《化工原理课程设计》报告
50000吨/年乙醇~水 精馏装置设计
年级 专业 设计者姓名 设计单位 完成日期
2010级 10生物工程
吴瑶 巢湖学院 2012年 12 月 25 日
目 录
一、概述 ························································································ 1
1.1 设计依据 ············································································ 1 1.2 技术来源 ············································································ 1 1.3 设计任务及要求 ··································································· 1 二：计算过程 ·················································································· 2
1. 塔型选择 ·············································································· 2 2. 操作条件的确定 ····································································· 4
2.1 操作压力 ······································································ 4 2.2 进料状态 ······································································ 4 2.3 加热方式 ······································································ 4 2.4 热能利用 ······································································ 5 3. 有关的工艺计算 ····································································· 5
3.1 工艺流程简图 ································································ 5 3.2 工艺计算 ······································································ 5 3.3 最小回流比、操作比的计算 ·············································· 6 3.4 塔顶产品产量及釜残夜量的计算 ········································ 7 3.5全凝器冷凝介质的消耗量 ·················································· 7 3.6热能利用 ······································································· 8
3.7 理论塔板层数的确定 ······················································· 8
3.8全塔效率的估算 ······························································ 9 3.9 实际塔板数NP ···································· 错误！未定义书签。
4. 精馏塔主题尺寸的计算 ·································· 错误！未定义书签。 4.1 精馏段与提馏段的体积流量 ···················· 错误！未定义书签。
4.1.1 精馏段 ······································· 错误！未定义书签。 4.1.2 提馏段 ······································· 错误！未定义书签。 4.2 塔径的计算 ········································· 错误！未定义书签。 4.3 塔高的计算 ········································· 错误！未定义书签。 5. 塔板结构尺寸的确定 ····································· 错误！未定义书签。
5.1 塔板尺寸 ············································ 错误！未定义书签。 5.2 弓形降液管 ········································· 错误！未定义书签。
5.2.1 堰高 ·········································· 错误！未定义书签。 5.2.2 降液管底隙高度h0 ························ 错误！未定义书签。 5.2.3 进口堰高和受液盘 ························ 错误！未定义书签。 5.3 浮阀数目及排列 ··································· 错误！未定义书签。
5.3.1 浮阀数目 ···································· 错误！未定义书签。 5.3.2 排列 ·································································· 19 5.3.3 校核 ·········································· 错误！未定义书签。
6. 流体力学验算 ·············································· 错误！未定义书签。
6.1 气体通过浮阀塔板的压力降(单板压降)hp ·· 错误！未定义书签。
6.1.1 干板阻力hc ································ 错误！未定义书签。 6.1.2 板上充气液层阻力h1 ···················· 错误！未定义书签。 6.1.3 由表面张力引起的阻力h? ·············· 错误！未定义书签。 6.2 漏液验算 ············································ 错误！未定义书签。
6.3 液泛验算 ············································ 错误！未定义书签。 6.4 雾沫夹带验算 ······································ 错误！未定义书签。 7. 操作性能负荷图 ··········································· 错误！未定义书签。
7.1 雾沫夹带上限线 ··································· 错误！未定义书签。 7.2 液泛线 ··············································· 错误！未定义书签。 7.3 液体负荷上限线 ··································· 错误！未定义书签。 7.4 漏液线 ··············································· 错误！未定义书签。 7.5 液相负荷下限线 ··································· 错误！未定义书签。 7.6 操作性能负荷图 ··································· 错误！未定义书签。 8. 各接管尺寸的确定 ········································ 错误！未定义书签。
8.1 进料管 ··············································· 错误！未定义书签。 8.2 釜残液出料管 ······································ 错误！未定义书签。 8.3 回流液管 ············································ 错误！未定义书签。 8.4 塔顶上升蒸汽管 ··································· 错误！未定义书签。 8.5 水蒸汽进口管 ······································ 错误！未定义书签。
9.主要符号说明 ······································································· 30 10.结论 ················································································ 32
10.1评述及感想 ········································································ 32 10.2参考文献 ·············································································· 33
一、概述
乙醇~水是工业上最常见的溶剂，也是非常重要的化工原料之一，是无色、无毒、无致癌性、污染性和腐蚀性小的液体混合物。因其良好的理化性能，而被广泛地应用于化工、日化、医药等行业。近些年来，由于燃料价格的上涨，乙醇燃料越来越有取代传统燃料的趋势，且已在郑州、济南等地的公交、出租车行业内被采用。山东业已推出了推广燃料乙醇的法规。
长期以来，乙醇多以蒸馏法生产，但是由于乙醇~水体系有共沸现象，普通的精馏对于得到高纯度的乙醇来说产量不好。但是由于常用的多为其水溶液，因此，研究和改进乙醇`水体系的精馏设备是非常重要的。
塔设备是最常采用的精馏装置，无论是填料塔还是板式塔都在化工生产过程中得到了广泛的应用，在此我们作板式塔的设计以熟悉单元操作设备的设计流程和应注意的事项是非常必要的。
塔设备是化工、炼油生产中最重要的设备之一。塔设备的设计和研究，已经受到化工行业的极大重视。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。 1.1 设计依据
本设计依据于教科书的设计实例，对所提出的题目进行分析并做出理论计算。 1.2 技术来源
目前，精馏塔的设计方法以严格计算为主，也有一些简化的模型，但是严格计算法对于连续精馏塔是最常采用的，我们此次所做的计算也采用严格计算法。 1.3 设计任务及要求
原料：乙醇~水溶液，年产量50000吨
乙醇含量：40%(质量分数)，原料液温度：45℃
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设计要求：塔顶的乙醇含量不小于95%(质量分数) 塔底的乙醇含量不大于1%(质量分数)
表1 乙醇~水溶液体系的平衡数据
液相中乙醇的含量(摩尔分数) 汽相中乙醇的含量(摩尔分数) 液相中乙醇的含量(摩尔分数) 汽相中乙醇的含量(摩尔分数) 0.0 0.004 0.01 0.02 0.04 0.06 0.08 0.10 0.14 0.18 0.20 0.25 0.30 0.35
二：计算过程 1. 塔型选择
0.0 0.053 0.11 0.175 0.273 0.34 0.392 0.43 0.482 0.513 0.525 0.551 0.575 0.595 0.40 0.45 0.50 0.55 0.60 0.65 0.70 0.75 0.80 0.85 0.894 0.90 0.95 1.0 0.614 0.635 0.657 0.678 0.698 0.725 0.755 0.785 0.82 0.855 0.894 0.898 0.942 1.0 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气相中，气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。
筛板塔是孔板塔的一种，内装若干层水平塔板，板上有许多小孔，形状如筛；
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