3.7万吨乙烯浮阀塔设计说明书

内容摘要

精馏塔是进行精馏的一种塔式汽液接触装置，又称为蒸馏塔。有板式塔与填料塔两种主要类型。根据操作方式又可分为连续精馏塔与间歇精馏塔。

液蒸汽由塔底进入，与液体进行逆流接触，两相接触中，下降中的易挥发(低沸点)组分不断地向蒸汽中转移，蒸汽中的难挥发(高沸点)组分不断地向下降液中转移，蒸汽愈接近塔顶，其易挥发组分浓度愈高，而下降液愈接近塔底，其难挥发组分则愈富集，达到组分分离的目的。由塔顶上升的蒸汽进入冷凝器，冷凝的液体的一部分作为回流液返回塔顶进入精馏塔中，其余的部分则作为馏出液取出。塔底流出的液体，其中的一部分送入再沸器，经过再沸器的加热，蒸汽返回塔中，另一部分液体作为釜残液取出。

我设计的精馏塔为年产3.7万吨乙烯精馏浮阀塔设备。其设计内容包括两个部分，第一部分为塔设备的工艺计算，包括对进出塔组分的分析，回流比的计算，塔径的确定，塔高，塔板结构以及流体演算和塔附属设备的计算。第二部分为塔设备的强度校核，包括对壳体的强度计算，质量载荷计算，地震以及风弯矩的计算，以及裙座和裙座附属结构的计算。

通过这次设计我了解到了精馏塔操作的优点，包括以下几点：一：生产能力大：即单位塔截面大的气液相流率，不会产生液泛等

沈阳化工大学毕业设计内容摘要

不正常流动。二：效率高：气液两相在塔内保持充分的密切接触，具有较高的塔板效率或传质效率。三：流体阻力小：流体通过塔设备时阻力降小，可以节省动力费用，在减压操作是时，易于达到所要求的真空度。四：有一定的操作弹性：当气液相流率有一定波动时，两相均能维持正常的流动，而且不会使效率发生较大的变化。五：结构简单，造价低，安装检修方便。六：能满足某些工艺的特性：腐蚀性，热敏性，起泡性等。

本塔的主要结构尺寸为：塔高30.4米，塔径1.6米，塔的壁厚为18毫米，其中塔板有49块，裙座高度为3米.塔内操作压力位2.0 MPa。

关键词：精馏塔；塔板；再沸器；冷凝器；热敏性

沈阳化工大学毕业设计内容摘要

Abstract

Distillation column is a distillation tower vapor-liquid contact devices, also known as the distillation column. There are plate tower with the two main types of packed tower. According to mode of operation can be divided into continuous distillation and batch distillation.

Steam from the bottom to enter, with the decline in countercurrent contact with liquid, two-phase contact, a decrease in the volatile liquid (low boiling point) component continually transferred to the steam, steam evaporation of hard (high boiling point) component continue to to the decline in the transfer of liquid, steam the closer we get to the top of the tower, the higher the concentration of volatile components, and the closer we get to the bottom liquid drop, and its difficult they are, the more volatile-rich component to the purpose of separation. Steam rising from the top of the tower into the condenser, part of the liquid condensate as reflux liquid into the distillation column to return to the top of the tower, the rest of the part removed as distillate. The liquid bottom, into which part of the reboiler, thermal evaporation, the vapor to return to Tajikistan, the other part of the liquid residue removed as the kettle.

I design the distillation column for the annual production capacity of 37,000 tons of ethylene distillation tower equipment plate. The design includes three parts, the first part of the process equipment for the tower,

沈阳化工大学毕业设计内容摘要

including both components of the tower and out of the analysis, the calculation of reflux ratio, the determination of column diameter, height, structure, and fluid tray tower calculus and ancillary equipment calculation. The second part of the strength check of tower equipment, including the strength of the shell, the mass loading, the moment the earthquake, as well as the calculation of the wind, as well as group Block group Block, and the calculation of a subsidiary structure. Part III is divided into the design process in the selected literature.

I understand that through the design of the merits of the distillation operation, including the following: a: large production capacity: that is, large section of the tower unit gas-liquid flow rate will not result in flooding, such as abnormal flow. B: high efficiency: gas-liquid two-phase to keep the tower full of close contact with high efficiency or the tray mass transfer efficiency. III: fluid resistance small: when the fluid through the column pressure drop small, can save power costs, when in the decompression operation is easy to reach the required vacuum. Four: a certain degree of flexibility in operation: When the gas-liquid flow rate fluctuations in a certain time, they maintain the normal two-phase flow, and will not lead to large changes in efficiency. Five: simple structure, low cost and easy installation maintenance. 6: Process to meet some of the characteristics: corrosive, heat-sensitive, foaming, and so on.

The main structure of the tower dimensions are: height 30.4 meters, 1.6

沈阳化工大学毕业设计内容摘要

meters diameter tower, tower wall thickness of 18 mm, of which there are 49trays, skirt height of three meters. Tanega bit operating pressure 2.0MPa. Keywords: distillation; tray; reboiler; condenser; thermosensitive

沈阳化工大学毕业设计内容摘要

目录

一. 工艺计算 (1)

1.1物料衡算 (1)

1.2确定塔温 (2)

1.2.1塔顶温度 (2)

1.2.2塔底温度 (2)

1.2.3进料温度 (3)

1.3塔板数的计算 (3)

1.3.1确定最小回流比 (3)

1.3.2最小理论板数 (4)

1.3.3塔板数的确定 (4)

1.3.4确定进料位置 (5)

1.4塔径的计算 (5)

1.4.1气液相负荷及密度 (5)

1.4.2初估塔径 (9)

1.5塔内物件的工艺尺寸 (10)

1.5.1流程数的选择 (10)

1.5.2提馏段 (12)

1.6流体力学演算 (15)

1.6.1精馏段 (15)

1.6.2提馏段 (16)

1.7塔的操作负荷性能图 (18)

1.7.1精馏段的操作负荷性能图 (18)

1.7.2提馏段 (21)

1.8附属设备的选择 (23)

1.8.1全凝器的的计算 (23)

1.8.2再沸器的热量衡算 (24)

1.8.3回流泵的选取 (25)

1.9管径的确定 (25)

1.9.1塔顶蒸汽管 (25)

1.9.2塔顶回流管 (26)

1.9.3进料管 (26)

1.9.4塔釜出料管 (26)

1.9.5釜液进再沸器管 (26)

1.9.6再沸器蒸汽入塔管 (27)

二强度及稳定性计算 (28)

2.1封头与筒体 (28)

2.2开孔补强计算 (28)

2.2.1塔顶蒸汽管 (29)

2.2.2回流管 (29)

2.2.3进料管 (30)

2.2.4塔釜出料管 (31)

2.2.5釜液进再沸器管 (31)

2.2.6再沸器入塔管 (32)

2.3质量载荷计算 (33)

2.4塔的自振周期 (34)

2.5地震载荷及地震弯距计算： (34)

2.6风载荷和风弯矩计算 (36)

2.7最大弯矩 (38)

2.8圆筒应力校核 (39)

2.9裙座壳轴向应力校核 (40)

2.10基础环厚度计算 (41)

2.11地脚螺栓 (42)

2.12筋板 (42)

2.13盖板 (43)

2.14裙座与塔壳对接连接焊缝的验算 (44)

三吊柱的强度计算 (44)

3.1设计载荷 (44)

3.2进杆部分的校核 (45)

3.3柱的校核 (46)

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