Optimization on shell side structure of twisty flow heat exchanger based on orthogonal experiment

doi:10.16085/j.issn.1000-6613.2018-1364

Abstract

Abstract:

Periodic entire cross-section computation model of twisty flow shell-and-tube heat exchanger is established, and the reliability of numerical simulation method and its results is verified by contrast experiment. The major factors affecting the heat transfer and flow resistance performance on shell side fluid of twisty flow heat exchanger include the spacing between two adjacent groups of trapezoidal baffles, the width of baffles, the inclination angle of baffles and the number of per group of baffles. The various parameters influencing heat transfer coefficient, pressure drop and comprehensive performance on shell side fluid of twisty flow heat exchanger are studied by designing orthogonal experiment, and the structural parameters with significant effect are optimized. The results show that in the range of research parameters, the main and secondary order which influence the comprehensive performance on shell side fluid of twisty flow heat exchanger are that the spacing between two adjacent groups of trapezoidal baffles > the number of per group of baffles > the inclination angle of baffles > the width of baffles. The optimal structural parameters of combination considered comprehensive performance should be that the spacing between two adjacent groups of trapezoidal baffles is 100mm, the number of per group of baffles is 2,the inclination angle of baffles is 52.5° and the width of baffles is 100mm, then the comprehensive performance is 114.9. The results of the study provide a new method for multi-objective optimization of shell-side structural parameters of shell-and-tube heat exchanger which has certain guiding significance.

Key words: shell-and-tube heat exchanger, twisty flow, orthogonal experiment, numerical simulation, heat transfer enhancement

摘要：

建立扭转流管壳式换热器周期性全截面数值计算模型，采用对比实验验证了数值模拟方法及其结果的可靠性。影响扭转流换热器壳程流体换热和流阻性能的主要因素有相邻两组类梯形导流板间距、导流板宽度、导流板倾斜角度以及每组导流板的数量。设计正交试验，综合研究各参数对扭转流换热器壳程流体传热系数、压降及综合性能的影响，并对影响显著的结构参数进行了优化。结果表明，在研究参数范围内，影响扭转流换热器壳程流体综合性能的主次顺序为：相邻两组导流板间距>每组导流板数量>导流板倾斜角度>导流板宽度。综合性能最优的结构参数组合是相邻两组导流板间距为100mm、每组导流板个数为2、导流板倾斜角度为52.5°、导流板宽度为100mm，综合性能最高为114.9。研究结果为管壳式换热器壳程结构参数进行多目标优化提供了一种新方法，具有一定的指导意义。

关键词: 管壳式换热器, 扭转流, 正交试验, 数值模拟, 传热强化

CLC Number:

TK124

Xin GU, Zhiyang ZHENG, Yuankun LUO, Xiaochao XIONG, Dabo ZHANG. Optimization on shell side structure of twisty flow heat exchanger based on orthogonal experiment[J]. Chemical Industry and Engineering Progress, 2019, 38(04): 1688-1695.

古新, 郑志阳, 罗元坤, 熊晓朝, 张大波. 基于正交试验的扭转流换热器壳程结构优化[J]. 化工进展, 2019, 38(04): 1688-1695.

Figures/Tables 14

References 22

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水平	模拟因素
水平	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度/(°)	每组导流板数量/块
1	100	80	30.0	2
2	125	85	37.5	3
3	150	90	45.0	4
4	175	95	52.5	5
5	200	100	60.0	6

水平	模拟因素
水平	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度/(°)	每组导流板数量/块
1	100	80	30.0	2
2	125	85	37.5	3
3	150	90	45.0	4
4	175	95	52.5	5
5	200	100	60.0	6

试验	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度 /(°)	每组导流板数量 /块	数值计算结果
试验	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度 /(°)	每组导流板数量 /块	?p /Pa·m^-1	α /W·m^-2·K^-1	Nu /f ^1/3
1	100	80	30.0	2	2915.5	3124.6	112.2
2	100	85	37.5	3	3674	3292.2	111.1
3	100	90	45.0	4	3231	3111.8	107.1
4	100	95	52.5	5	2534.5	2860.2	104.5
5	100	100	60.0	6	2076.1	2691.3	102.4
6	125	80	37.5	4	2970.3	2876.7	98.1
7	125	85	45.0	5	2398.5	2694.1	97.4
8	125	90	52.5	6	2096.6	2783.5	105.6
9	125	95	60.0	2	678.9	2059.9	101.6
10	125	100	30.0	3	5363	3268.1	99.5
11	150	80	45.0	6	2275	2588.4	93.2
12	150	85	52.5	2	677.5	2128.5	105.2
13	150	90	60.0	3	694.8	2052.5	99.4
14	150	95	30.0	4	4894.4	3095.1	94.6
15	150	100	37.5	5	4506.3	3027.1	96.1
16	175	80	52.5	3	789.4	2077.1	97.6
17	175	85	60.0	4	618.8	1945.7	96.2
18	175	90	30.0	5	5012.7	2857.5	85.5
19	175	95	37.5	6	2672.9	2695.4	93.9
20	175	100	45.0	2	991.2	2317.4	104.7
21	200	80	60.0	5	591.9	2007.9	99.3
22	200	85	30.0	6	1802.4	2321.4	87.2
23	200	90	37.5	2	1154.9	2302.9	100.2
24	200	95	45.0	3	1214.5	2204.2	92.7
25	200	100	52.5	4	998.3	2350.2	105.9

试验	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度 /(°)	每组导流板数量 /块	数值计算结果
试验	相邻两组导流板间距 /mm	导流板宽度 /mm	导流板倾斜角度 /(°)	每组导流板数量 /块	?p /Pa·m^-1	α /W·m^-2·K^-1	Nu /f ^1/3
1	100	80	30.0	2	2915.5	3124.6	112.2
2	100	85	37.5	3	3674	3292.2	111.1
3	100	90	45.0	4	3231	3111.8	107.1
4	100	95	52.5	5	2534.5	2860.2	104.5
5	100	100	60.0	6	2076.1	2691.3	102.4
6	125	80	37.5	4	2970.3	2876.7	98.1
7	125	85	45.0	5	2398.5	2694.1	97.4
8	125	90	52.5	6	2096.6	2783.5	105.6
9	125	95	60.0	2	678.9	2059.9	101.6
10	125	100	30.0	3	5363	3268.1	99.5
11	150	80	45.0	6	2275	2588.4	93.2
12	150	85	52.5	2	677.5	2128.5	105.2
13	150	90	60.0	3	694.8	2052.5	99.4
14	150	95	30.0	4	4894.4	3095.1	94.6
15	150	100	37.5	5	4506.3	3027.1	96.1
16	175	80	52.5	3	789.4	2077.1	97.6
17	175	85	60.0	4	618.8	1945.7	96.2
18	175	90	30.0	5	5012.7	2857.5	85.5
19	175	95	37.5	6	2672.9	2695.4	93.9
20	175	100	45.0	2	991.2	2317.4	104.7
21	200	80	60.0	5	591.9	2007.9	99.3
22	200	85	30.0	6	1802.4	2321.4	87.2
23	200	90	37.5	2	1154.9	2302.9	100.2
24	200	95	45.0	3	1214.5	2204.2	92.7
25	200	100	52.5	4	998.3	2350.2	105.9

水平	传热系数α/W·m^-2·K^-1
水平	相邻两组导流板间距 /mm	导流板宽度/mm	导流板倾斜角度 /(°)	每组导流板数量/块
均值1	3016.1	2534.9	2933.3	2406.7
均值2	2736.5	2466.4	2838.8	2578.8
均值3	2578.3	2621.6	2583.2	2675.9
均值4	2378.6	2582.9	2439.9	2689.3
均值5	2237.3	2750.8	2151.4	2616.1
极差	778.7	284.4	781.9	282.6