化工設(shè)計(jì)答辯終稿

二硫化碳-四氯化碳蒸餾分離過程與精餾塔的設(shè)計(jì)湖南師范大學(xué)“大鬧化工隊(duì)”團(tuán)隊(duì)成員：郭駿、王瑛璞、韓鵬指導(dǎo)老師：趙海紅設(shè)計(jì)任務(wù)書1)生產(chǎn)能力：10噸每小時(shí)（料液）2)原料組成：34%的二硫化碳和66%的四氯化碳（摩爾分率，下同）3)產(chǎn)品組成：餾出液97%的二硫化碳，釜液5%的二硫化碳4)操作壓力：塔頂壓強(qiáng)為常壓5)進(jìn)料溫度：58℃6)進(jìn)料狀況：自定7)加熱方式：間接蒸汽加熱8)塔板效率:0.5；9)建廠地址：湖南長(zhǎng)沙地區(qū)；10)其他參數(shù)（除給出外）可自選。目錄摘要······················································3前言······················································4第一章設(shè)計(jì)方案簡(jiǎn)介·································61.1流程的設(shè)計(jì)及說明·······························61.2已知參數(shù)···········································71.3選塔依據(jù)··········································7第二章設(shè)計(jì)計(jì)算······································92.1精餾流程的確定··································92.2塔的物料衡算····································102.3塔板數(shù)計(jì)算········································11第三章板式塔主要工藝尺寸設(shè)計(jì)計(jì)算············163.1塔工藝條件及物性數(shù)據(jù)計(jì)算···················163.2精餾塔氣液負(fù)荷計(jì)算····························203.3塔和塔板主要工藝尺寸計(jì)算···················203.4篩板的流體力學(xué)驗(yàn)算····························253.5塔板負(fù)荷性能圖··································29

3.6精餾塔的計(jì)算結(jié)果總表·························36第四章精餾塔的附屬設(shè)備以及接管尺寸·········394.1接管設(shè)計(jì)···········································394.2塔總高度計(jì)算

·····································404.3熱量衡算············································414.4再沸器的選擇······································444.5泵的選型············································444.6主要符號(hào)說明······································46參考文獻(xiàn)·················································49設(shè)計(jì)結(jié)果評(píng)述與小結(jié)··································50致謝·······················································51附錄·······················································53人員分配BOSS:趙海紅老師“藝術(shù)總監(jiān)”：韓鵬“項(xiàng)目經(jīng)理”：郭駿“高級(jí)工程師”：王瑛璞原料液經(jīng)過預(yù)熱器預(yù)熱后進(jìn)入精餾塔內(nèi)。操作時(shí)連續(xù)的從再沸器中取出部分液體作為塔底產(chǎn)品（釜?dú)堃海?。再沸器中原料液部分汽化，產(chǎn)生上升蒸汽，依次通過各層塔板。塔頂蒸汽進(jìn)入冷凝器中全部冷凝，然后進(jìn)入回流罐，并將冷凝液送回塔頂作為回流液體，其余部分經(jīng)過冷凝器后被送出作為塔頂產(chǎn)品。為了使精餾塔連續(xù)的穩(wěn)定的進(jìn)行，流程中還要考慮設(shè)置原料槽、產(chǎn)品槽和相應(yīng)的泵。為了便于了解操作中的情況及時(shí)發(fā)現(xiàn)問題和采取相應(yīng)的措施，常在流程中的適當(dāng)位置設(shè)置必要的儀表，比如流量計(jì)、溫度計(jì)和壓力表等，以測(cè)量物流的各項(xiàng)參數(shù)。

設(shè)計(jì)方案的選定物料衡算能量衡算塔的位置CS2的質(zhì)量分率平均分子量（g/mol）物料衡算kmol/h塔頂aD=0.941MD=78.34D=24.73進(jìn)料aF=0.203MF=127.48F=53.71塔釜aW=0.0251MW=150.1W=78.44單位總熱量Qv塔頂溜出液熱量QD回流熱量QR進(jìn)料熱量QF塔底殘液熱量QW水蒸氣還需要提供熱量Qh冷凝器消耗的熱量Qc再沸器提供的熱量QBkJ/h3526022918353277186372925444999279331064693450568物料流程圖塔板數(shù)的確定確定方法根據(jù)相平衡方程和操作線方程，采用逐板計(jì)算求得塔板數(shù)理論板數(shù)總理論板數(shù)為11（包括蒸餾釜），精餾段理論板數(shù)為5，第6板為為進(jìn)料板，提餾段理論板數(shù)為6∴NT=（11-1）=10層（不包括塔釜）

塔板效率

ET=0.5

實(shí)際板數(shù)精餾段：N精=5/ET=5/0.5=10層；提餾段：N提=5/ET=5/0.5=10層計(jì)算表格xD=0.9700y1=0.9700x1==0.9258y2=0.9354x2=0.8482y3=0.8478x3=0.7296y4=0.7822x4=0.5810y5=0.6661x5=0.4351y6=0.5522x6=0.3225xf=0.3330y7=0.4568x7=0.2451y8=0.3412x8=0.1666y9=0.2241x9=0.1003y10=0.1251x10=0.0523y11=0.0535x11=0.0214xw=0.05塔體工藝尺寸的確定板間距的選擇板間距取0.4m

塔徑的確定將提餾段與精餾段取相同的塔徑，故取1.4m塔板主要工藝尺寸的確定

塔板類型篩板塔

板上液體的流型單流型

是否分塊是分四塊塔板結(jié)構(gòu)（區(qū)域、開孔數(shù)目）取邊緣區(qū)寬度Wc=0.035m，安定區(qū)寬度Ws=0.065m

塔板結(jié)構(gòu)圖主體設(shè)備裝配圖塔板的流體力學(xué)驗(yàn)算類型霧沫夾帶量eV篩板的穩(wěn)定性系數(shù)k液泛m單板壓降pa精餾段提餾段塔板負(fù)荷性能圖操作彈性操作彈性

pp配管計(jì)算管型進(jìn)料管回流管塔底出料管塔頂蒸汽出料管塔底蒸汽進(jìn)氣管規(guī)格接管尺寸由內(nèi)蒸汽速度及體積、流量決定，各接管允許的蒸汽速度查表得標(biāo)準(zhǔn)設(shè)備的選型選型方法再沸器的選擇選擇120℃水蒸氣加熱，傳熱系數(shù)取出料液溫度

泵的選型由額定流量和揚(yáng)程確定公稱直徑1mm管程數(shù)NP排管數(shù)n管程流通面積1m2換熱面積A/m2換熱管長(zhǎng)度L/mm40041290.005955.64500型號(hào)50AY-60B流量10揚(yáng)程m40功率機(jī)4軸2.9轉(zhuǎn)速2950效率37%泵殼許用壓力16126結(jié)構(gòu)單級(jí)

致謝經(jīng)過兩個(gè)多月的化工原理課程設(shè)計(jì)，我已明白課程設(shè)計(jì)對(duì)我來說的意義，它不僅僅是讓我們把所學(xué)的理論知識(shí)與實(shí)踐相結(jié)合起來，提高自己的實(shí)際動(dòng)手能力和獨(dú)立思考的能力，更重要的是同學(xué)間的團(tuán)結(jié)，雖然我們這次花去的時(shí)間比別人多，但我相信我們得到的也會(huì)更多!

作為一名化工學(xué)院的大三學(xué)生，我覺得課程設(shè)計(jì)是十分有意義的，而且是十分必要的。在已度過的大學(xué)時(shí)間里，我們?cè)谡n堂上掌握的僅僅是理論知識(shí)，如何