《年产10万吨苯甲醇工艺设计》14000字（论文）

年产10万吨苯甲醇工艺设计摘要：苯甲醇作为合成香料和医药的重要中间体，在感光、染整、化妆品、涂料及油墨等众多领域有着十分广泛的应用。本设计首先进行初步工艺设定，查找根据三大平衡算出各路线上的参数，然后利用AspenPlus化工流程模拟软件对全流程进行模拟，其次通过优化流程中设备的操作条件，得到最优的操作条件，在热量衡算、物料衡算的基础上，对精馏塔设备进行选型。最后对生产进行技术经济核算，并且绘制了制备苯甲醇工艺流程图。本设计采用的是氯化苄连续水解法制备苯甲醇，此法具有收率高、无环境污染等优点，国内尚处于起步阶段，研究连续水解法生产工艺具有重要的现实意义。关键词：工艺设计；苯甲醇；AspenPlus模拟目录引言 [17]。因此，接下来我们使用AspenPlus对分离单元中各精馏塔的上述变量进行灵敏度分析，旨在达到控制指标的前提下，获得最佳的操作条件。4.1氯化苄回收塔操作参数的设计对氯化苄回收塔T1而言，其轻关键组分XB为氯化苄，重关键组分XD为苯甲醇。该塔条件设计的目标为：塔顶馏出液中苯甲醇回收率控制在0.0001以下，塔釜液中的氯化苄质量含量控制在10mg/L以下。下面逐个考察单个条件的影响：4.1.1操作压力的影响取理论塔板数为29块，馏出比为0.4701，回流比为0.9，进料塔板为第15块，改变操作压力，经AspenPlus模拟后，得到表4-1所示：表4-1操作压力对氯化苄回收塔对的影响操作压力（Bar）OHCL冷凝器冷负荷（KJ/hr）再沸器热负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟见图4-1所示：图4-1操作压力对氯化苄回收塔对的影响由图4-1可知，塔顶苯甲醇回收率、塔釜氯化苄含量、冷凝器冷负荷、再沸器热负荷均随着操作压力的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选择操作压力P=0.1Bar=10KPa。4.1.2.回流比的影响取理论塔板数为29块，塔顶馏出比为0.4701，操作压力为10KPa,进料塔板为第15块，改变回流比，经AspenPlus模拟后，得到表4-2所示：表4-2回流比对氯化苄回收塔对的影响回流比OHKG/HRCL冷凝器冷负荷（KJ/hr）再沸器冷负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-2所示：图4-2回流比对氯化苄回收塔对的影响经过初步分析，把氯化苄回收塔回流比设定0.84~0.86在之间，由图4-2分析可知，塔顶苯甲醇回收率和塔釜氯化苄含量随着回流比的增加而下降；冷凝器冷负荷、再沸器热负荷随着回流比的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选回流比R=0.9。4.1.3.塔板数的影响取进料塔板为第15块，塔顶馏出比为0.4701，操作压力为10KPa，回流比为0.9，改变塔板数，经AspenPlus模拟后，得到表4-3所示：表4-3塔板数对氯化苄回收塔对的影响塔板数OHKG/HRCL冷凝器冷负荷（KJ/hr）再沸器冷负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-3所示：图4-3塔板数对氯化苄回收塔对的影响经过初步分析，把进料板位置设定在第10~29块板之间，由图4-3分析可知，塔顶苯甲醇回收率和塔釜氯化苄含量随着塔板数的增加而下降，当塔板数超过块29块后，曲线基本持平，变化很小；冷凝器冷负荷、再沸器热负荷也同样如此，综合考虑设备费用、操作费用及产品纯度，我们选塔板数NT=29。4.1.4.进料板影响取塔板数为第29块,塔顶馏出比为0.4701，操作压力为10KPa，回流比为0.9,改变进料板位置，经AspenPlus模拟后，得到表4-4所示：表4-4进料板对氯化苄回收塔对的影响进料板位置OHKG/HRCL冷凝器冷负荷（KJ/hr）再沸器热负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-4所示：图4-4进料板对氯化苄回收塔对的影响经过初步分析，把进料板位置设定在第10~18块板之间，由图4-4分析可知，塔顶苯甲醇回收率和塔釜氯化苄含量开始随着进料板的增加而下降，但当进料板为第15块时，塔顶苯甲醇回收率和塔釜氯化苄含量开始随着进料板的增加而增加；冷凝器冷负荷、再沸器热负荷也同样如此，综合考虑设备费用、操作费用及产品纯度，我们选进料板位置NF=15。4.1.5.采出影响取理论塔板数为29块，取进料塔板为第15块，塔顶馏出比为0.4701，操作压力为10KPa，回流比为0.9，改变采出，经AspenPlus模拟后，得到表4-5所示：表4-5采出对氯化苄回收塔对的影响塔顶馏出比OHKG/HRCL冷凝器冷负荷（KJ/hr）再沸器热负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-5所示：图4-5采出对氯化苄回收塔对的影响经过初步分析，把塔顶馏出比设定在0.4700~0.4800之间，由图4-5可知，塔顶苯甲醇回收率开始随着塔顶馏出比的增加变化不大，当塔顶馏出比超过0.4701时，塔顶苯甲醇回收率随着塔顶馏出比的增加直线上升；塔釜氯化苄含量开始随着塔顶馏出比的增加直线下降，当塔顶馏出比超过0.4701时，塔釜氯化苄含量随着塔顶馏出比的增加变化不大；冷凝器冷负荷、再沸器热负荷随着塔顶馏出比的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选塔顶馏出比D/F=0.4701。4.2苯甲醇成品塔操作参数的设计对苯甲醇成品塔B10而言，其轻关键组分XB为苯甲醇，重关键组分XD为二苄醚。该塔条件设计的目标为：塔顶馏出液中苯甲醇回收率达到0.99,塔顶馏出液中苯甲醇含量大于0.99999。下面逐个考察单个条件的影响：4.2.1.操作压力的影响取理论塔板数为31块，馏出比为0.9782，回流比为0.2，进料塔板为第17块，改变操作压力，经AspenPlus模拟后，得到表4-6所示：表4-6操作压力对苯甲醇成品塔的影响操作压力（Bar）OHKG/HROH冷凝器冷负荷（KJ/hr）再沸器热负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-6所示：图4-6操作压力对苯甲醇成品塔的影响由图4-6可知，塔顶苯甲醇回收率、塔顶苯甲醇含量受操作压力的影响不大；冷凝器冷负荷、再沸器热负荷均随着操作压力的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选择操作压力P=0.03Bar=3KPa。4.2.2.回流比的影响取理论塔板数为31块，馏出比为0.9782，回流比为0.2，进料塔板为第17块，改变操作压力，经AspenPlus模拟后得到表4-7所示：表4-7回流比对苯甲醇成品塔的影响回流比OHKG/HRWOH冷凝器冷负荷（KJ/hr）再沸器冷负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-7所示：图4-7回流比对苯甲醇成品塔的影响经过初步分析，把苯甲醇成品塔回流比设定在0.1~0.3之间，由图4-7分析可知，塔顶苯甲醇回收率和塔顶苯甲醇含量随着回流比的增加而增加，当回流比超过0.2144时，曲线基本持平，变化很小；冷凝器冷负荷、再沸器热负荷随着回流比的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选回流比R=0.2。4.2.3.塔板数的影响取理论塔板数为31块，馏出比为0.9782，操作压力为3KPa，回流比为0.2，改变塔板数，经AspenPlus模拟后得到表4-8所示：表4-8塔板数对苯甲醇成品塔的影响塔板数OHKG/HROH冷凝器冷负荷（KJ/hr）冷凝器冷负荷（KJ/hr）塔釜温度（℃）塔釜温度（℃）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影响模拟图见图4-8所示：图4-8塔板数对苯甲醇成品塔的影响经过初步分析，把塔板数设定在块板16~31之间，由图4-8分析可知，塔顶苯甲醇回收率、塔顶苯甲醇含量受塔板数的影响不大；冷凝器冷负荷、再沸器热负荷随着塔板数的增加小幅下降，综合考虑设备费用、操作费用及产品纯度，我们选塔板数NT=31。4.2.4.进料板影响取理论塔板数为31块，馏出比为0.9782，回流比为0.2，操作压力为3KPa，改变进料板位置，经AspenPlus模拟后得到表4-9所示：表4-9进料板对苯甲醇成品塔的影响进料板位置OHKG/HROH冷凝器冷负荷（KJ/hr）再沸器冷负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-9所示：图4-9进料板对苯甲醇成品塔的影响经过初步分析，把进料板位置设定在第2~31块板之间，由图4-9分析可知，塔顶苯甲醇回收率和塔顶苯甲醇含量开始随着进料板的增加而增加，当进料板超过第17块后，曲线基本持平，变化很小；冷凝器冷负荷、再沸器热负荷开始随着进料板的增加而减少，当进料板超过第17块后，曲线基本持平，变化很小，综合考虑设备费用、操作费用及产品纯度，我们选进料板位置NF=17。4.2.5.采出影响取理论塔板数为31块，馏出比为0.9782，回流比为0.2,操作压力为3KPa，进料塔板为第17块，改变塔顶馏出比，经AspenPlus模拟后，得到表4-10所示：表4-10采出对苯甲醇成品塔的影响塔顶馏出比OHKG/HROH冷凝器冷负荷（KJ/hr）再沸器冷负荷（KJ/hr）塔顶温度（℃）塔釜温度（℃）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影响模拟图见图4-10所示：图4-10采出对苯甲醇成品塔的影响经过初步分析，把塔顶馏出比设定在0.96~0.98之间，由图4-10分析可知，塔顶苯甲醇回收率随着塔顶馏出比的增加而增加，塔顶苯甲醇含量随着塔顶馏出比的增加变化不大；冷凝器冷负荷、再沸器热负荷随着塔顶馏出比的增加而增加，综合考虑设备费用、操作费用及产品纯度，我们选塔顶馏出比D/F=0.9782。

5主要塔设备的设计本章主要对流程中的分解单元的氯化苄回收塔和苯甲醇合成塔进行设计。5.1氯化苄回收塔的设计5.1.1设计依据本工艺需要处理的物料流量大，故而适合选择板式塔，而填料塔。板式塔可以依据塔盘的类型分为有筛板、泡罩、浮阀及穿流式，由于浮阀塔具有操作弹性好、板效率高，处理量大等优点。根据本工艺塔的操作要求，决定氯化苄回收塔选择浮阀塔。一般来说水力学数据被认为是氯化苄回收塔的设计基础，本项目通过AspenPlus模拟得到了氯化苄回收塔T1的水力学数据，见表5-1表5-1氯化苄回收塔T1的水力学数据塔板液相质量流量汽相质量流量液相质量密度汽相质量密度液相粘度汽相粘度表面张力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塔内件的设计（1）利用AspenPlus对塔进行选型，本次选择板式塔，板式塔的类型很多，根据考虑，选择浮阀塔。提馏段的设计见下图5-1：图5-1氯化苄回收塔提馏段尺寸设计经计算后，塔板的几何尺寸结果如下表5-2表5-2塔板提馏段的几何尺寸结果物性值单位塔盘类型NUTTER-BDP直径2.6meter塔板间距0.6meter通道数1脚长375IN(9.53MM)浮阀材料CS浮阀厚度14GAUGE单位有效面积中的浮阀数量117.71821/sqm浮阀数量500塔板表厚度10GAUGE塔板表厚度值3.4mm横截面积5.309292sqm有效面积4.247433sqm净面积4.778362sqm（2）利用AspenPlus对塔进行选型，本次选择板式塔，板式塔的类型很多，根据考虑，选择浮阀塔。精馏段的设计见下图5-2：图5-2氯化苄回收塔精馏段尺寸设计经计算后，塔板的几何尺寸结果如下表5-3表5-3塔板精馏段的几何尺寸结果物性值单位塔盘类型NUTTER-BDP直径2.8m塔板间距0.6m通道数1脚长375IN(9.53MM)浮阀材料CS浮阀厚度14GAUGE单位有效面积中的浮阀数量142.10261/sqm浮阀数量700塔板表厚度10GAUGE塔板表厚度值3.4mm横截面积6.157522sqm有效面积4.926017sqm净面积5.541769sqm5.1.3氯化苄回收塔的高度塔高度等参数如下表5-4表5-4塔高度参数塔板/填料级数27总高度16.2m总压头损失(热液相高度)1.031398m总压降0.098213Bar塔段数2直径数2总停留时间0.044194hr氯化苄回收塔的总高度为16.2m。5.1.4管口设计（1）氯化苄进料管根据经验提供的流速，确定氯化苄进料流速是μ=5m/s，由于进料体积流量是V=22.72m3/h，所以通过下面的管径计算公式计算管径。d=4vπμ×3600=显而易见的这根管子要选用管径为ϕ148×3.5mm的管道。（2）塔顶出料管根据经验确定了塔顶出料液的流速μ=2m/s，由于塔顶出料液的体积流量是V=9.84m3/h，所以通过下面的管径计算公式计算管径。d=4Vπμ×3600=显而易见的这根管子要选用管径为ϕ48×3.5mm的管道。（3）塔底出料管根据经验确定了塔顶出料流速μ=0.5m/s，由于塔顶出料液体积流量V=14.30m3/h，所以通过下面的管径计算公式计算管径。d=4Vπμ×3600=显而易见的这根管子要选用管径20为ϕ×6mm的管道。5.1.5氯化苄回收塔的设计工艺参数汇总将计算结果汇总得到表5-5表5-5氯化苄回收塔计算结果汇总塔径2800mm板间距600mm塔高16200mm人孔间距4800mm理论塔板数24实际塔板数29全塔效率0.75人孔数3接管尺寸塔底进料管塔底出料口塔顶出料管塔盘形式φ48×3.5mmΦ48×3.5mmφ20×6mm浮阀5.2苯甲醇合成塔的设计5.2.1设计依据AspenPlus模拟得到了苯甲醇合成塔的水力学数据，见表5-6表5-6苯甲醇合成塔B10的水力学数据塔板液相质量流量汽相质量流量液相质量密度汽相质量密度液相粘度汽相粘度表面张力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塔内件的设计（1）利用AspenPlus对塔进行选型，本次选择板式塔，板式塔的类型很多，根据考虑，选择浮阀塔。提馏段的设计见下图5-3：图5-3苯甲醇合成塔提馏段尺寸设计经计算后，塔板的几何尺寸结果如下表5-7表5-7塔板提馏段的几何尺寸结果物性值单位塔盘类型BALLAST-V1直径4.6m塔板间距0.8m通道数1脚长375IN(9.53MM)浮阀材料CS浮阀厚度14GAUGE单位有效面积中的浮阀数量99.520361/sqm浮阀数量1400塔板表厚度10GAUGE塔板表厚度值3.4mm横截面积16.61903sqm有效面积14.06747sqm净面积15.34325sqm（2）利用AspenPlus对塔进行选型，本次选择板式塔，板式塔的类型很多，根据考虑，选择浮阀塔。精馏段的设计见下图5-8图5-2苯甲醇合成塔精馏段尺寸设计经计算后，塔板的几何尺寸结果如下表5-8表5-8塔板精馏段的几何尺寸结果物性值单位塔盘类型BALLAST-V1直径4.6m塔板间距0.6m通道数1脚长375IN(9.53MM)浮阀材料CS浮阀厚度14GAUGE单位有效面积中的浮阀数量112.82251/sqm浮阀数量1500塔板表厚度10GAUGE塔板表厚度值3.4mm横截面积16.61903sqm有效面积13.29522sqm净面积14.95712sqm5.2.3苯甲醇合成塔的高度塔高度等参数如下表5-9表5-9塔高度参数塔板/填料级数29总高度20.2m总压头损失(热液相高度)1.435956m总压降0.134108Bar塔段数2直径数1总停留时间0.260486苯甲醇合成塔的塔高为20.2m。5.2.4管口设计（1）苯甲醇进料管根据经验提供的流速，确定苯甲醇进料流速是μ=5m/s，由于进料体积流量是V=14.30m3/h，所以通过下面的管径计算公式计算管径。d=4Vπμ×3600=显而易见的这根管子要选用管径为ϕ36×8mm的管道。