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个人收集整理资料，仅供交流学习，勿作商业用途1/39淮阴工学院课程设计说明书作者:学号：系(院:专业:题目:苯-甲苯筛板精馏塔的设计指导者：2018年6月化工原理课程设计说明书中文摘要个人收集整理资料，仅供交流学习，勿作商业用途2/39精馏是利用混合液中组分挥发度的差异，实现组分高纯度分离的多级蒸馏操作，即同时实现多次部分汽化和部分冷凝的过程。实现精馏操作的主体设备是精馏塔。塔设备是能够实现蒸馏的气液传质设备，广泛应用于化工、石油化工、石油等工业中，其结构形式基本上可以分为板式塔和填料塔两大类。我国石油工业具有一定的水平，但还是一个发展中的国家,摆在我们石油工作者面前的任务是繁重的。因此必须坚持独立自主、自力更生，革新挖潜，全面提高，综合利用，大搞化工原料，赶超世界先进水平。关键词：精馏塔塔板苯—甲苯塔板负荷淮阴工学院个人收集整理资料，仅供交流学习，勿作商业用途3/39化工原理课程设计任务书专业：化学工程与工艺班级：姓名：学号：设计日期：2018年6月21日至2018年7月2日设计题目：苯-甲苯筛板精馏塔的设计设计条件：进料量F=160kmol/h进料组成=0.55摩尔分率）进料温度tF=泡点温度产品要求=96%回收率=94%设计内容:1、精馏塔的物料衡算；2、塔板数、压降的计算；3、精馏塔的工艺条件及有关物性数据的计算；4、精馏塔的相关工艺尺寸计算；5、绘制精馏塔设计条件图。个人收集整理资料，仅供交流学习，勿作商业用途4/39指导教师：胡涛2018年6月目录1.引言··························································61.1塔设备的分类···················································61.2塔设备在化工生产中的作用和地位·······························61.3设计条件·····················································6个人收集整理资料，仅供交流学习，勿作商业用途5/391.4问题研究·····················································62.板式塔的设计·················································62．1工业生产对塔板的要求·········································62.2设计方案的确定················································72.2.2操作压力的选择··············································72.2.3进料热状况的选择············································72.2.4加热方式的选择··············································7个人收集整理资料，仅供交流学习，勿作商业用途6/392.2.5回流比的选择················································73工艺流程图······················································74.工艺计算及主体设备的计算·······································84.1精馏塔的物料衡算··············································84.1.1原料液及塔顶、塔底产品的摩尔分率·····························84.1.2原料液及塔顶、塔底产品的平均摩尔质量·························84.1.3物料衡算···········································8个人收集整理资料，仅供交流学习，勿作商业用途7/394.2塔板数的确定··················································94.2.1理论板层数NT的求取········································94.2.2实际板层数的求解···········································94.3精馏塔的工艺条件及有关物性数据计算···························94.3.1操作压力的计算··············································104.3.2操作温度计算················································114.3.3平衡摩尔质量的计算··········································11个人收集整理资料，仅供交流学习，勿作商业用途8/394.3.4平均密度的计算·············································124.3.5液体平均表面张力计算·······································134.3.6液体平均粘度计算···········································134.4精馏塔的塔体工艺尺寸计算······································144.4.1塔径计算····················································144.4.2精馏塔有效高度的计算·······································154.5.塔板主要工艺尺寸的计算······································15个人收集整理资料，仅供交流学习，勿作商业用途9/394.5.1溢流装置计算················································154.5.2塔板布置····················································164.6.筛板的流体力学验算···········································174.6.1塔板压降····················································174.6.2液面落差····················································184.6.3液沫夹带···················································184.6.4漏液························································19个人收集整理资料，仅供交流学习，勿作商业用途10/394.6.5液泛························································194.7塔板负荷性能图················································194.7.1漏液线······················································204.7.2液沫夹带····················································204.7.3液相负荷下限线··············································214.7.4液相负荷上限线··············································214.7.5液泛线······················································22个人收集整理资料，仅供交流学习，勿作商业用途11/395.辅助设备的草图及选型·········································245.1回流冷凝器··················································245.2再沸器······················································25结束语····························································27参考文献···························································27个人收集整理资料，仅供交流学习，勿作商业用途12/39引言1.1塔设备的分类塔设备是能够实现蒸馏的气液传质设备，广泛应用于化工、石油化工、石油等工业中，其结构形式基本上可以分为板式塔和填料塔两大类。板式塔内设置一定数量的塔板，气体以鼓泡或喷射的方式穿过板上的液层，进行传质于传热。在正常操作下，气相为分散相，液相为连续相，气相组成呈阶梯变化，属于逐级接触逆流操作过程。填料塔内装有一定高度的填料层，液体自塔顶沿填料表面下流，气体逆流向上(有时也采用并流向下流动，气体两相密切接触进行传热与传质。在正常操作过程中，气相为连续相，液相为分散相，气相组成呈连续变化，属于微分接触逆流操作过程。1.2塔设备在化工生产中的作用和地位精馏过程的实质是利用混合物中各组分具有不同的挥发度。即在同一温度下，各组分的饱和蒸汽压不同这一性质，使液相中的轻组分转移到汽相中，汽相中的重组分转移到液相中，从而达到分离的目的。因此精馏塔操作弹性的好坏直接关系到石油化工企业的经济效益。在化工生产中，塔设备的性能对于整个装置的产品产量、质量、生产能力和消耗定额，以及三废处理和环境保护等各个方面，都有非常重大的影响。个人收集整理资料，仅供交流学习，勿作商业用途13/391.3设计条件进料量每小时160千摩尔，原料中含苯55%摩尔分率），以沸点状态送入塔内。要求塔顶馏出物含苯96%摩尔分率），塔釜残液中含苯不大于4%，操作回流比取最小回流比的2.5倍。1.4问题研究本设计是针对苯—甲苯的分离而专门设计的塔设备。根据设计条件以及给出的数据描述出塔温度的分布，求得最小回流比以及塔顶的相对挥发度、塔釜的相对挥发度、全塔平均相对挥发度，又根据物料平衡公式分别计算出精馏段和提馏段的汽、液两相的流量。之后，计算塔板数、塔径等。根据这些计算结果进行了塔板结构的设计等。计算和设计这些之后进行了有关的力学性能计算和一系列的校核。2．板式塔的设计2.1工业生产对塔板的要求：①通过能力要大，即单位塔截面能处理的气液流量大。②塔板效率要高。③塔板压力降要低。④操作弹性要大。⑤结构简单，易于制造。在这些要求中，对于要求产品纯度高的分离操作，首先应考虑高效率；对于处理量大的一般性分离如原油蒸馏等），主要是考虑通过能力大。2．2设计方案的确定2．2.1装置流程的确定精馏装置包括精馏塔，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。蒸馏过程按操作方式不同，可分为连续精馏和间歇精馏两种流程。个人收集整理资料，仅供交流学习，勿作商业用途14/39在本次的设计中，是为分离苯—甲苯混合物。对于二元混合物的分离，应该采用连续精馏流程。2.2.2操作压力的选择蒸馏过程按操作压力不同，可分为常压蒸馏，减压蒸馏和加压蒸馏。一般除热敏性物系外，凡通过常压分离要求