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1、设计题目板 式精 僧 塔设 计成绩课 程 设 计 主 要 内 容一、精馅塔优化设计计算1、精僧流程的确定2、塔的物料衡算3、塔的工艺条件及物性数据计算4、塔板数的确定5、塔径的初步设计6、溢流装置的设计7、塔板布置8、浮阀数n与开孔率仞的确定9、塔板流动性能的校核10、塔板负荷性能图11、塔的结构与辅助设备的设计12、精馅塔主体装备的机械设计二、工艺流程图的设计及绘制三、精馅塔主体装配图的设计及绘制指 导 老 师 评 语指导老师签名：2011年 月 日1.8工艺流程说明一整套精馅装置应该包括精儒塔、原料预热器、再沸器、冷凝器、釜液冷却 器和产品冷却器等设备。热量自塔釜输入，物料在塔内经多次部分
2、气化与部分冷 凝进行精僧分离，由冷凝器和冷却器中的冷却介质将余热带走。乙醇一水混合液原料经预热器加热到泡点温度后送入精馄塔进料板，在进料板上 与自塔上部下降的的回流液体汇合后，逐板溢流，最后流入塔底。在每层板上， 回流液体与上升蒸汽互相接触，进行热和质的传递过程。操作时，连续地从再沸 器取出部分液体作为塔底产品，部分液体气化，产生上升蒸汽，一起通过各层塔 板。塔顶蒸汽进入冷凝器中被冷凝，并将部分冷凝液送回塔顶作为回流液，其余 部分经冷凝器冷凝后送出作为塔顶产品，经冷凝器冷却后送入贮槽。塔釜采用再 沸器加热。塔底产品经冷却后送入贮槽。工艺计算2.1物料衡算2.1.1. 将质量分数转换成摩尔分数4
3、04。46.068460= 0.2068761 46.0684 18.01489446.0684 = 0.859676 946146.0684 18.01480.0546.06840.05 F 46.068499.9518.0148= 0.00019562.1.2. 平均摩尔质量M)= 46.0684x0.8597 + (1-0.8597) x 18.0148 = 42.131/ kmolMf = 0.2068X 46.0684+ (1 - 0.2068) x 18.0148 = 23.8 59kg/kmolMw = 0.0001956x 46.0684 + (1-0.0001956) X18
4、.0148=18.0203g / kmol2.1.3. 物料衡算4861.1Y0.94DH).000W=0.4x486LI解方程组，得rD = 2067.024432794.07562. 1.4.摩尔流量的计算F = FMf = 4861.1 - 23.8159 = 204.111 Ikmol/hD = DM d = 2067.02443 + 42.1318 = 49.06094%。，W = WMw = 2794.0756 -18.0203 = 155.05164kmol / h 2. 2塔板数确定2. 2.1.理论塔板数Nt的求取由乙醇一水相平衡数据画得相平衡图，作出对角线y=x ,取点(0
5、. 859676, 0. 859676)液体中酒精质蒸汽中沸点液体中酒精摩尔分蒸汽中量分数酒精质 / C 数酒精摩量质量尔分数分数0.010.1399.90.0040.0530.11.399.80.040.510.151.9599.70.0550.770.22.699.60.081.030.33.899.50.121.570.44.999.40.161.980.56.199.30.192.480.67.199.20.232.90.78.199.10.273.30.89990.313.7250.99.998.90.354.12110.7598.750.394.51219.797.650.798.
6、76327.296.651.1912.75433.395.81.6116.3453794.952.0118.68641.194.152.4321.45744.693.352.8623.96847.692.63.2926.2195091.93.7328.121052.291.34.1629.921154.190.84.6131.561255.890.55.0733.061357.489.75.5134.571458.889.25.9835.831560896.4636.981661.188.36.8638.061762.287.97.4139.161863.287.77.9540.181964.
7、387.48.4141.272065878.9242.092165.886.79.4242.942266.686.49.9343.822367.386.210.4844.61246885.951145.412568.685.711.5346.082669.385.412.0846.92769.885.212.6447.492870.38513.1948.082970.884.813.7748.683071384.714.3549.33171.784.514.9549.773272.184.315.5550.273372.584.216.1550.783472.983.816.7751.2735
8、73.283.7517.4151.673673.583.718.0352.043773.883.518.6852.43387483.419.3452.683974383.32053.094074.683.120.6853.464174.882.9521.3853.764275.182.7822. 0754.124375.482.6522.7954.544475.682.523.5154.84575.982.4524.2555.224676.182.352555.484776.382.325.7555.744876.582.1526.5356.034976.88227.3256.44507781
9、.928.1256.715177.381.828.9357.125277.581.729.857.415377.781.630.6157.7547881.531.4758.115578.281.432.3458.395678.581.333.2458.785778.781.2534.1659.1587981.235.0959.555979.281.136.0259.846079.58136.9860.296179.780.9537.9160.58628080.8538.9561.026380.380.754061.446480.580.6541.0261.766580.880.642.0962
10、.22668180.543.1762.526781.380.4544.2762.996881.680.445.4163.436981.980.346.5563.917082.180.247.7264.217182.480.148.9264.77282.88050.1665.347383.179.9551.3965.817483.479.8552.6866.287583.879.755466.937684.179.7255.3467.427784.579.756.7168.077884.979.6558.7168.767985.479.5559.5569.598085.879.561.0270.
11、298186.379.462.5271.148286.779.364.0571.868387.279.265.6472.718487.779.167.2773.618588.378.9568.9274.698688.978.8570.6275.818789.578.75723676.938890.178.6574.15788990.778.675.9979.269091.378.577.8880.42919278.479.8281.839292.6578.381.8283.159393.478.2783.8784.79494.278.285.9786.49595.0578.1888.1588.
12、2595.5795.5778.1589.4189.41从像图中可知在点(0. 7788;0. 8042)处有斜率最大值。设其值为K.v 0.859676 0.8042K= 0.685940.859676-0.7788由此可得R前广一仁=Q6859 =2.184 m，n 1-K 1-0.68594经编程(13. 1)可得Rmm=2.21R 代 1.2xRmm = L2x2.21 = 2.652原设回流比与所求最优回流比相差不大，符合要求。J = J + J2 + AJ为精馄塔总费用4为精馅塔塔体的折旧费以及维修费，）% %为再沸器折旧费及操作费用，另4=（E.+O.O6）（C + G/）式中稣是塔体折旧率，c/,己=；二；8 10G是塔板的费用，元 C是塔体的费用，元C, = 278.38凡5久 exp（0.57R.）N/E 弓为美元对人民币的汇率取6.5171E为塔板类型因子，浮阀塔昌=1
