精馏塔课程设计资料，希望有用.doc

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一、概述

1.1 设计依据

1.2 技术来源

1.3 设计任务及要求

二：计算过程

1. 塔型选择

2. 操作条件的确定

2.1 操作压力

2.2 进料状态

2.3 加热方式

2.4 热能利用

3. 有关的工艺计算

3.1 最小回流比及操作回流比的确定

3.2 塔顶产品产量、釜残液量及加热蒸汽量的计算

3.3 全凝器冷凝介质的消耗量

3.4 热能利用

3.5 理论塔板层数的确定

3.6 全塔效率的估算

3.7 实际塔板数

4. 精馏塔主题尺寸的计算

4.1 精馏段与提馏段的体积流量

4.1.1 精馏段

4.1.2 提馏段

4.2 塔径的计算

4.3 塔高的计算

5. 塔板结构尺寸的确定

5.1 塔板尺寸

5.2 弓形降液管

5.2.1 堰高

5.2.2 降液管底隙高度h0

5.2.3 进口堰高和受液盘

5.3 浮阀数目及排列

5.3.1 浮阀数目

5.3.2 排列

5.3.3 校核

6. 流体力学验算

6.1 气体通过浮阀塔板的压力降(单板压降)

6.1.1 干板阻力

6.1.2 板上充气液层阻力

6.1.3 由表面张力引起的阻力

6.2 漏液验算

6.3 液泛验算

6.4 雾沫夹带验算

7. 操作性能负荷图

7.1 雾沫夹带上限线

7.2 液泛线

7.3 液体负荷上限线

7.4 漏液线

7.5 液相负荷下限线

7.6 操作性能负荷图

8. 各接管尺寸的确定

8.1 进料管

8.2 釜残液出料管

8.3 回流液管

8.4 塔顶上升蒸汽管

8.5 水蒸汽进口管

《化工原理课程设计》报告 48000 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年月日 1

目录一、概述 ························································································ 4 1.1 设计依据 ·············································································4 1.2 技术来源 ·············································································4 1.3 设计任务及要求 ····································································5 二：计算过程 ·················································································· 5 1. 塔型选择 ·············································································· 6 2. 操作条件的确定 ····································································· 6 2.1 操作压力 ·······································································6 2.2 进料状态 ·······································································6 2.3 加热方式 ·······································································6 2.4 热能利用 ·······································································7 3. 有关的工艺计算 ····································································· 7 3.1 最小回流比及操作回流比的确定 ········································ 8 3.2 塔顶产品产量、釜残液量及加热蒸汽量的计算 ······················ 8 3.3 全凝器冷凝介质的消耗量 ················································· 9 3.4 热能利用 ·······································································9 3.5 理论塔板层数的确定 ······················································10 3.6 全塔效率的估算 ···························································· 11 3.7 实际塔板数 PN ·····························································12 4. 精馏塔主题尺寸的计算 ·························································· 12 4.1 精馏段与提馏段的体积流量 ·············································12 4.1.1 精馏段 ································································12 4.1.2 提馏段 ································································14 4.2 塔径的计算 ·································································· 15 4.3 塔高的计算 ·································································· 17 5. 塔板结构尺寸的确定 ······························································17 5.1 塔板尺寸 ····································································· 17 5.2 弓形降液管 ·································································· 18 5.2.1 堰高 ···································································18 5.2.2 降液管底隙高度 h0 ················································ 18 5.2.3 进口堰高和受液盘 ·················································19 5.3 浮阀数目及排列 ···························································· 19 2

5.3.1 浮阀数目 ·····························································19 5.3.2 排列 ···································································19 5.3.3 校核 ···································································20 6. 流体力学验算 ·······································································21 ph ···························21 6.1 气体通过浮阀塔板的压力降(单板压降) 6.1.1 干板阻力 ch ························································· 21 6.1.2 板上充气液层阻力 1h ············································· 21 6.1.3 由表面张力引起的阻力 h ······································ 21 6.2 漏液验算 ····································································· 22 6.3 液泛验算 ····································································· 22 6.4 雾沫夹带验算 ······························································· 22 7. 操作性能负荷图 ····································································23 7.1 雾沫夹带上限线 ···························································· 23 7.2 液泛线 ········································································ 23 7.3 液体负荷上限线 ···························································· 24 7.4 漏液线 ········································································ 24 7.5 液相负荷下限线 ···························································· 24 7.6 操作性能负荷图 ···························································· 25 8. 各接管尺寸的确定 ·································································26 8.1 进料管 ········································································ 26 8.2 釜残液出料管 ······························································· 27 8.3 回流液管 ····································································· 27 8.4 塔顶上升蒸汽管 ···························································· 27 8.5 水蒸汽进口管 ······························································· 28 3

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。 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。 4

1.3 设计任务及要求原料：乙醇~水溶液，年产量 48000 吨乙醇含量：35%(质量分数)，原料液温度：45℃ 设计要求：塔顶的乙醇含量不小于 90%(质量分数) 塔底的乙醇含量不大于 0.5%(质量分数) 表 1 乙醇~水溶液体系的平衡数据液相中乙醇的汽相中乙醇的液相中乙醇的汽相中乙醇的含量(摩尔分数) 含量(摩尔分数) 含量(摩尔分数) 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 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 二：计算过程 5

1. 塔型选择根据生产任务，若按年工作日 300 天，每天开动设备 24 小时计算，产品流量为 6667 /kg h ，由于产品粘度较小，流量较大，为减少造价，降低生产过程中压降和塔板液面落差的影响，提高生产效率，选用浮阀塔。 2. 操作条件的确定 2.1 操作压力由于乙醇~水体系对温度的依赖性不强，常压下为液态，为降低塔的操作费用，操作压力选为常压其中塔顶压力为 1.01325 10 Pa  5 塔底压力 [1.01325 10  5  N (265 ~ 530)] Pa 2.2 进料状态虽然进料方式有多种，但是饱和液体进料时进料温度不受季节、气温变化和前段工序波动的影响，塔的操作比较容易控制；此外，饱和液体进料时精馏段和提馏段的塔径相同，无论是设计计算还是实际加工制造这样的精馏塔都比较容易，为此，本次设计中采取饱和液体进料 2.3 加热方式精馏塔的设计中多在塔底加一个再沸器以采用间接蒸汽加热以保 6

证塔内有足够的热量供应；由于乙醇~水体系中，乙醇是轻组分，水由塔底排出，且水的比热较大，故可采用直接水蒸气加热，这时只需在塔底安装一个鼓泡管，于是可省去一个再沸器，并且可以利用压力较底的蒸汽进行加热，无论是设备费用还是操作费用都可以降低。 2.4 热能利用精馏过程的原理是多次部分冷凝和多次部分汽化。因此热效率较低，通常进入再沸器的能量只有 5%左右可以被有效利用。虽然塔顶蒸汽冷凝可以放出大量热量，但是由于其位能较低，不可能直接用作为塔底的热源。为此，我们拟采用塔釜残液对原料液进行加热。 3. 有关的工艺计算由于精馏过程的计算均以摩尔分数为准，需先把设计要求中的质量分数转化为摩尔分数。原料液的摩尔组成： x f  n CH CH OH n  n CH CH OH 3 2 3 2 35/ 46 35/ 46 65/18   H O 2  0.1740 同理可求得： x D  0.7790, x W  0.0002 原料液的平均摩尔质量： M f  x M f CH CH OH 3 2 (1   x M f ) H O 2  0.174 46 0.826) 18 22.3     kg kmol / 同理可求得： M D  39.81 kg kmol M / ,  W 18.1 kg kmol / 45℃下，原料液中  H O 2  971.1 kg m / 3 ,  CH CH OH 3 2  735 kg m / 3 由此可查得原料液，塔顶和塔底混合物的沸点，以上计算结果见 7

表 2。名称 / %fx 表 2 原料液、馏出液与釜残液的流量与温度原料液馏出液釜残液 35 90 fx (摩尔分数) 0.1740 0.7790 摩尔质量 /kg kmol 沸点温度t /℃ 22.3 83.83 39.81 78.62 3.1 最小回流比及操作回流比的确定 0.5 0.0002 18.1 99.38 由于是泡点进料， x q x f  0.174 ，过点 (0.174,0.174) e 做直线 x  0.174 交平衡线于点 d ，由点 d 可读得 qy  0.516 ，因此： R min(1)  x d y q   q y x q  0.779 0.516 0.516 0.174    0.769 又过点 (0.779,0.779) a 作平衡线的切线，切点为 g ，读得其坐标为 x q ' 0.55,  y q ' 0.678  ，因此： R min(2)  x D y q  '  q y x q ' '  0.779 0.678 0.678 0.55    0.789 所以， min R R min(2)  0.789 可取操作回流比 R  1( R R / min  1.27) 3.2 塔顶产品产量、釜残液量及加热蒸汽量的计算 8

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