250ThHD330导热油的管壳式换热器的设计毕业论文

 2022-03-09 08:03

论文总字数:19709字

摘 要

高效管壳式换热器因其有优越的传热性能,在各类工程上的使用日益普及。使用高效能的导热油以及合理配置的换热器结构,不仅可以降低换热器的制造所需要的费用,也大大增加了高低温流体之间的换热器系数,达到高效节能的目的。

本次设计从热量,结构,流动阻力以及强度等多个方向多个角度考虑设计管壳式换热器。通过对传热系数K,以及传热面积F的预先估算,再进行详细的热力计算,对于估算的传热系数以及传热面积进行迭代校核,保证真实的传热面积和计算出所需要的面积相比有着15%左右的设计余量,使换热器达到最优化的设计,在合理的选型和体积下,换热系数达到最大。

本次设计中我们可以发现高效导热油为流体的管壳式换热器热交换率可以达到普通流体换热器的几十倍。在计算中发现冷热流体的有效平均温差对于换热器的性能影响也很大,传热系数K的数值直接由的变大而明显增加。结合传热效率和经济性的原则选取1-2型的管壳式换热器,流体的流速均为1m/s。本次设计得出的换热器的主要数据:管总数为284根,正三角形的排列方式,传热系数371,传热面积为83.8m2

关键词: 高效 管壳式换热器 有效平均温差 传热系数 迭代校核

Design of Shell-and-tube Heat Exchanger for 250T/h HD330 Heat Transfer Oil

ABSTRACT

High efficiency shell and tube heat exchanger because of its superior heat transfer performance, the use of various types of projects increasingly popular. The use of high-performance heat transfer oil and the rational configuration of the heat exchanger structure, not only can reduce the heat exchanger manufacturing costs, but also greatly increased the high and low temperature fluid between the heat exchanger coefficient, to achieve the purpose of energy efficient.

This design from the heat, structure, flow resistance and strength and other directions from multiple angles to consider the design of shell and tube heat exchanger. Through the preheating of the heat transfer coefficient K and the heat transfer area F, the detailed heat calculation is carried out, and the estimated heat transfer coefficient and the heat transfer area are iteratively checked to ensure the true heat transfer area and calculate the required area Compared with about 15% of the design margin, so that the heat exchanger to achieve the optimal design, in a reasonable selection and volume, the heat transfer coefficient to achieve the maximum.

In this design, we can find that the heat exchange rate of the shell-and-tube heat exchanger with high efficiency heat transfer oil can reach several times that of the ordinary fluid heat exchanger. In the calculation, it is found that the effective average temperature difference between the hot and cold fluid is also great for the performance of the heat exchanger, and the value of the heat transfer coefficient K is greatly increased. Combined with heat transfer efficiency and economic principles of the choice of 1-2 type shell and tube heat exchanger, the fluid flow rate of 1m / s. The main data of the heat exchanger design: the total number of 284 tubes, the arrangement of the triangle, the heat transfer coefficient of 371, the heat transfer area of 83.8m2.

Key words: Efficient Shell and tube heat exchanger Effective average temperature difference Heat transfer coefficient Iterative check

目录

摘要....................................................Ⅰ

ABSTRACT..............................................Ⅱ

符号表...................................................VI

第一章 绪论...............................................1

第二章 工艺计算...........................................5

2.1 物性参数的确定........................................5

2.2核算换热器传热面积.....................................6

4.2.1传热量及平均温差................................7

4.2.2估算传热面积....................................7

第三章 管壳式换热器结构计算...............................8

3.1换热管计算及排布方式...................................8

3.2壳体内径的估算........................................10

3.3进出口连接管直径的计算................................11

3.4折流板................................................11

3.5管板..................................................14

3.6封头..................................................15

3.7支座..................................................15

第四章 传热校核及阻力计算................................17

4.1管程换热系数..........................................17

4.2 壳程换热系数.........................................18

4.3传热面积校核..........................................18

4.4 管程阻力计算.........................................19

4.5壳程阻力计算..........................................21

第五章 结论与展望..............................................23

参考文献.................................................24

致谢....................................................27

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