11萬噸每年甲基叔丁基醚工藝計算

11萬噸/MTBE裝置設計第五章工藝計算設計物料平衡異丁烯經(jīng)過醚化反響和催化精餾最終轉化率為96％序號物料名稱Wt％kg/h序號物料名稱Wt％kg/ht/dt/a進料4合計10045342.71088.23971931C89.2240850980.435784642甲醇10.784934118.4243223.3合計10045784出料1098.4400923..31MTBE27..312379297.1108441..52C72..732963.7791.1288751..5主要原料性質以及外購的工業(yè)甲醇為原料，組成如下：5-2C4原料性質組分wt％異丁烷36.23異丁烯20.11正丁烯9.04正丁烷5.52反丁烯-214.44順丁烯-214.66合計1000.1％主反響器的物熱平衡計算醚化反響器醚化反響器為固定床水冷卻列管反響器,管內裝催化劑，進料組成如表5-3所列。操作條件： 入口溫度:60℃出口溫度：65℃操作壓力：0.7MPa甲醇與異丁烯摩爾比：1.05異丁烯轉化率：90％冷卻水進口溫度：25℃冷卻水出口溫度：30℃溫升：5℃物料衡算：組分流組分流Kg/h量Kmol/h組 成％〔質量〕%〔摩爾〕C36.2320.119.045.5214.4414.66100.00035.540.05920.419.02314.614.9100.000CHOH3HO2共計49344.9345789154.030.27873.299.900.1100.00099.830.17100.0004異丁烷14800255.2異丁烯8215146.7正丁烯369365.9正丁烷225538.9反丁烯-25899105.3順丁烯-25988106.9共計40850718.9原料甲醇5-4醚化反響器出料流量和組成kg/hkmol/h％〔質量〕%〔摩爾〕14800255.232.0534.42821.514.71.781.98369365.97.998.89225538.94.885.255899105.312.7714.205988106.912.9714.42704.022.01.072.0811595131.826.4418.7219.980.270.0430.03645789741.2100.000100.000組分組分流量組成異丁烷異丁烯正丁烯正丁烷反丁烯-2順丁烯-2CHOH3MTBE總計146.7×〔1－0.9〕＝14.67〔kmol/h〕=821.5(kg/h)0.27kmol/h。1mol0.27×1＝0.27〔kmol/h〕=19.98(kg/h)MTBE 146.7-14.67-0.27=131.8(kmol/h)=11595(kg/h)CHOH 154.0-0.27-131.8＝22.0〔kmol/h〕=704.0(kg/h)3熱量衡算H=FCt5－5i ip,ii組分進組分進料60℃出料65℃kg/hkJ/(kg·K)kJ/hkg/hkJ/(kg·K)kJ/h148002.67913203183148002.6951348146882152.4616732299.3821.52.517698887.836932.461302646136932.4863103109.722551.7501314101.322552.2301699683.758992.6085123069.158992.6375257814.159882.7135409732.859882.8455758120.749342.7354493665.27042.805667455.401.7550115951.8357191566.903.447019.983.48623541.84.934.178685904.18304578939309370.74578937881648.1FCHFCFCHFCHj p，j j j p，j j異丁烷異丁烯正丁烯正丁烷CHOH3MTBEHO2總計異丁烯醚化反響反響熱用下式計算:H 38602.18+8.5918T+0.11166T2-0.0003918T3r式中 Hr

kJ/kmolT——反響溫度。K.60℃算反響熱H 38602.18+8.5918333+0.111663332-0.0003918333337439.3(kJ/kmol)r所以單位反響熱為Q (HR

)N xA0

37439.3146.70.90.27

/h)式中 N——異丁烯進料流量，kmol/h；A0xA熱量平衡式H-H=Q－Q2 1 c rKj/h，3－3；Qc——反響器冷卻水取熱量，kJ/h。Q39309370.737881648.149330026360724.6(kJ/h)cctr冷卻水流量 ctr式中 ?——水的比熱，4.180kJ/〔kg·K；rt——水溫升，℃6360724.6W 4.1805

304340.9kg/h304.3t/h催化精餾塔操作條件：進料溫度:65℃操作壓力：1.079MPa塔頂氣溫度操作條件：進料溫度:65℃操作壓力：1.079MPa塔頂氣溫度70℃塔釜溫度75℃冷卻水進口溫度：25℃冷卻水出口溫度：30℃溫升：5℃分別要求：重關鍵組分甲醇回收率為95％MTBE99.7％MTBE99.8％異丁烯最終轉化率：96％〔A〕5-4。依據(jù)分別要求，并假底不消滅。出料各物流的流量和組成計算如下：甲醇塔頂流量n=〔22-146.7×0.06〕×0.95＝12.5〔kmol/h〕1甲醇塔釜流量n＝13.2－12.5=0.7(kmol/h)2塔頂總質量流量為14800＋3693＋2255＋5899＋5988＋328.6＋401.2＋24.7＝33389.5〔kg/h〕MTBE12369.6×(1-99.8％)=24.7(kg/h)MTBE12369.6-24.7＝12344.9〔kg/h〕物料衡算結果如表組分異丁烷異丁烯正丁烯正丁烷反丁烯-2組分異丁烷異丁烯正丁烯正丁烷反丁烯-2順丁烯-2CHOH3MTBE總計CHOH3MTBE總計出塔物料總計質量流量kg/h組成％〔質量〕塔頂物料摩爾流量kmol/h組成％〔摩爾〕1480044.33255.243.19328.60.985.870.99369311.0665.911.1522556.7538.96.58589917.67105.317.82598817.93106.918.09401.21.2012.52.1124.70.0740.280.04733389.5100.00590.85100.0021.1塔釜物料0.170.660.4712344.999.67140.5699.3419.980.160.270.1912386.0100.000141.49100.0045789(B)熱量衡算催化精餾塔熱量衡算取各組分0℃純物質液態(tài)作為焓基準態(tài)。Hi=FiCp,iti5-7進料65℃進料65℃FCH異丁烷異丁烯正丁烯正丁烷反丁烯-2順丁烯-2CHOH3MTBE總計異丁烷異丁烯正丁烯正丁烷反丁烯-2順丁烯-2CHOH3MTBE總計jP，jF,jkg/hkJ/〔kg·K〕kJ/h148002.69513481468821.52.517698887.836932.4863103109.722552.2301699683.758992.6375257814.159882.8455758120.7704.02.805667455.4115951.8357191566.919.983.48623541.84578937881648塔頂蒸汽70℃塔底產(chǎn)品75℃FF CH FFC HjP，jF,jjP，jF,jkg/hkJ/〔kg·K〕kJ/hkg/hkJ/〔kg·K〕kJ/h148002.79514188538328.62.617294961.536932.5863275683.622552.3301802173.558992.7375537928.159882.9456048688.4401.22.905399761.721.12.98521330.824.71.93516393.512344.91.9758312808.803.686019.983.58624238.333389.531564128.312386.08358378用標準反響熱〔產(chǎn)物與反響物標準生成熱之差〕及產(chǎn)物，反響物的比熱差ΔCp＝Δα＋ΔβT＋ΔγT2對溫度進展積分，可得異丁烯醚化反響再不同溫度下的反響熱公式。異丁烯醚化反響反響熱用下式計算:Hr式中 Hr

38602.18+8.5918T+0.11166T2-0.0003918T3——反響熱，kJ/kmol反響溫度。K.70℃算反響熱H 38602.18+8.5918343+0.111663432-0.0003918343338329(kJ/kmol)r所以單位反響熱為Q (H)N x 38329146.70.06337371.9(kJ/h)R r A0 AN—異丁烯進料流量，kmol/h；A0xA熱量平衡式H-H=Q+Q1 2 c rKj/hQc—塔釜再沸器供給熱量，kJ/hQ 39922