1200噸丙酮-水連續(xù)填料精餾塔設(shè)計(jì)-化工原理課程設(shè)計(jì)

化工原理課程設(shè)計(jì)1200噸丙酮-水連續(xù)填料精餾塔設(shè)計(jì)學(xué)院：化學(xué)生物與材料科學(xué)學(xué)院專業(yè)：化學(xué)工程與工藝設(shè)計(jì)人：二零一六年六月設(shè)計(jì)任務(wù)一、設(shè)計(jì)題目設(shè)計(jì)分離丙酮-水混合液的填料精餾塔。二、設(shè)計(jì)數(shù)據(jù)及條件1、生產(chǎn)能力年處理丙酮-水混合液：1200噸（開工率：300/年）；2、原料組成丙酮含量為80%（質(zhì)量百分率，下同），水含量為20%3、分離要求產(chǎn)品中水分含量≤4%（質(zhì)量分?jǐn)?shù)）殘夜中丙酮含量≤4%（質(zhì)量分?jǐn)?shù)）4、設(shè)計(jì)條件操作方式：連續(xù)精餾操作壓力：常壓進(jìn)料狀態(tài)：飽和液體進(jìn)料回流比：R=3.59塔填料：500Y金屬孔板波紋填料塔頂冷凝器：全凝器三、設(shè)計(jì)計(jì)算內(nèi)容1、物料衡算2、填料精餾塔計(jì)算=1\*GB2⑴操作條件的確定=2\*GB2⑵塔徑的確定=3\*GB2⑶填料層高度的確定=4\*GB2⑷填料層壓降的計(jì)算=5\*GB2⑸液體分布器設(shè)計(jì)計(jì)算=6\*GB2⑹接管管徑的計(jì)算3、冷凝器和再沸器的計(jì)算與選型4、填料塔結(jié)構(gòu)圖、填料結(jié)構(gòu)圖、填料支撐板結(jié)構(gòu)圖摘要本設(shè)計(jì)任務(wù)是“1200噸丙酮-水連續(xù)填料精餾塔設(shè)計(jì)”。通過(guò)該課程設(shè)計(jì)，將在抗生素藥物生產(chǎn)過(guò)程中的產(chǎn)生的廢丙酮溶媒進(jìn)行分離。對(duì)于二元混合物的分離，應(yīng)采用連續(xù)精餾流程。設(shè)計(jì)中采用泡點(diǎn)進(jìn)料，將原料液通過(guò)預(yù)熱器加熱至泡點(diǎn)后送入精餾塔內(nèi)。丙酮常壓下的沸點(diǎn)是56.2℃，故可采用常壓操作，用30℃的循環(huán)水進(jìn)行冷凝。塔頂上升蒸汽采用全凝器冷凝，冷凝液在泡點(diǎn)下一部分回流至塔內(nèi)，其余部分經(jīng)產(chǎn)品冷卻器冷卻后送至儲(chǔ)槽。因所分離的物系的重組分是水，故選用直接蒸汽加熱方式，釜?dú)堃褐苯优懦?。丙?水物系分離的難易程度適中，氣液負(fù)荷適中，設(shè)計(jì)中選用500Y金屬孔板波紋填料。該設(shè)計(jì)說(shuō)明書主要內(nèi)容為：物料衡算、理論塔板數(shù)計(jì)算、精餾塔塔體工藝尺寸計(jì)算、填料層高度的計(jì)算、填料層壓降計(jì)算、液體分布器分布點(diǎn)密度計(jì)算、精餾塔接管尺寸計(jì)算。在抗生素藥物生產(chǎn)過(guò)程中的產(chǎn)生的廢丙酮溶媒中由于含有大量丙酮，不能直接排放到環(huán)境中，如果進(jìn)行丙酮回收，既可以降低生產(chǎn)費(fèi)用，又能使廢水排放達(dá)到生產(chǎn)要求。因此，將廢丙酮回收，降低排放廢水中的丙酮含量，從而產(chǎn)生社會(huì)效益和經(jīng)濟(jì)效益，是一個(gè)很重要的課題。設(shè)計(jì)主要結(jié)果：理論塔塔板數(shù)為27，塔徑為350mm，填料層分段高度為4m,填料層壓降為3.3×10－3MPa,液體分布器布液點(diǎn)數(shù)為20。關(guān)鍵字：泡點(diǎn)進(jìn)料;填料精餾塔;孔板波紋;設(shè)計(jì)計(jì)算目錄緒論······································································61.1課題背景································································61.2.1選擇填料塔的依據(jù)····················································61.2.2選擇金屬孔板波紋填料的依據(jù)··········································61.2精餾塔的選擇依據(jù)························································62.設(shè)計(jì)方案及設(shè)計(jì)工藝流程確定·················································62.1工藝設(shè)計(jì)要求····························································62.1.1進(jìn)料要求····························································62.1.2分離要求····························································72.1.3塔頂冷凝器設(shè)計(jì)要求··················································72.1.4液體分布器設(shè)計(jì)要求··················································72.1.5接管管徑設(shè)計(jì)要求····················································72.2設(shè)計(jì)工藝流程····························································73.工藝過(guò)程設(shè)計(jì)計(jì)算···························································83.1填料精餾塔的物料衡算····················································83.1.1原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的摩爾分率·································83.1.2原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的平均摩爾質(zhì)量····························83.1.3物料恒算····························································93.1.4原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的質(zhì)量流量·································93.1.5物料衡算結(jié)果一覽表··················································93.2填料精餾塔設(shè)計(jì)計(jì)算······················································93.2.1操作溫度····························································93.2.2塔徑計(jì)算···························································103.2.3液體噴淋密度及空塔氣速核算·········································153.2.4填料層高度計(jì)算·····················································153.2.5填料層壓降計(jì)算·····················································154.接管管徑計(jì)算·······························································164.1進(jìn)料管管徑的計(jì)算·······················································164.2進(jìn)氣管管徑的計(jì)算·······················································164.3出氣管管徑的計(jì)算·······················································164.4回流管管徑的計(jì)算·······················································164.5出液管管徑的計(jì)算·······················································174.6接管管徑計(jì)算結(jié)果·······················································175.附屬設(shè)備計(jì)算·······························································175.1液體分布器簡(jiǎn)要設(shè)計(jì)·····················································185.1.1液體分布器的選型···················································185.1.2孔流速計(jì)算·························································185.1.3布液計(jì)算···························································185.1.4分布點(diǎn)密度計(jì)算·····················································185.2冷凝器的計(jì)算與選型·····················································185.2.1冷凝器換熱面積計(jì)算·················································185.2.2冷凝器的選型·······················································185.2.3總傳熱系數(shù)的核算···················································185.2.4冷凝水用量計(jì)算·····················································186.設(shè)計(jì)結(jié)果一覽表·····························································197.設(shè)計(jì)小結(jié)···································································208.設(shè)計(jì)心得與體會(huì)·····························································21參考文獻(xiàn)·····································································221.緒論1課題背景廢丙酮溶媒來(lái)自于抗生素類藥物“鹽酸四環(huán)素”的生產(chǎn)過(guò)程。在抗生素類藥物生產(chǎn)過(guò)程中，需要用丙酮溶媒洗滌晶體，洗滌過(guò)濾后產(chǎn)生廢丙酮溶媒，其組成為含丙酮80%，水20%（質(zhì)量分?jǐn)?shù)）。廢液中由于含有大量丙酮，不能直接排放到環(huán)境中，如果進(jìn)行丙酮回收，既可以降低生產(chǎn)費(fèi)用，又能使廢水排放達(dá)到生產(chǎn)要求。因此，將廢丙酮回收，降低排放廢水中的丙酮含量，從而產(chǎn)生社會(huì)效益和經(jīng)濟(jì)效益，是一個(gè)很重要的課題。1.2精餾塔的選擇依據(jù)1.2.1選擇填料塔的依據(jù)塔設(shè)備按其結(jié)構(gòu)形式基本上可以分為兩類：板式塔和填料塔。板式塔為逐板接觸式汽液傳質(zhì)設(shè)備，它具有結(jié)構(gòu)簡(jiǎn)單、安裝方便、壓降低，操作彈性大，持液量小等優(yōu)點(diǎn)。同時(shí)也有投資費(fèi)用較高，填料易堵塞等缺點(diǎn)。填料塔的基本特點(diǎn)是結(jié)構(gòu)簡(jiǎn)單，壓力降小，傳質(zhì)效率高，便于采用耐腐蝕材料制造等，對(duì)于熱敏性及容易發(fā)泡的物料，更顯出其優(yōu)越性。過(guò)去，填料塔多推薦用于0.6-0.7m以下的塔徑。近年來(lái)，隨著高效新型填料和其他高性能塔內(nèi)件的開發(fā)，以及人們對(duì)填料流體力學(xué)、放大效應(yīng)及傳質(zhì)機(jī)理的深入研究，使填料塔技術(shù)得到了迅速發(fā)展。本設(shè)計(jì)目的是分離丙酮-水混合液，采用填料精餾塔。1.2.2選擇金屬孔板波紋填料的依據(jù)塔填料是填料塔中氣液接觸的基本構(gòu)件，其性能的優(yōu)劣是決定填料塔操作性能的主要因素，因此，填料塔的選擇是填料塔設(shè)計(jì)的重要環(huán)節(jié)。填料類型有很多，根據(jù)裝填方式的不同，可分為散裝填料和規(guī)整填料兩大類。規(guī)整填料根據(jù)特點(diǎn)不同，又可分為格柵填料、波紋填料、脈沖填料。這次設(shè)計(jì)使用的是金屬孔板波紋填料。2.設(shè)計(jì)方案及設(shè)計(jì)工藝流程確定2.1工藝設(shè)計(jì)要求2.1.1進(jìn)料要求進(jìn)料采用飽和液體進(jìn)料，廢丙酮溶媒的處理量為每天4.15噸（每天按24小時(shí)計(jì)）。其中原料液的組成為：丙酮：80%水：20%2.1.2分離要求產(chǎn)品中水分含量≤4%釡液中丙酮含量≤4%2.1.3塔頂冷凝器設(shè)計(jì)要求冷凝器采用冷水冷卻作為冷流體，冷卻水進(jìn)口溫度30℃，冷卻水溫升8~10℃，總傳熱系數(shù)600W/（m·℃）2.1.4液體分布器設(shè)計(jì)要求要求選用管式液體分布器.孔流速計(jì)算的系數(shù)為0.6,再分布器設(shè)計(jì)同液體分布器設(shè)計(jì)要求相同。2.1.5接管管徑設(shè)計(jì)要求管徑后要圓整為標(biāo)準(zhǔn)管。2.2設(shè)計(jì)工藝流程3.工藝過(guò)程設(shè)計(jì)計(jì)算3.1精餾塔的物料衡算3.1.1原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的摩爾分率丙酮的摩爾質(zhì)量MA=58.03kg/kmol水的摩爾質(zhì)量MB=18.02kg/kmolxxx3.1.2原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的平均摩爾質(zhì)量進(jìn)料：MF=0.554×58.03＋(1－0.553)×18.02=40.20kg/kmol精餾段：MD=0.882×58.03＋（1－0.882）×18.02=53.309kg/kmol提餾段：MW=0.0123×58.03＋(1-0.0123)×18.02=18.512kg/kmol3.1.3物料恒算廢丙酮溶媒的處理量為1200噸/年，每年按300個(gè)工作日計(jì)算。原料處理量F=1200000300總物料衡算4.15=D+W丙酮物料衡算4.15×0.554=0.882D+0.0123W聯(lián)立解得D=2.585kmol/hW=1.565kmol/h3.1.4原料液及塔頂產(chǎn)品、塔釜產(chǎn)品的質(zhì)量流量ωωω3.1.5物料衡算結(jié)果一覽表表1.物料衡算表流股摩爾流量kmol/h質(zhì)量流量kg/h丙酮質(zhì)量分?jǐn)?shù)水質(zhì)量分?jǐn)?shù)丙酮摩爾分?jǐn)?shù)水摩爾分?jǐn)?shù)F4.15166.670.800.200.5540.446D2.585139.2760.960.040.8820.118W1.56527.9730.040.960.01270.98733.2精餾塔設(shè)計(jì)計(jì)算3.2.1操作溫度根據(jù)安托尼方程：查閱手冊(cè)得到相關(guān)數(shù)據(jù)制得下圖t-x(y)圖1.時(shí)間與氣(液)相關(guān)系圖由圖1.可知tD=56.12℃,tw=89℃,tF=60℃3.2.2塔徑計(jì)算計(jì)算最小回流比及理論板數(shù)查閱相關(guān)書籍[3]可得：全塔平均相對(duì)揮發(fā)度為α精餾段平均相對(duì)揮發(fā)度為α表2.常壓下丙酮-水氣液平衡數(shù)據(jù)丙酮摩爾分?jǐn)?shù)氣相y丙酮摩爾分?jǐn)?shù)液相x丙酮摩爾分?jǐn)?shù)氣相y丙酮摩爾分?jǐn)?shù)液相x0.00000.00000.80000.19650.05000.00870.82000.35540.10000.00940.84000.50120.15000.01240.86000.70120.20000.01360.88000.76520.25000.01780.90000.82150.30000.01870.91000.85260.35000.02000.92000.87850.40000.02120.93000.90110.45000.02930.94000.91630.50000.03240.95000.93210.55000.03780.96000.94830.60000.05010.97000.96020.65000.06930.98000.97300.70000.08940.99000.98550.75000.12751.00001.00000.00000.00000.80000.1965由表2數(shù)據(jù)繪制的常壓下丙酮-水氣液平衡曲線，見下圖：圖2.丙酮-水氣液相平衡線由于泡點(diǎn)進(jìn)料可得：xq得：y最小回流比：R取R=1.5R得操作回流比：R=3.59N-NminN-R-圖3.吉利蘭圖像利用吉利蘭圖，求解全塔理論板數(shù)當(dāng)N-N其中NminN聯(lián)立（1）（2）式，解得N=26.43取N精餾段理論板數(shù)NNN解得：N'=6.78表3.填料塔塔板數(shù)匯總表理論塔板數(shù)精餾段塔板數(shù)提鎦段塔板數(shù)27720第8塊為加料板計(jì)算精餾段和提餾段的物性參數(shù)表4.丙酮和水在塔頂和塔底條件下的密度表（kg/m3)tD=56.12℃tw=89℃tF=60℃水氣相（V）0.22140.11540.5956水液相（l）976.17984.57958.47丙酮液相（l)729.1748.1695.4表5.丙酮和水在塔頂和塔底條件下的黏度數(shù)據(jù)表(mPa.s)tD=56.12℃tw=89℃tF=60℃水0.39130.48910.2841丙酮0.23670.21060.175精餾段塔徑計(jì)算精餾段塔徑按第一塊板的數(shù)據(jù)近似計(jì)算。將y1=得：y1=L1D=RV1y1=液相平均摩爾質(zhì)量為：MV1氣象平均摩爾質(zhì)量為：ML液相質(zhì)量流量為：WL=氣象質(zhì)量流量為：WV=氣相密度：ρv1液相密度：

ρL1=771.714液相粘度：則：查波紋填料的最大負(fù)荷因子圖可知：CS,max=0.078CS=0.8CS,max=0.062214214m/s.1211vlvsCu302302m.04uVDs提餾段塔徑計(jì)算提餾段塔徑按進(jìn)料板的數(shù)據(jù)近似計(jì)算，計(jì)算方法同精餾段。提餾段相關(guān)數(shù)據(jù)：WL＇=506.966kg/hWv＇=497.135kg/hΨ＇=0.044Cs,max＇=0.075Cs＇=0.060u＇=1.383m/sVs＇=0.086D=0.281m比較精餾段與提餾段計(jì)算結(jié)果，二者基本相同，圓整塔徑取D=350mm3.2.3液體噴淋密度及空塔氣速核算精餾段液體噴淋密度為：精餾段空塔氣速為：提餾段液體噴淋密度：提餾段空塔氣速為：3.2.4填料層高度計(jì)算填料層高度計(jì)算采用理論板當(dāng)量高度法。對(duì)500Y金屬孔板波紋填料，查金屬孔板波紋填料的性能參數(shù)表可得，每米填料理論板數(shù)為4-4.5塊，取nt=4。則：HETP=1/nt=0.25m由Z=NT×HETP，精餾段填料層高度為：Z精=7×0.25=1，75mZ‘精=1.75×1.25=2.188m提餾段填料層高度為：Z提=20×0.25=5mZ’提=5×1.25=6.25m設(shè)計(jì)取精餾段填料層高度為2.188m，提餾段填料層高度為6.25m根據(jù)式（5-54），取填料層的分段高度為：h=16×HETP=16×0.25=4m3.2.5填料層壓降計(jì)算對(duì)500Y金屬孔板波紋填料，查金屬孔板波紋填料的性能參數(shù)表可得每米填料層壓降為精餾段填料層壓降為：提餾段填料層壓降為：填料層總壓降為：4.接管管徑計(jì)算4.1進(jìn)料管管徑的計(jì)算取液體流速為0.8m/s圓整后直徑取20mm4.2進(jìn)氣管管徑的計(jì)算取氣體流速為12m/s圓整后直徑取150mm4.3出氣管管徑的計(jì)算取氣體流速為12m/s圓整后直徑取150mm4.4回流管管徑的計(jì)算取液體流速為0.8m/s圓整后直徑取25mm4.5出液管管徑的計(jì)算取液體流速為0.8m/s圓整后直徑取20mm4.6接管管徑計(jì)算結(jié)果表6.接管管徑計(jì)算結(jié)果摩爾流量(kmol/h)平均摩爾質(zhì)量(g/mol)密度(kg/m3)V(m3/h)u(m/s)d(m)圓整后(mm)進(jìn)料管26.8520.7881916.21.692×10-40.80.016420出氣管21.6757.82362.130.1710120.135150進(jìn)氣管21.6718.49670.60.1856120.140150回流管16.8057.6994748.63.597×10-40.80.023925出液管26.8518.10419561.412×10-40.80.0150205.附屬設(shè)備計(jì)算5.1液體分布器簡(jiǎn)要設(shè)計(jì)5.1.1液體分布器的選型該精餾塔塔徑較小，故選用管式液體分布器。液體分布均勻使整個(gè)填料面積得到充分利用，壁流、溝流大為減少。此塔操作彈性較低，屬于簡(jiǎn)單操作，結(jié)合經(jīng)濟(jì)效益選此分布器。5.1.2孔流速計(jì)算其中則：5.1.3布液計(jì)算取設(shè)計(jì)取d0=2.3mm液體再分布器與液體分布器相同，設(shè)計(jì)原則也相同。5.1.4分布點(diǎn)密度計(jì)算該精餾塔塔徑較小，且500Y孔板波紋填料的比表面積較大，故應(yīng)選取較大的分布點(diǎn)密度，設(shè)計(jì)中取分布點(diǎn)密度為布液點(diǎn)數(shù)為：按分布幾何均勻與流量均勻的原則，進(jìn)行布點(diǎn)設(shè)計(jì)。設(shè)計(jì)結(jié)果，主管直徑為，支管直徑為，采用5根支管，支管中心距為65mm，采用正方形排列，實(shí)際布點(diǎn)數(shù)為n=215.2冷凝器的計(jì)算與選型5.2.1冷凝器換熱面積計(jì)算

5.2.2冷凝器的選型查表得S=15m2選型為G400Ⅱ-16-155.2.3總傳熱系數(shù)的核算5.2.4冷凝水用量計(jì)算6.設(shè)計(jì)結(jié)果一覽表表7.填料精餾塔設(shè)計(jì)結(jié)果一覽表名稱工藝參數(shù)水丙酮操作壓力/kPa101101操作溫度/℃8956.12進(jìn)料管管徑/mm15020出口管徑/mm15020填料層壓降/Pa3300提餾段填料層高度/mm6.25精餾段填料層高度/mm2.188塔徑/mm350分布點(diǎn)數(shù)217.設(shè)計(jì)小結(jié)本次課程設(shè)計(jì)為“12000噸丙酮-水連續(xù)精餾填料塔設(shè)計(jì)”。設(shè)計(jì)主要內(nèi)容有基礎(chǔ)性物理數(shù)據(jù)、物料衡算、理論塔板數(shù)計(jì)算、精餾塔塔體工藝尺寸計(jì)算、填料層高度的計(jì)算、填料層壓降計(jì)算、液體分布器分布點(diǎn)密度計(jì)算、精餾塔接管尺寸計(jì)算。對(duì)于二元混合物的分離，應(yīng)采用連續(xù)精餾流程。設(shè)計(jì)中采用泡點(diǎn)進(jìn)料，將原料液通過(guò)預(yù)熱器加熱至泡點(diǎn)后送入精餾塔內(nèi)。丙酮常壓下的沸點(diǎn)是56.2℃，故可采用常壓操作，用30℃的循環(huán)水進(jìn)行冷凝。塔頂上升蒸汽采用全凝器冷凝，冷凝液在泡點(diǎn)下一部分回流至塔內(nèi)，其余部分經(jīng)產(chǎn)品冷卻器冷卻后送至儲(chǔ)槽。因所分離的物系的重組分是水，故選用直接蒸汽加熱方式，釜?dú)堃褐苯优懦?。丙?水物系分離的難易程度適中，氣液負(fù)荷適中，設(shè)計(jì)中選用500Y金屬孔板波紋填料。通過(guò)設(shè)計(jì)計(jì)算可知，水的進(jìn)出口徑為150mm，丙酮進(jìn)出口徑為20mm，提餾段填料層高度為6.25mm，精餾段填料高度為2.188mm，液體分布器分布點(diǎn)數(shù)為21，塔徑為350mm，填料層壓降為33000Pa。8.設(shè)計(jì)心得與體會(huì)這次的課程設(shè)計(jì)要求我們每人完成一個(gè)填料精餾塔的設(shè)計(jì)，從最基本的要求到物料衡算、塔的設(shè)計(jì)過(guò)程計(jì)算，最后還有工藝流程圖和設(shè)計(jì)條件圖。其中很多東西是我們?cè)凇痘ぴ怼愤@門課中學(xué)過(guò)的，在這次設(shè)計(jì)中我們?nèi)跁?huì)貫通了這些知識(shí)，了解了它們?cè)谒脑O(shè)計(jì)中起了什么作用。我體驗(yàn)到了獲得新知識(shí)的喜悅。我們小組還為這次設(shè)計(jì)進(jìn)行了幾次討論，共同研究怎樣設(shè)計(jì)計(jì)算，雖然有的意見不同，但大家都按自己的想法實(shí)踐了出來(lái)，得到了收獲。經(jīng)過(guò)幾周的努力，課程設(shè)計(jì)終于完成了。真心覺得這個(gè)課程設(shè)計(jì)來(lái)之不易。作為一名化工專業(yè)大三的學(xué)生，我覺得能做這樣的課程設(shè)計(jì)是十分有意義的。在已度過(guò)的三年大學(xué)生活里我們大多數(shù)接觸的是專業(yè)基礎(chǔ)課。我們?cè)谡n堂上掌握的僅僅是專業(yè)基礎(chǔ)課的理論面，如何去面對(duì)現(xiàn)實(shí)中的各種化工設(shè)備的機(jī)械設(shè)計(jì)？如何把我們所學(xué)到的專業(yè)基礎(chǔ)理論知識(shí)用到實(shí)踐中去呢？我想做類似的大作業(yè)就為我們提供了良好的實(shí)踐平臺(tái)。在做本次課程設(shè)計(jì)的過(guò)程中，我感觸最深的當(dāng)屬查閱了很多次設(shè)計(jì)書和指導(dǎo)書。為了讓自己的設(shè)計(jì)更加完善，更加符合工程標(biāo)準(zhǔn)，一次次翻閱機(jī)械設(shè)計(jì)書是十分必要的，同時(shí)也是必不可少的。我們做的是課程設(shè)計(jì)，而不是藝術(shù)家的設(shè)計(jì)。藝術(shù)家可以拋開實(shí)際，盡情在幻想的世界里翱翔，我們是工程師，一切都要有據(jù)可依.有理可尋，不切實(shí)際的構(gòu)想永遠(yuǎn)只能是構(gòu)想，永遠(yuǎn)無(wú)法升級(jí)為設(shè)計(jì)。在這個(gè)過(guò)程中，我學(xué)到了很多知識(shí)如作圖、查閱文獻(xiàn)資料、word排版，這對(duì)我們的以后的發(fā)展更為有益，比如為即將面臨的畢業(yè)論文、考研或畢業(yè)后的工作打下堅(jiān)實(shí)的基礎(chǔ)。

對(duì)于那些在設(shè)計(jì)過(guò)程中幫助過(guò)我的所有老師和同學(xué)，我再一次的表示深深的感謝！參考文獻(xiàn)[1]賈紹義、柴誠(chéng)敬﹒化工原理課程設(shè)計(jì).[M].天津：天津大學(xué)出版社.2002年[2]賈紹義、柴誠(chéng)敬﹒化工單元操作課程設(shè)計(jì)﹒[M].天津：天津大學(xué)出版社，2011年[3]馬沛生、夏清.化學(xué)化工物性數(shù)據(jù)手冊(cè).[M].北京：化學(xué)工業(yè)出版社.2013年.基于C8051F單片機(jī)直流電動(dòng)機(jī)反饋控制系統(tǒng)的設(shè)計(jì)與研究基于單片機(jī)的嵌入式Web服務(wù)器的研究MOTOROLA單片機(jī)MC68HC（8）05PV8/A內(nèi)嵌EEPROM的工藝和制程方法及對(duì)良率的影響研究基于模糊控制的電阻釬焊單片機(jī)溫度控制系統(tǒng)的研制基于MCS-51系列單片機(jī)的通用控制模塊的研究基于單片機(jī)實(shí)現(xiàn)的供暖系統(tǒng)最佳啟停自校正（STR）調(diào)節(jié)器單片機(jī)控制的二級(jí)倒立擺系統(tǒng)的研究基于增強(qiáng)型51系列單片機(jī)的TCP/IP協(xié)議棧的實(shí)現(xiàn)基于單片機(jī)的蓄電池自動(dòng)監(jiān)測(cè)系統(tǒng)基于32位嵌入式單片機(jī)系統(tǒng)的圖像采集與處理技術(shù)的研究基于單片機(jī)的作物營(yíng)養(yǎng)診斷專家系統(tǒng)的研究基于單片機(jī)的交流伺服電機(jī)運(yùn)動(dòng)控制系統(tǒng)研究與開發(fā)基于單片機(jī)的泵管內(nèi)壁硬度測(cè)試儀的研制基于單片機(jī)的自動(dòng)找平控制系統(tǒng)研究基于C8051F040單片機(jī)的嵌入式系統(tǒng)開發(fā)基于單片機(jī)的液壓動(dòng)力系統(tǒng)狀態(tài)監(jiān)測(cè)儀開發(fā)模糊Smith智能控制方法的研究及其單片機(jī)實(shí)現(xiàn)一種基于單片機(jī)的軸快流CO〈,2〉激光器的手持控制面板的研制基于雙單片機(jī)沖床數(shù)控系統(tǒng)的研究基于CYGNAL單片機(jī)的在線間歇式濁度儀的研制基于單片機(jī)的噴油泵試驗(yàn)臺(tái)控制器的研制基于單片機(jī)的軟起動(dòng)器的研究和設(shè)計(jì)基于單片機(jī)控制的高速快走絲電火花線切割機(jī)床短循環(huán)走絲方式研究基于單片機(jī)的機(jī)電產(chǎn)品控制系統(tǒng)開發(fā)基于PIC單片機(jī)的智能手機(jī)充電器基于單片機(jī)的實(shí)時(shí)內(nèi)核設(shè)計(jì)及其應(yīng)用研究基于單片機(jī)的遠(yuǎn)程抄表系統(tǒng)的設(shè)計(jì)與研究基于單片機(jī)的煙氣二氧化硫濃度檢測(cè)儀的研制基于微型光譜儀的單片機(jī)系統(tǒng)單片機(jī)系統(tǒng)軟件構(gòu)件開發(fā)的技術(shù)研究基于單片機(jī)的液體點(diǎn)滴速度自動(dòng)檢測(cè)儀的研制基于單片機(jī)系統(tǒng)的多功能溫度測(cè)量?jī)x的研制基于PIC單片機(jī)的電能采集終端的設(shè)計(jì)和應(yīng)用基于單片機(jī)的光纖光柵解調(diào)儀的研制氣壓式線性摩擦焊機(jī)單片機(jī)控制系統(tǒng)的研制基于單片機(jī)的數(shù)字磁通門傳感器基于單片機(jī)的旋轉(zhuǎn)變壓器-數(shù)字轉(zhuǎn)換器的研究基于單片機(jī)的光纖Bragg光柵解調(diào)系統(tǒng)的研究單片機(jī)控制的便攜式多功能乳腺治療儀的研制基于C8051F020單片機(jī)的多生理信號(hào)檢測(cè)儀基于單片機(jī)的電機(jī)運(yùn)動(dòng)控制系統(tǒng)設(shè)計(jì)Pico專用單片機(jī)核的可測(cè)性設(shè)計(jì)研究基于MCS-51單片機(jī)的熱量計(jì)基于雙單片機(jī)的智能遙測(cè)微型氣象站MCS-51單片機(jī)構(gòu)建機(jī)器人的實(shí)踐研究基于單片機(jī)的輪軌力檢測(cè)基于單片機(jī)的GPS定位儀的研究與實(shí)現(xiàn)基于單片機(jī)的電液伺服控制系統(tǒng)用于單片機(jī)系統(tǒng)的MMC卡文件系統(tǒng)研制基于單片機(jī)的時(shí)控和計(jì)數(shù)系統(tǒng)性能優(yōu)化的研究基于單片機(jī)和CPLD的粗光柵位移測(cè)量系統(tǒng)研究單片機(jī)控制的后備式方波UPS提升高職學(xué)生單片機(jī)應(yīng)用能力的探究基于單片機(jī)控制的自動(dòng)低頻減載裝置研究基于單片機(jī)控制的水下焊接電源的研究基于單片機(jī)的多通道數(shù)據(jù)采集系統(tǒng)基于uPSD3234單片機(jī)的氚表面污染測(cè)量?jī)x的研制基于單片機(jī)的紅外測(cè)油儀的研究96系列單片機(jī)仿真器研究與設(shè)計(jì)基于單片機(jī)的單晶金剛石刀具刃磨設(shè)備的數(shù)控改造基于單片機(jī)的溫度智能控制系統(tǒng)的設(shè)計(jì)與實(shí)現(xiàn)基于MSP430單片機(jī)的電梯門機(jī)控制器的研制基于單片機(jī)的氣體測(cè)漏儀的研究基于三菱M16C/6N系列單片機(jī)的CAN/USB協(xié)議轉(zhuǎn)換器基于單片機(jī)和DSP的變壓器油色譜在線監(jiān)測(cè)技術(shù)研究基于單片機(jī)的膛壁溫度報(bào)警系統(tǒng)設(shè)計(jì)基于AVR單片機(jī)的低壓無(wú)功補(bǔ)償控制器的設(shè)計(jì)基于單片機(jī)船舶電力推進(jìn)電機(jī)監(jiān)測(cè)系統(tǒng)基于單片機(jī)網(wǎng)絡(luò)的振動(dòng)信號(hào)的采集系統(tǒng)基于單片機(jī)的大容量數(shù)據(jù)存儲(chǔ)技術(shù)的應(yīng)用研究基于單片機(jī)的疊圖機(jī)研究與教學(xué)方法實(shí)踐基于