采用扭曲片内插件的管壳式换热器自动设计新方法

doi:10.16085/j.issn.1000-6613.2023-1410

化工进展 ›› 2024, Vol. 43 ›› Issue (9): 4824-4832.DOI: 10.16085/j.issn.1000-6613.2023-1410

• 化工过程与装备 • 上一篇

采用扭曲片内插件的管壳式换热器自动设计新方法

崔祎¹(), 李孟原¹, 杨路², 李海东², 张奇琪², 常承林²^,³(), 王彧斐¹

^1.中国石油大学(北京)化学工程与环境学院，北京 102249
^2.重庆大学化学化工学院，重庆 401331
^3.浙江大学化学工程与生物工程学院，浙江杭州 310027

收稿日期:2023-08-13 修回日期:2023-10-16 出版日期:2024-09-15 发布日期:2024-09-30
通讯作者: 常承林
作者简介:崔祎（1999—），男，博士研究生，研究方向为过程系统工程。E-mail：cuiyi0227@foxmail.com。
基金资助:
中央高校基本科研业务费专项(2024CDJXY010);重庆市出站留（来）渝博士后择优资助项目(Z20240373);国家自然科学基金(22008210)

New method for automatic design of intensified shell and tube heat exchanger with twisted-tape insert

CUI Yi¹(), LI Mengyuan¹, YANG Lu², LI Haidong², ZHANG Qiqi², CHANG Chenglin²^,³(), WANG Yufei¹

^1.College of Chemical Engineering, China University of Petroleum, Beijing 102249, China
^2.School of Chemistry and Chemical Engineering, Chongqing University, Chongqing 401331, China
^3.College of Chemical and Biological Engineering, Zhejiang University, Hangzhou 310027, Zhejiang, China

Received:2023-08-13 Revised:2023-10-16 Online:2024-09-15 Published:2024-09-30
Contact: CHANG Chenglin

摘要/Abstract

摘要：

管壳式换热器作为应用最广泛的换热器，对其进行优化设计是一个十分重要的研究主题。现有的设计方法多数是基于启发式方法求解或调用商业求解器，其运算速度较慢且不能保证设计解的质量。本文将集合修剪算法应用于管壳式换热器的自动设计，将管外径、管长、壳程直径、管程数、扭曲片节距、扭曲片厚度等定义为离散变量后输入，程序自动输出设计结果与方案。对采用扭曲片内插件的管壳式换热器进行自动设计优化，分别以最小化换热面积、年度总费用、净现值作为优化目标进行单目标优化。对比发现集合修剪算法可以保证设计解的全局最优，同时降低优化求解时间，可在0.5~2s内给出结果。以换热面积最小化为目标函数的优化结果显示，集合修剪算法可得到更小的换热面积，比文献值减少了0.7%，同时采用强化传热可减少换热面积。热流分配在管程时，强化技术降低了7.7%的换热面积，管程侧的压降则提高了16.9%；热流分配在壳程时，则降低14.6%的换热面积，管程压降提高了98.7%。以最小化年度总费用和净现值为目标的优化结果显示，强化传热的费用低于未强化情况，热流分配在管程时费用降低13.1%，分配在壳程时则降低0.57%。此外，换热器的费用也会受到成本参数的影响。

关键词: 换热器, 强化传热, 全局最优, 集合修剪

Abstract:

Shell and tube heat exchangers are the most widely used heat exchangers, and optimizing their design is a crucial research topic. Most existing design methods are based on heuristic methods or commercial solvers, which are slow in solving and can't guarantee the quality of design solutions. This paper applied set trimming to the automatic design of shell and tube heat exchangers. The outer diameter of tubes, the length of tubes, the diameter of the shell side, the number of tube sides, the pitch of twist-tapes, and the thickness of twist-tapes were defined as discrete variables and input into the program, which automatically output the design results and solutions. The automatic design optimization of shell and tube heat exchangers that intensified with twisted-tape insert was carried out by using single-objective optimization with the minimization heat exchange area, total annualized cost, and net present cost as optimization objectives. By comparison, we find that set trimming could ensure the global optimization of the design solution, and its solving time was very short. It could provide results within 0.5—2s. The results of minimizing the heat transfer area as the objective function showed that set trimming could obtain a smaller heat transfer area, which was reduced by 0.7% compared to the literature value. At the same time, the use of intensification techniques could reduce the heat transfer area. When the heat stream was distributed on the tube side, the technique reduced the heat transfer area by 7.7%, and the tube-side pressure drop increased by 16.9%. When the heat stream was distributed on the shell side, the heat transfer area was reduced by 14.6%, and the tube-side pressure drop increased by 98.7%. The optimization results with the objective of minimizing total annualized cost and net present cost showed that the cost of intensified conditions was lower than that of non-intensified states, and when the heat stream distribution was on the tube side, it was 13.1% lower. When distributed on the shell side, it was 0.57% lower. In addition, the cost of heat exchangers will also be affected by cost parameters.

Key words: heat exchanger, heat transfer enhancement, global optimization, set trimming

中图分类号:

TQ021

崔祎, 李孟原, 杨路, 李海东, 张奇琪, 常承林, 王彧斐. 采用扭曲片内插件的管壳式换热器自动设计新方法[J]. 化工进展, 2024, 43(9): 4824-4832.

CUI Yi, LI Mengyuan, YANG Lu, LI Haidong, ZHANG Qiqi, CHANG Chenglin, WANG Yufei. New method for automatic design of intensified shell and tube heat exchanger with twisted-tape insert[J]. Chemical Industry and Engineering Progress, 2024, 43(9): 4824-4832.

图/表 9

参考文献 26

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变量	取值
管外径/m	0.019，0.025，0.032，0.038，0.051
管长/m	1.220，1.829，2.439，3.049，3.659，4.877，6.098
间径比	1.25，1.33，1.50
管束布局方式	1表示正方形布局，2表示三角形布局
管程	1，2，4，6
挡板数	1，2，3，…，20
壳程直径/m	0.787，0.838，0.889，0.940，0.991，1.067，1.143，1.219，1.372，1.524
扭曲片节距/m	0.074700，0.103275，0.131850
扭曲片厚/m	0.002，0.003，0.004

变量	取值
管外径/m	0.019，0.025，0.032，0.038，0.051
管长/m	1.220，1.829，2.439，3.049，3.659，4.877，6.098
间径比	1.25，1.33，1.50
管束布局方式	1表示正方形布局，2表示三角形布局
管程	1，2，4，6
挡板数	1，2，3，…，20
壳程直径/m	0.787，0.838，0.889，0.940，0.991，1.067，1.143，1.219，1.372，1.524
扭曲片节距/m	0.074700，0.103275，0.131850
扭曲片厚/m	0.002，0.003，0.004

物流	质量流量 /kg·s^-1	进口温度 /℃	出口温度 /℃	污垢系数 /m²·K·W^-1	密度 /kg·m^-3	比热容 /J·kg^-1·K^-1	黏度 /Pa·s	热导率 /W·m^-1·K^-1	允许压降 /Pa	流速范围 /m·s^-1
热流乙醇	55.6	150	60	0.00020	789.0	2470.0	0.00067	0.170	100000	[1.0,3.0]
冷流冷却水	295.0	30	40	0.00040	995.0	4186.8	0.00080	0.590	100000	[0.5,2.0]

物流	质量流量 /kg·s^-1	进口温度 /℃	出口温度 /℃	污垢系数 /m²·K·W^-1	密度 /kg·m^-3	比热容 /J·kg^-1·K^-1	黏度 /Pa·s	热导率 /W·m^-1·K^-1	允许压降 /Pa	流速范围 /m·s^-1
热流乙醇	55.6	150	60	0.00020	789.0	2470.0	0.00067	0.170	100000	[1.0,3.0]
冷流冷却水	295.0	30	40	0.00040	995.0	4186.8	0.00080	0.590	100000	[0.5,2.0]

设计参数	ST	SS	ST-TI	SS-TI
管外径/m	0.019	0.019	0.025	0.019
管长/m	4.877	6.098	6.098	4.877
间径比	1.25	1.25	1.25	1.25
管束布局方式	正方形	正方形	正方形	三角形
管程	6	1	4	1
挡板数	4	15	6	11
壳程直径/m	0.991	0.838	0.940	0.838
扭曲片节距/m	—	—	0.074700	0.074700
扭曲片厚/ m	—	—	0.004	0.002

采用扭曲片内插件的管壳式换热器自动设计新方法

New method for automatic design of intensified shell and tube heat exchanger with twisted-tape insert

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图/表 9

参考文献 26

相关文章 15

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Metrics

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优化结果	ST	SS	ST-TI	SS-TI
换热面积/m²	337.4	329.4	288.3	304.2
管程流速/m·s^-1	1.9	1.7	1.8	1.8
壳程流速/m·s^-1	1.5	1.1	1.8	1.0
管程传热系数/W·m^-2·K^-1	2120.5	7138.4	3155.3	9636.7
壳程传热系数/W·m^-2·K^-1	6447.8	1800.3	6243.1	2003.9
总传热系数/W·m^-2·K^-1	712.2	691.9	839.6	743.5
管程压降/Pa	84105.4	16419.2	98350.5	32628.5
壳程压降/Pa	74199.6	88556.3	95056.2	86121.3

设计参数	ST	SS	ST-TI	SS-TI
管外径/ m	0.019	0.019	0.019	0.025
管长/m	4.877	4.877	4.877	4.877
间径比	1.5	1.25	1.5	1.25
管束布局方式	三角形	正方形	三角形	三角形
管程	6	1	4	1
挡板数	5	13	4	13
壳程直径/m	1.143	0.94	1.067	0.991
扭曲片节距/m	—	—	0.074700	0.074700
扭曲片厚/m	—	—	0.002	0.002

优化结果	ST	SS	ST-TI	SS-TI
年度总费用/USD·a^-1	85439.0	73357.3	74255.8	72941.1
净现值/USD·a^-1	323881.2	278081.9	281488.0	276504.0
换热面积/m²	359.8	331.6	313.5	323.3
管程流速/m·s^-1	1.8	1.3	1.4	1.0
壳程流速/m·s^-1	1.0	1.1	0.9	1.0
管程传热系数/W·m^-2·K^-1	2014.1	5938.9	3091.6	6400.8
壳程传热系数/W·m^-2·K^-1	4153.6	1775.7	3902.2	1758.0
总传热系数/W·m^-2·K^-1	657.9	672.4	754.2	692.0
管程压降/Pa	74773.8	8830.7	91101.0	10110.9
壳程压降/Pa	27144.4	83074.4	17190.4	83682.3

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换热情况	用时/s
ST	0.216
SS	0.204
ST-TI	2.366
SS-TI	2.264
SS-MILP	2824

换热情况	用时/s
ST	0.216
SS	0.204
ST-TI	2.366
SS-TI	2.264
SS-MILP	2824