國(guó)國(guó)家標(biāo)準(zhǔn)GB150-2011《壓力容器》.[8]JB/T4736-2002《補(bǔ)強(qiáng)圈標(biāo)準(zhǔn)》.[9]HG/T20592-206352009《鋼制管法蘭、墊片和緊固件》.[10]根據(jù)GB713-2008《鍋爐和壓力容器用鋼板》和GB3531《低溫壓力容器用低合金鋼板》.NewplateheatexchangeroptimizationSelectionW.LubandS.A.TassoubDepartmentofMechanicalEngineering,SchoolofEngineeringandDesign,BrunelUniversity,Uxbridge,Middlesex,UK.[Abstract]:TheplateheatexchangerSelectionisbasedontheoptimizationoftheuseofheatexchangersandintheprocessoftheparametersandNTU=KA/MC=△t/△tm,thatis,transferunitsofNTUandthetemperaturedifferencethan(theaveragetemperaturedifference--Heattransferinpower)chooseplateshapes,plateheatexchangerandthetypeofstructure.[Keywords]:theaveragetemperaturedifferencebetweenNTUplateevaporatorcondenser1meantemperaturedifference△tmFromtheformulaQ=K△tmA,△TM=1/A∫A(T1-T2)dAknowable,meantemperaturedifference△TMisthedrivingforceforheattransfer,flowform,suchastocalculatetheaveragetemperature,thesurfacetemperaturedifferencebetweenthefluidonbothsidesoftheaverageareavalue,canheatexchangeheatexchanger.Theaveragetemperatureisamoreintuitiveconcept,butalsoanimportantindextoevaluatetheperformanceofplateheatexchanger1.2thenumberoftransferunitsIntheheattransferunitoftheintroductionofafewdimensionlessparametersNTU,knownasthenumberoftransferunits,itsaidplateheatexchangerofthetotalthermalconductivity(heatexchangerheatresistanceofthecountdown)andtheratiooffluidheatcapacityNTU=KA/MC,itsaidinrelationtoheatfluidflow,heattransfercapacityoftheheatexchangerofthesizeoftheheatexchangerthatis,non-dimensional"heattransfercapability."Theplateheatexchangerfor,KA/MC=△t/△tm,where△t/△tmknownasthetemperaturedifferencethan,ontherightsideoftheprocessusedNTUpthatlefttheconditionsofheattransferequipmentusedNTUEsaid.NTUpisfluidtemperaturechangesintemperatureandtheaverageratiothatisused1℃△tmofseveralchangesinthevalueoffluidtemperaturechanges,when△tmlarge,NTUpissmallwhen△tmhours,ithasbecomebiggerThetendency.Onthecontrary,inNTUplargerintheprocess,△tmofthelargertemperaturechanges,NTUpsmaller,its△tmsmallchangesintemperature(seetable1).Plateheatexchanger,theoptimaldesign,isknownNTUEtemperaturedifferencethantheconditions,todetermineareasonablemodel,processesandheattransferarea,equivalenttoNTUpNTUE.Table1△tm,NTUprelations△tm大△tm小NTUp小NTUp大NTUp大NTUp小△tm的溫度變化大△tm的溫度變化小1.3heattransferprocessandtheNTUHeatingandair-conditioningrelatedtotheheattransferprocessiftheshowareasfollows:⑴steamheatingwater⑵water-waterheatexchangera.steam133→133℃c.awater65→60℃Water5→65℃(hotwater)Secondarywater45←40℃(heating)b.Steam133→133℃d.awater14→9℃Water55→65℃(heating)secondarywater13←7℃(refrigeration)e.awater29→24℃Secondarywater26←21℃(refrigeratorcooling)MorethanfivecasesoftheprocessNTUp(seetable2)Table2heatingair-conditioningprocessofNTUp過(guò)程△tmNTUpa133→133℃5→65℃94.86（65－5）／94.86＝0.632b133→133℃55→65℃72.88（65－55）／72.88＝0.13c65→60℃45←40℃20.00（45－40）／20＝0.25d14←9℃13←7℃1.44（13－7）／1.44=4.17e29→24℃26←21℃3.00（26－21）／3＝1.671.4plateheatexchangerandNTUENTUEplateheatexchangerthatthecapacityofheatexchangeristhesizeofacertainlengthoftheheatandthecombinationofheattransferunits,thetotallengthofheattransferprocessisthelengthandnumberofunitsoftheproduct.WhenthetotalnumberofNTUEis,ifthenumberofprocessesforevery1NTUe,thenNTUE=n?NTUe(wherenisthenumberofprocesses).WhenNTUe=NTUE=NTUp,theheatexchangerforone-way.IfNTUe<NTUp,theheatexchangerformanyprocesses,itshouldbedesignedtotargetn.Aseachplateofone-wayNTUevalueisessentiallyfixedvalue,suchasineTable2fortheflowof25m3/hoftheone-wayNTUeplateheatexchangerfor17squaremeters.FromNTUe=A?K/MCtellsusthatwhenNTUetobeonduty,A?Kisinverselyproportional,stilleexample,whenK=500kcal/㎡?h?℃time,A=1.67×25000/500=83.5㎡,theprocessofn=83.5/17≈5.WhenK=2500kcal/㎡?h?℃time,A=16.7squaremeters,theflowofn=1.EachprocessNTUeasfollows:K=500,NTUe=NTUE/n=0.33,K=2500when,NTUe=1.67.So,canbeobtainedunderNTUetheflowofheatexchangers,heattransfercoefficientandheattransferarea.Fromtheabovewecanseethatiftheplateheatexchangerdesignunreasonableandlikelytoheattransferareaistoolarge,mayalsobepartitionedsothatflowistoohigh,toomuchresistance.1.5plateheatexchangermanufacturingandtechnologicalprogress,platetypeofincrease,raisingtheplateheatexchangerofthevariousprocessesofadaptation.（1）theNTU(∽8),small△tm(∽1~2)theplateheatexchangertomeetthedistrictcoolingandheatpumpunitsevaporator,condenserrequirements.Fromtheaboveanalysisknow,△tmisthedrivingforceofheattransfer,if△tmsmall,meansthatthedriverofsmall,toachievetheheattransferbetweenthetwofluid,wemustincreaseheattransfercoefficient,increasingheattransferarea,inordertoHeattomakeuptoolarge,istheonlyincreaseheattransfercoefficientK.（2）smallNTU(∽0.3~2),the△tm(∽40~90℃)oftheplateheatexchangertomeettheheatrecoveryprocessandtheprocessheatingandcoolingrequirements.Whentheprocessinthe△tmconductedunderconditionsofheattransfer,thatdrivingforce,theheatandthesmaller,theheattransfercoefficientdemandisnothigh,butthatthisprocessorhigh-pressurework,orworkHightemperature,orprocessheatingandcoolingprocessintheliquidcontainingfiberdiameterorlargerparticles,theplateheatexchanger,thepressure,temperatureandabilitytorequest,theheatexchangertotheplatespacingrequirements.換熱器的優(yōu)化選型W.Lub和S.A.Tassoub英國(guó)米德?tīng)柸怂梗剪攦?nèi)爾大學(xué)機(jī)械設(shè)計(jì)工程部[摘要]板式換熱器的優(yōu)化選型是根據(jù)換熱器的用途和工藝過(guò)程中的參數(shù)和NTU＝KA／MC＝△t／△tm，即傳熱單元數(shù)NTU和溫差比（對(duì)數(shù)平均溫差—換熱的動(dòng)力）選擇板片形狀、板式換熱器的類型和結(jié)構(gòu)。[關(guān)鍵詞]平均溫差NTU板式蒸發(fā)器冷凝器1平均溫差△tm從公式Q＝K△tmA，△tm＝1／A∫A（t1－t2）dA中可知，平均溫差△tm是傳熱的驅(qū)動(dòng)力，對(duì)于各種流動(dòng)形式，如能求出平均溫差，即板面兩側(cè)流體間溫差對(duì)面積的平均值，就能出換熱器的傳熱量。平均溫差是一個(gè)較為直觀的概念，也是評(píng)價(jià)板式換熱器性能的一項(xiàng)重要指標(biāo)。1.2傳熱單元數(shù)法在傳熱單元數(shù)法中引入一個(gè)無(wú)量綱參數(shù)NTU，稱為傳熱單元數(shù)，它表示板式換熱器的總熱導(dǎo)（即換熱器傳熱熱阻的倒數(shù)）與流體熱容量的比值NTU＝KA／MC，它表示相對(duì)于流體熱容流量，該換熱器傳熱能力的大小，即換熱器的無(wú)量綱“傳熱能力”。對(duì)于板式換熱器來(lái)說(shuō)，KA／MC＝△t／△tm，式中△t／△tm稱為溫差比，上式中的右邊的工藝過(guò)程用NTUp表示，左邊的換熱設(shè)備的條件用NTUE表示。NTUp是流體溫度的變化與平均溫差的比值，表示的是用1℃△tm的變化引起幾度流體溫度變化的值，當(dāng)△tm大時(shí)，NTUp則小；當(dāng)△tm小時(shí)，它有變大的傾向。相反，在NTUp變大的過(guò)程中，△tm的溫度變化較大，NTUp較小時(shí)，其△tm的溫度變化較小（見(jiàn)表1）。板式換熱器的優(yōu)化設(shè)計(jì)計(jì)算，就是在已知溫差比NTUE的條件下，合理地確定其型號(hào)、流程和傳熱面積，使NTUp等于NTUE。表1△tm，NTUp的關(guān)系△tm大△tm小NTUp小NTUp大NTUp大NTUp小△tm的溫度變化大△tm的溫度變化小1.3換熱過(guò)程和NTU與供熱空調(diào)相關(guān)的換熱過(guò)程如下如示：⑴用蒸汽加熱水⑵水—水換熱蒸汽133→133℃c.一次水65→60℃水5→65℃（生活熱水）二次水45←40℃（采暖）b.蒸汽133→133℃d.一次水14→9℃水55→65℃（采暖）二次水13←7℃（制冷）e.一次水29→24℃二次水26←21℃（制冷機(jī)的冷卻）以上5例工藝過(guò)程的NTUp（見(jiàn)表2）表2供熱空調(diào)工藝過(guò)程的NTUp過(guò)程△tmNTUpa133→133℃5→65℃94.86（65－5）／94.86＝0.632b133→133℃55→65℃72.88（65－55）／72.8