年產10萬噸苯甲醇工藝設計摘要：苯甲醇作為合成香料和醫藥的重要中間體，在感光、染整、化妝品、涂料及油墨等眾多領域有著十分廣泛的應用。本設計首先進行初步工藝設定，查找根據三大平衡算出各路線上的參數，然后利用AspenPlus化工流程模擬軟件對全流程進行模擬，其次通過優化流程中設備的操作條件，得到最優的操作條件，在熱量衡算、物料衡算的基礎上，對精餾塔設備進行選型。最后對生產進行技術經濟核算，并且繪制了制備苯甲醇工藝流程圖。本設計采用的是氯化芐連續水解法制備苯甲醇，此法具有收率高、無環境污染等優點，國內尚處于起步階段，研究連續水解法生產工藝具有重要的現實意義。關鍵詞：工藝設計；苯甲醇；AspenPlus模擬目錄引言 [17]。因此，接下來我們使用AspenPlus對分離單元中各精餾塔的上述變量進行靈敏度分析，旨在達到控制指標的前提下，獲得最佳的操作條件。4.1氯化芐回收塔操作參數的設計對氯化芐回收塔T1而言，其輕關鍵組分XB為氯化芐，重關鍵組分XD為苯甲醇。該塔條件設計的目標為：塔頂餾出液中苯甲醇回收率控制在0.0001以下，塔釜液中的氯化芐質量含量控制在10mg/L以下。下面逐個考察單個條件的影響：4.1.1操作壓力的影響取理論塔板數為29塊，餾出比為0.4701，回流比為0.9，進料塔板為第15塊，改變操作壓力，經AspenPlus模擬后，得到表4-1所示：表4-1操作壓力對氯化芐回收塔對的影響操作壓力（Bar）OHCL冷凝器冷負荷（KJ/hr）再沸器熱負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.15.3439460.000117-2795.93654.50770.41595142.09480.1025.4186990.000124-2794.633659.35370.89307142.51830.1045.4977750.000131-2793.313664.09971.36556142.9360.1065.5803520.000138-27923668.78471.82994143.34780.1085.6665640.000146-2790.733673.40972.28649143.7540.115.7565440.000154-2789.473677.97672.7355144.15480.1125.8517860.000162-2788.243682.48773.17724144.55020.1145.949760.000171-2787.043686.94373.61195144.94040.1166.0518650.00018-2785.853691.34674.03988145.32570.1186.1582610.000189-2784.683695.69774.46125145.7060.126.269090.000199-2783.543699.99874.87629146.08150.1226.3844960.000209-2782.413704.2575.2852146.45250.1246.504630.00022-2781.33708.45375.68817146.81890.1266.6296440.000231-2780.213712.61176.08538147.18090.1286.7596990.000242-2779.133716.72376.47703147.53870.136.8949520.000254-2778.073720.7976.86326147.89220.1327.0355750.000267-2777.033724.81577.24426148.24170.1347.1823270.00028-2776.013728.79877.62016148.58720.1367.3344270.000293-27753732.73977.99111148.92890.1387.4924650.000307-27743736.64178.35727149.26670.147.6565870.000321-2773.023740.50378.71875149.60090.1427.8270440.000336-2772.063744.32879.07569149.93140.1448.0040490.000352-2771.113748.11579.42822150.25840.1468.1880230.000368-2770.173751.86579.77644150.5820.1488.3786840.000385-2769.243755.58180.12048150.90220.158.5764610.000402-2768.333759.26180.46044151.219影響模擬見圖4-1所示：圖4-1操作壓力對氯化芐回收塔對的影響由圖4-1可知，塔頂苯甲醇回收率、塔釜氯化芐含量、冷凝器冷負荷、再沸器熱負荷均隨著操作壓力的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選擇操作壓力P=0.1Bar=10KPa。4.1.2.回流比的影響取理論塔板數為29塊，塔頂餾出比為0.4701，操作壓力為10KPa,進料塔板為第15塊，改變回流比，經AspenPlus模擬后，得到表4-2所示：表4-2回流比對氯化芐回收塔對的影響回流比OHKG/HRCL冷凝器冷負荷（KJ/hr）再沸器冷負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.85.9893910.000174-2709.223567.77970.41414142.09240.825.7231910.000151-2739.283597.85670.41435142.09340.845.5053970.000132-2769.363627.93870.41469142.09420.857675.3400910.000117-2795.933654.51970.41483142.09490.865.3285780.000116-2799.443658.02470.41488142.09490.885.1825270.000103-2829.523688.11470.41495142.09550.95.0601629.25E-05-2859.613718.20370.41512142.0959影響模擬圖見圖4-2所示：圖4-2回流比對氯化芐回收塔對的影響經過初步分析，把氯化芐回收塔回流比設定0.84~0.86在之間，由圖4-2分析可知，塔頂苯甲醇回收率和塔釜氯化芐含量隨著回流比的增加而下降；冷凝器冷負荷、再沸器熱負荷隨著回流比的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選回流比R=0.9。4.1.3.塔板數的影響取進料塔板為第15塊，塔頂餾出比為0.4701，操作壓力為10KPa，回流比為0.9，改變塔板數，經AspenPlus模擬后，得到表4-3所示：表4-3塔板數對氯化芐回收塔對的影響塔板數OHKG/HRCL冷凝器冷負荷（KJ/hr）再沸器冷負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）102591.1570.219024-3103.63831.75467.10322129.7563112591.0910.219019-3103.463831.55767.09739129.7568122591.370.219042-3103.183831.27467.09703129.7559132591.6210.219062-3102.953831.03667.09685129.7551142591.8410.21908-3102.763830.83667.0967129.7544152592.0310.219096-3102.593830.66367.09658129.7537161676.2480.14428-2999.593790.25968.30942136.0755171105.1930.095721-2933.123746.89769.09068138.102118727.19640.063166-2887.733716.61969.57425139.438119471.41040.040958-2856.183695.50969.88469140.363220297.9910.025818-2834.283680.71770.08731141.000521182.4360.015693-2819.453670.65270.21873141.429822108.12770.009166-2809.773664.06770.30173141.70782362.583710.00516-2803.773659.96170.352141.8792436.047040.002823-2800.233657.52870.38117141.9792521.213260.001516-2798.223656.1470.39742142.03492613.155520.000806-2797.13655.36570.40623142.0654278.8471660.000426-2796.493654.92770.41095142.0816286.5574860.000224-2796.143654.67470.41345142.0903295.3478910.000118-2795.943654.52170.41477142.0948影響模擬圖見圖4-3所示：圖4-3塔板數對氯化芐回收塔對的影響經過初步分析，把進料板位置設定在第10~29塊板之間，由圖4-3分析可知，塔頂苯甲醇回收率和塔釜氯化芐含量隨著塔板數的增加而下降，當塔板數超過塊29塊后，曲線基本持平，變化很小；冷凝器冷負荷、再沸器熱負荷也同樣如此，綜合考慮設備費用、操作費用及產品純度，我們選塔板數NT=29。4.1.4.進料板影響取塔板數為第29塊,塔頂餾出比為0.4701，操作壓力為10KPa，回流比為0.9,改變進料板位置，經AspenPlus模擬后，得到表4-4所示：表4-4進料板對氯化芐回收塔對的影響進料板位置OHKG/HRCL冷凝器冷負荷（KJ/hr）再沸器熱負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）21260.5250.109307-2951.763759.21468.8868137.5513657.36790.057143-2878.473710.28269.66162139.68654365.9360.03176-2842.283685.95770.00939140.74895205.7520.017739-2821.843672.12870.19626141.34536113.45140.009634-2810.063664.14270.29611141.6886760.613140.004986-2803.193659.46870.35432141.8869831.286890.002404-2799.353656.84970.3865141.9968915.726220.001033-2797.33655.45570.40346142.0556107.8205130.000336-2796.263654.74570.41208142.0855114.6372845.52E-05-2795.843654.45770.41554142.0975124.377223.23E-05-2795.813654.43270.41584142.0985134.4804784.14E-05-2795.823654.44370.41572142.0981144.7631186.63E-05-2795.863654.46970.41542142.0971155.3450250.000118-2795.943654.52170.4148142.0949166.4923010.000219-2796.093654.62470.41356142.0905178.7245220.000415-2796.383654.82570.41116142.08211813.028760.000795-2796.943655.20870.4065142.06581921.183850.001514-2798.013655.93970.39763142.0352036.301040.002845-28003657.29270.38118141.97792163.362250.005228-2803.533659.70470.35157141.87622109.6550.0093-2809.563663.80170.30055141.70223184.81970.015902-2819.263670.39970.21696141.420324301.12490.026093-2834.113680.45370.08449140.98825475.03240.041273-2855.973695.19169.88124140.349526730.92890.063489-2887.393716.22469.57068139.4237271108.5380.096007-2932.613746.31469.08822138.09281678.6920.144487-2998.773789.41968.31241136.0675292593.4680.219214-3101.43829.46567.09882129.7488影響模擬圖見圖4-4所示：圖4-4進料板對氯化芐回收塔對的影響經過初步分析，把進料板位置設定在第10~18塊板之間，由圖4-4分析可知，塔頂苯甲醇回收率和塔釜氯化芐含量開始隨著進料板的增加而下降，但當進料板為第15塊時，塔頂苯甲醇回收率和塔釜氯化芐含量開始隨著進料板的增加而增加；冷凝器冷負荷、再沸器熱負荷也同樣如此，綜合考慮設備費用、操作費用及產品純度，我們選進料板位置NF=15。4.1.5.采出影響取理論塔板數為29塊，取進料塔板為第15塊，塔頂餾出比為0.4701，操作壓力為10KPa，回流比為0.9，改變采出，經AspenPlus模擬后，得到表4-5所示：表4-5采出對氯化芐回收塔對的影響塔頂餾出比OHKG/HRCL冷凝器冷負荷（KJ/hr）再沸器熱負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.41.0978130.131862-2377.653240.40567.31335136.61920.421.2860240.097863-2497.543358.07368.25755137.98930.441.4895050.061092-2616.893476.04469.15427139.50550.461.710460.021197-2735.833594.46170.00482141.19110.4700664.3788443.24E-05-2795.813654.43470.41583142.09850.48248.86118.87E-06-2886.293734.91370.54696142.10820.5741.56093.99E-06-3065.793894.25670.78691142.1269影響模擬圖見圖4-5所示：圖4-5采出對氯化芐回收塔對的影響經過初步分析，把塔頂餾出比設定在0.4700~0.4800之間，由圖4-5可知，塔頂苯甲醇回收率開始隨著塔頂餾出比的增加變化不大，當塔頂餾出比超過0.4701時，塔頂苯甲醇回收率隨著塔頂餾出比的增加直線上升；塔釜氯化芐含量開始隨著塔頂餾出比的增加直線下降，當塔頂餾出比超過0.4701時，塔釜氯化芐含量隨著塔頂餾出比的增加變化不大；冷凝器冷負荷、再沸器熱負荷隨著塔頂餾出比的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選塔頂餾出比D/F=0.4701。4.2苯甲醇成品塔操作參數的設計對苯甲醇成品塔B10而言，其輕關鍵組分XB為苯甲醇，重關鍵組分XD為二芐醚。該塔條件設計的目標為：塔頂餾出液中苯甲醇回收率達到0.99,塔頂餾出液中苯甲醇含量大于0.99999。下面逐個考察單個條件的影響：4.2.1.操作壓力的影響取理論塔板數為31塊，餾出比為0.9782，回流比為0.2，進料塔板為第17塊，改變操作壓力，經AspenPlus模擬后，得到表4-6所示：表4-6操作壓力對苯甲醇成品塔的影響操作壓力（Bar）OHKG/HROH冷凝器冷負荷（KJ/hr）再沸器熱負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.0312768.270.999786-2369.272108.004109.0768167.80540.03212768.280.999788-2364.432114.461110.479168.77820.03412768.290.99979-2359.852120.605111.8056169.72460.03612768.310.999791-2355.52126.469113.0647170.6460.03812768.320.999793-2351.362132.08114.2634171.5440.0412768.330.999794-2347.42137.459115.4074172.41980.04212768.330.999795-2343.622142.629116.502173.27470.04412768.340.999796-2339.992147.605117.5513174.10970.04612768.350.999797-2336.492152.404118.5593174.92580.04812768.360.999799-2333.132157.038119.5293175.72410.0512768.360.999799-2329.892161.52120.4642176.5053影響模擬圖見圖4-6所示：圖4-6操作壓力對苯甲醇成品塔的影響由圖4-6可知，塔頂苯甲醇回收率、塔頂苯甲醇含量受操作壓力的影響不大；冷凝器冷負荷、再沸器熱負荷均隨著操作壓力的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選擇操作壓力P=0.03Bar=3KPa。4.2.2.回流比的影響取理論塔板數為31塊，餾出比為0.9782，回流比為0.2，進料塔板為第17塊，改變操作壓力，經AspenPlus模擬后得到表4-7所示：表4-7回流比對苯甲醇成品塔的影響回流比OHKG/HRWOH冷凝器冷負荷（KJ/hr）再沸器冷負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.112745.050.996457-2147.031883.269109.1105159.00970.1212750.210.997197-2185.861922.577109.1031160.6940.1412755.40.99794-2224.681961.91109.0956162.53250.1612760.360.998651-2263.492001.258109.0883164.44910.1812764.470.999241-2302.342040.589109.0823166.1390.212767.170.999627-2341.242079.836109.0785167.29790.21439212768.270.999786-2369.272108.002109.0768167.81160.2212768.560.999827-2380.22118.974109.0764167.93110.2412769.180.999917-2419.192158.046109.0755168.22230.2612769.460.999956-2458.192197.089109.0751168.34920.2812769.570.999973-2497.212236.115109.0749168.41080.312769.630.999981-2536.222275.14109.0748168.4321影響模擬圖見圖4-7所示：圖4-7回流比對苯甲醇成品塔的影響經過初步分析，把苯甲醇成品塔回流比設定在0.1~0.3之間，由圖4-7分析可知，塔頂苯甲醇回收率和塔頂苯甲醇含量隨著回流比的增加而增加，當回流比超過0.2144時，曲線基本持平，變化很小；冷凝器冷負荷、再沸器熱負荷隨著回流比的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選回流比R=0.2。4.2.3.塔板數的影響取理論塔板數為31塊，餾出比為0.9782，操作壓力為3KPa，回流比為0.2，改變塔板數，經AspenPlus模擬后得到表4-8所示：表4-8塔板數對苯甲醇成品塔的影響塔板數OHKG/HROH冷凝器冷負荷（KJ/hr）冷凝器冷負荷（KJ/hr）塔釜溫度（℃）塔釜溫度（℃）1612577.470.972734-2381.922111.779109.355131.23041712676.080.986631-2377.162109.404109.2108143.43781812739.820.995709-2373.872109.667109.118157.3961912762.110.998902-2372.452110.418109.0857165910.999591-2371.852110.411109.0788167.19782112767.740.99971-2371.472110.14109.0776167.56752212767.910.999735-2371.162109.85109.0773167.6442312767.980.999745-2370.882109.573109.0772167.67582412768.030.999752-2370.612109.319109.0771167.69852512768.080.999758-2370.382109.086109.0771167.71822612768.120.999764-2370.162108.87109.077167.7362712768.150.999769-2369.952108.672109.077167.75222812768.180.999774-2369.762108.487109.0769167.7672912768.210.999778-2369.592108.316109.0769167.78073012768.240.999782-2369.422108.156109.0768167.79333112768.270.999786-2369.272108.007109.0768167.8049影響模擬圖見圖4-8所示：圖4-8塔板數對苯甲醇成品塔的影響經過初步分析，把塔板數設定在塊板16~31之間，由圖4-8分析可知，塔頂苯甲醇回收率、塔頂苯甲醇含量受塔板數的影響不大；冷凝器冷負荷、再沸器熱負荷隨著塔板數的增加小幅下降，綜合考慮設備費用、操作費用及產品純度，我們選塔板數NT=31。4.2.4.進料板影響取理論塔板數為31塊，餾出比為0.9782，回流比為0.2，操作壓力為3KPa，改變進料板位置，經AspenPlus模擬后得到表4-9所示：表4-9進料板對苯甲醇成品塔的影響進料板位置OHKG/HROH冷凝器冷負荷（KJ/hr）再沸器冷負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）212731.390.994504-2370.912106.058109.1303155.0068312749.280.997063-2370.122106.742109.1043160.3962412756.450.998091-2369.82107.138109.0939162.9424512760.250.998636-2369.632107.385109.0884164.4061612762.570.998968-2369.522107.549109.0851165.3426712764.110.999189-2369.462107.664109.0828165.9841812765.190.999344-2369.412107.749109.0813166.4446912765.980.999457-2369.372107.812109.0801166.78681012766.580.999543-2369.352107.862109.0793167.04631112767.030.999609-2369.322107.899109.0786167.25141212767.40.999661-2369.312107.93109.0781167.4121312767.690.999702-2369.32107.955109.0777167.54191412767.920.999736-2369.282107.975109.0773167.64741512768.110.999763-2369.282107.991109.077167.7341612768.270.999786-2369.272108.005109.0768167.80551712768.40.999805-2369.262108.016109.0766167.86511812768.510.99982-2369.262108.025109.0765167.91491912768.60.999833-2369.252108.033109.0763167.95672012768.680.999844-2369.252108.04109.0762167.99192112768.740.999854-2369.252108.046109.0761168.02142212768.80.999861-2369.252108.05109.076168.04622312768.840.999868-2369.242108.054109.076168.06682412768.880.999873-2369.242108.058109.0759168.08312512768.90.999876-2369.242108.06109.0759168.09312612768.860.999871-2369.242108.056109.0759168.0782712768.470.999815-2369.262108.022109.0765167.89742812764.350.999223-2369.452107.683109.0825166.08532912738.810.995565-2370.582106.297109.1195157.09933012673.620.986283-2373.432105.582109.2143143.03683112576.130.972546-2377.562107.404109.3573131.0835影響模擬圖見圖4-9所示：圖4-9進料板對苯甲醇成品塔的影響經過初步分析，把進料板位置設定在第2~31塊板之間，由圖4-9分析可知，塔頂苯甲醇回收率和塔頂苯甲醇含量開始隨著進料板的增加而增加，當進料板超過第17塊后，曲線基本持平，變化很小；冷凝器冷負荷、再沸器熱負荷開始隨著進料板的增加而減少，當進料板超過第17塊后，曲線基本持平，變化很小，綜合考慮設備費用、操作費用及產品純度，我們選進料板位置NF=17。4.2.5.采出影響取理論塔板數為31塊，餾出比為0.9782，回流比為0.2,操作壓力為3KPa，進料塔板為第17塊，改變塔頂餾出比，經AspenPlus模擬后，得到表4-10所示：表4-10采出對苯甲醇成品塔的影響塔頂餾出比OHKG/HROH冷凝器冷負荷（KJ/hr）再沸器冷負荷（KJ/hr）塔頂溫度（℃）塔釜溫度（℃）0.9612531.160.999785-2325.272060.629109.0768138.84350.96212557.270.999785-2330.122065.415109.0768139.90160.96412583.380.999785-2334.962070.234109.0768141.15280.96612609.480.999785-2339.812075.099109.0768142.63880.96812635.590.999785-2344.652080.025109.0768144.43550.9712661.70.999786-2349.492085.035109.0768146.65820.97212687.810.999786-2354.342090.158109.0768149.52960.97412713.910.999786-2359.182095.484109.0768153.30150.97612740.020.999786-2364.032101.136109.0768158.62090.97812766.130.999786-2368.872107.437109.0768166.90220.97816412768.270.999786-2369.272108.004109.0768167.80660.9812782.190.998348-2374.172113.81109.0913175.0689影響模擬圖見圖4-10所示：圖4-10采出對苯甲醇成品塔的影響經過初步分析，把塔頂餾出比設定在0.96~0.98之間，由圖4-10分析可知，塔頂苯甲醇回收率隨著塔頂餾出比的增加而增加，塔頂苯甲醇含量隨著塔頂餾出比的增加變化不大；冷凝器冷負荷、再沸器熱負荷隨著塔頂餾出比的增加而增加，綜合考慮設備費用、操作費用及產品純度，我們選塔頂餾出比D/F=0.9782。

5主要塔設備的設計本章主要對流程中的分解單元的氯化芐回收塔和苯甲醇合成塔進行設計。5.1氯化芐回收塔的設計5.1.1設計依據本工藝需要處理的物料流量大，故而適合選擇板式塔，而填料塔。板式塔可以依據塔盤的類型分為有篩板、泡罩、浮閥及穿流式，由于浮閥塔具有操作彈性好、板效率高，處理量大等優點。根據本工藝塔的操作要求，決定氯化芐回收塔選擇浮閥塔。一般來說水力學數據被認為是氯化芐回收塔的設計基礎，本項目通過AspenPlus模擬得到了氯化芐回收塔T1的水力學數據，見表5-1表5-1氯化芐回收塔T1的水力學數據塔板液相質量流量汽相質量流量液相質量密度汽相質量密度液相粘度汽相粘度表面張力kg/hrkg/hrkg/cumkg/cumcPcP211687.2122766.231089.485630.3617980.5433060.0090728.28649311238.3722317.391068.167520.3590180.5483090.00908727.74423410608.9921688.011046.465260.354750.560210.00910427.67826510138.2121217.231028.082260.3519270.5654350.00911227.6083669856.0920935.111015.824810.351010.565470.00911527.5379279706.64920785.671008.853170.3515320.5637680.00911727.4827189632.27520711.291005.214510.3529080.5619290.00912127.4433399596.35520675.371003.379990.3547350.5602960.00912427.41449109579.22720658.241002.438840.3567850.5588580.00912827.39179119570.81520649.831001.831690.3589380.5576380.00913427.374071241857.1328575.311000.753530.3874210.5571740.00879227.370481341257.3927975.56981.7085590.3790310.5273490.00872526.836591440166.1726884.35965.2567040.3699080.5130030.00865426.640311539386.3626104.54952.1205040.3633190.4986330.0085926.452541638916.7125634.89943.2338480.3597210.4871060.00854526.30091738660.0825378.26937.8471780.3584620.479220.00851926.195111838529.3725247.55934.7655210.3587040.4741650.00850526.125671938467.9925186.17933.0332090.3598160.4708980.00849926.079512038443.5125161.69932.0436170.3614040.4686530.00849826.046792138438.3425156.52931.4502070.3632460.4669650.00849926.021442238443.1825161.35931.0649540.3652210.4655750.008526.000052338453.1725171.35930.7884060.3672650.4643450.00850325.980772438465.825183.98930.5686060.3693450.4632030.00850625.962632538479.7825197.96930.3785040.3714440.462110.00850925.945132638494.6425212.82930.2034340.3735550.4610480.00851225.928032738511.9725230.15930.0294040.3757010.4600160.00851625.911352838550.6325268.81929.786650.3781510.4591050.00852125.896755.1.2塔內件的設計（1）利用AspenPlus對塔進行選型，本次選擇板式塔，板式塔的類型很多，根據考慮，選擇浮閥塔。提餾段的設計見下圖5-1：圖5-1氯化芐回收塔提餾段尺寸設計經計算后，塔板的幾何尺寸結果如下表5-2表5-2塔板提餾段的幾何尺寸結果物性值單位塔盤類型NUTTER-BDP直徑2.6meter塔板間距0.6meter通道數1腳長375IN(9.53MM)浮閥材料CS浮閥厚度14GAUGE單位有效面積中的浮閥數量117.71821/sqm浮閥數量500塔板表厚度10GAUGE塔板表厚度值3.4mm橫截面積5.309292sqm有效面積4.247433sqm凈面積4.778362sqm（2）利用AspenPlus對塔進行選型，本次選擇板式塔，板式塔的類型很多，根據考慮，選擇浮閥塔。精餾段的設計見下圖5-2：圖5-2氯化芐回收塔精餾段尺寸設計經計算后，塔板的幾何尺寸結果如下表5-3表5-3塔板精餾段的幾何尺寸結果物性值單位塔盤類型NUTTER-BDP直徑2.8m塔板間距0.6m通道數1腳長375IN(9.53MM)浮閥材料CS浮閥厚度14GAUGE單位有效面積中的浮閥數量142.10261/sqm浮閥數量700塔板表厚度10GAUGE塔板表厚度值3.4mm橫截面積6.157522sqm有效面積4.926017sqm凈面積5.541769sqm5.1.3氯化芐回收塔的高度塔高度等參數如下表5-4表5-4塔高度參數塔板/填料級數27總高度16.2m總壓頭損失(熱液相高度)1.031398m總壓降0.098213Bar塔段數2直徑數2總停留時間0.044194hr氯化芐回收塔的總高度為16.2m。5.1.4管口設計（1）氯化芐進料管根據經驗提供的流速，確定氯化芐進料流速是μ=5m/s，由于進料體積流量是V=22.72m3/h，所以通過下面的管徑計算公式計算管徑。d=4vπμ×3600=顯而易見的這根管子要選用管徑為?148×3.5mm的管道。（2）塔頂出料管根據經驗確定了塔頂出料液的流速μ=2m/s，由于塔頂出料液的體積流量是V=9.84m3/h，所以通過下面的管徑計算公式計算管徑。d=4Vπμ×3600=顯而易見的這根管子要選用管徑為?48×3.5mm的管道。（3）塔底出料管根據經驗確定了塔頂出料流速μ=0.5m/s，由于塔頂出料液體積流量V=14.30m3/h，所以通過下面的管徑計算公式計算管徑。d=4Vπμ×3600=顯而易見的這根管子要選用管徑20為?×6mm的管道。5.1.5氯化芐回收塔的設計工藝參數匯總將計算結果匯總得到表5-5表5-5氯化芐回收塔計算結果匯總塔徑2800mm板間距600mm塔高16200mm人孔間距4800mm理論塔板數24實際塔板數29全塔效率0.75人孔數3接管尺寸塔底進料管塔底出料口塔頂出料管塔盤形式φ48×3.5mmΦ48×3.5mmφ20×6mm浮閥5.2苯甲醇合成塔的設計5.2.1設計依據AspenPlus模擬得到了苯甲醇合成塔的水力學數據，見表5-6表5-6苯甲醇合成塔B10的水力學數據塔板液相質量流量汽相質量流量液相質量密度汽相質量密度液相粘度汽相粘度表面張力kg/hrkg/hrkg/cumkg/cumcPcPdyne/cm26368.23419138.32962.19190.1086130.7556560.00786629.3682336351.86419121.95961.51520.1118150.7468020.0078829.2912546335.8719105.96960.85660.1150110.738320.00789429.2164256320.23119090.32960.21470.1182010.7301830.00790729.1436266304.93319075.02959.58850.1213860.7223680.0079229.0727276289.96919060.05958.97710.1245660.7148530.00793329.0036486275.34419045.43958.37910.1277410.707620.00794528.9362996261.08919031.18957.79270.1309120.7006510.00795728.8706106247.2919017.38957.21510.1340790.6939320.00796928.80653116234.14719004.23956.64060.1372440.687450.00798128.74412126222.11718992.2956.05740.140410.6811990.00799228.6835136212.20618982.29955.44150.1435850.6751830.00800428.62508146206.59318976.68954.74180.1467840.6694230.00801528.56983156209.9218980.01953.85440.1467030.6639850.00802828.519851618149.7917638.05952.60920.153180.6590080.00803828.479051718163.717651.97952.12010.1563190.6536870.00804828.423861818177.3917665.66951.64020.1594540.6485220.00805828.369751918190.8517679.12951.16890.1625850.6435050.00806828.316662018204.0817692.36950.70590.1657120.6386290.00807828.264562118217.1117705.39950.25080.1688360.6338880.00808728.213412218229.9417718.22949.80340.1719560.6292750.00809728.163182318242.6317730.91949.3630.1750730.6247840.00810628.113842418255.5317743.81948.92770.1781890.6204130.00811528.06542518270.1417758.42948.48510.1813190.6161670.00812428.018112618297.9317786.21947.95740.1845640.6121170.00813527.973722718407.7317896946.85790.1885880.6087180.00815427.943342819040.2718528.55942.85940.1977710.6087090.00820327.990262922066.9521555.22934.6360.2315370.6212880.00818128.274843028385.0327873.29932.92280.2899640.6301810.00790228.179445.2.2塔內件的設計（1）利用AspenPlus對塔進行選型，本次選擇板式塔，板式塔的類型很多，根據考慮，選擇浮閥塔。提餾段的設計見下圖5-3：圖5-3苯甲醇合成塔提餾段尺寸設計經計算后，塔板的幾何尺寸結果如下表5-7表5-7塔板提餾段的幾何尺寸結果物性值單位塔盤類型BALLAST-V1直徑4.6m塔板間距0.8m通道數1腳長375IN(9.53MM)浮閥材料CS浮閥厚度14GAUGE單位有效面積中的浮閥數量99.520361/sqm浮閥數量1400塔板表厚度10GAUGE塔板表厚度值3.4mm橫截面積16.61903sqm有效面積14.06747sqm凈面積15.34325sqm（2）利用AspenPlus對塔進行選型，本次選擇板式塔，板式塔的類型很多，根據考慮，選擇浮閥塔。精餾段的設計見下圖5-8圖5-2苯甲醇合成塔精餾段尺寸設計經計算后，塔板的幾何尺寸結果如下表5-8表5-8塔板精餾段的幾何尺寸結果物性值單位塔盤類型BALLAST-V1直徑4.6m塔板間距0.6m通道數1腳長375IN(9.53MM)浮閥材料CS浮閥厚度14GAUGE單位有效面積中的浮閥數量112.82251/sqm浮閥數量1500塔板表厚度10GAUGE塔板表厚度值3.4mm橫截面積16.61903sqm有效面積13.29522sqm凈面積14.95712sqm5.2.3苯甲醇合成塔的高度塔高度等參數如下表5-9表5-9塔高度參數塔板/填料級數29總高度20.2m總壓頭損失(熱液相高度)1.435956m總壓降0.134108Bar塔段數2直徑數1總停留時間0.260486苯甲醇合成塔的塔高為20.2m。5.2.4管口設計（1）苯甲醇進料管根據經驗提供的流速，確定苯甲醇進料流速是μ=5m/s，由于進料體積流量是V=14.30m3/h，所以通過下面的管徑計算公式計算管徑。d=4Vπμ×3600=顯而易見的這根管子要選用管徑為?36×8mm的管道。