换热器复杂流道中的强化传热研究
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摘要
本文对三种不同结构的换热器进行了强化传热研究，分别是圆形翅片管换热器、矩形自支撑缩放管换热器和管壳式换热器。
通过实验得到Re、纵向管间距（Sl）及管束排列方式对圆形翅片管换热器传热性能的影响数据，再利用数值模拟的方法分析这三个因素影响的原因。Re变化范围为4970~23620，Sl为66mm到130mm，而管束排列方式则为顺排和叉排。Nu及f均随Re的增加而增加，且增加趋势逐渐下降。增大管间距会提高顺排的传热性能，但是提高幅度随间距的增加而减小，在Sl=110mm时换热效果最好；而叉排则不同，增大间距反而会降低换热器的传热性能，叉排的换热效果在Sl=66mm时是最好的。相对于顺排，叉排的换热效果要更好。对于换热器传热性能的提高可以从场协同与回流区面积及尾流涡尺度三个方面的变化来进行分析，寻找换热器结构改善的途径。
在新型换热器——矩形自支撑矩形缩放管换热器的基础上，利用三维数值模拟的方法对换热器插入不同的插入物后，其流道内流动及传热特性进行了研究，Re数的变化范围为27900~41900。四种不同插入物分别为：圆环、扭带、旋流片和折板，并将加入不同插入物后换热器的综合性能与无插入物时的性能做对比，得出的结论如下：与无插入物时相比，壳侧的传热系数在分别加入圆环、扭带、旋流片及折板后依次增加了16.69~24.32%，31.07~33.08%，28.32~33.13%，38.01~46.74%，传热性能的提升伴随着阻力的增加，四种情况下阻力分别增加了74.02~89.5%，69.32~77.42%，54.35~65.74和68.49~87.16%，在综合考虑传热性能与摩擦阻力两方面的因素后发现，加入插入物后换热器的综合传热性能由高到低依次为插入折板、插入扭带、插入旋流片、插入圆环，无插入物时的综合性能是最差的。通过研究发现，提升矩形自支撑换热器传热性能的关键在于提高换热器两侧区域的传热性能。利用场协同理论进行分析后发现，减小速度场与温度场之间的夹角有利于提高换热器的传热性能。
在自支撑矩形缩放管换热器内插物研究的基础上，利用三维数值模拟的方法分别研究在缩放段长度比例保持不变的情况下，缩放节距及缩放肋高对换热器管程、壳程及整体综合传热性能的影响，并得出缩放管的优化尺寸。研究表明：对于换热器管程和壳程，缩放节距L越小，换热效果越好，阻力也越大，壳程在L=16.5mm时综合传热性能达到最佳，而管程则在L=9mm时综合传热性能最好；缩放肋高h越大，二者的换热效果越好，阻力也由于管子的粗糙程度增加而变大，此时综合传热性能管程在h=1.25mm时最好，壳程则在h=0.5mm时最好。引起这些变化的原因主要是由于随缩放节距与缩放肋高的增加，管程和壳程通道内的回流区不断增加，在回流区的增加造成阻力增加的同时，也改善了速度场与温度场的协同性，从而使二者的传热性能增强。最后将管程和壳程作为一个串联的整体进行综合考虑，得到整个换热器的综合传热性能在L=15mm，h=0.75mm时达到最佳，综合因子η=1.136-1.155（壳侧Re=27900-41900）。
以空气为工质，对缩放管间插入旋流片的管壳式换热器进行了单因素结构优化，经过第一轮优化后，得出换热器最佳尺寸参数为：缩放管节距L=28mm，肋高h=1.5mm，缩放比例ratioy=4.6，旋流片扭率y=3.33，旋流角度w=180°，旋流片间距Lp=896mm。在第一轮的优化研究基础上，又进行了第二轮结构优化，经过两轮的优化，最终得出换热器的最佳结构参数为：缩放管节距L=28mm，肋高h=1mm，缩放比例ratioy=4.6，旋流片扭率y=3.33，旋流角度w=180°，旋流片间距Lp=896mm。
Research on heat transfer enhancement of three different kinds of heat exchangers waspresented in this paper. They were annular-finned tube heat exchanger, self-supportedrectangle converging-diverging tube bundle heat exchanger, and shell and tube heat exchangerwith regularly spaced twisted tape inserted in shell side, respectively.
Experiments were performed for turbulent heat transfer and fluid flow characteristics ofannular-finned tube heat exchanger. The effects of three factors were examined: Re number,longitudinal tube spacing (Sl) and tube arrangements. Then3-D numerical simulations wereperformed to analyze the experimental results. The Reynolds number varied from4970to23620, and Slvaried from66mm to130mm. The tube arrangements were inline arrangementand staggered arrangement. It was found that Nusselt number and friction factor increasedwith the increase of Re for both inline and staggered arrangement, and the increasing trenddecreased. For inline arrangement, the heat transfer performance became better with theincrease of Sl, and it was the best when Slis110mm. However, it became worse with theincrease of Slfor staggered arrangement, and it was best when Slis66mm. Compared withinline arrangement, the heat transfer performance of staggered array was better. It was foundthat the effects of the three factors on the heat transfer performance of the annular-finned tubebanks can be well described by the field synergy principle, the area of recirculation region andthe wake vortex scale, i.e., the enhancement or deterioration of the heat transfer performancewas inherently related to the variations of the intersection angle between the velocity and thefluid temperature gradient, the area of recirculation region and the wake vortex scale.
Based on the new heat exchangers, self-support of rectangle converging-diverging(SS-RCD) tube bundle heat exchangers, three-dimensional numerical investigation wasperformed for turbulent heat transfer and fluid flow characteristics of the heat exchangers withdifferent inserts. The Reynolds numbers varied from27900to41900. The baselineconfiguration (without insert) was compared with four enhanced configurations (with inserts):Torus case, regularly spaced twisted-tape elements (RSTT) case, twisted tape (TT) case, andbaffle plate (BP) case. The inserts leaded to the variation of velocity distribution anduniformity of temperature. Compared with the baseline case, the air-side heat transfercoefficient of the four enhanced cases improved by16.69~24.32%,31.07~33.08%,28.32~33.13%, and38.01~46.74%, with an associated pressure drop penalty increase of74.02~89.5%,69.32~77.42%,54.35~65.74, and68.49~87.16%, respectively. The overallperformance was conducted by thermal enhancement factor. It is found that the BP case obtained the best overall performance, followed by TT case, RSTT case and Torus case, thebaseline case was the worst. The results indicated that the key point of enhancing heat transferof shell side is to improve the heat transfer performance on converging-diverging tube. Thenumerical results were analyzed from the view point of field synergy principle. It was foundthat the reduction in the average intersection angle between the velocity vector and thetemperature gradient was one of the essential factors influencing heat transfer performance.
Based on the above research,3-D numerical simulations were performed to get theoptimal structure of converging-diverging tube. The rib length (L) and height (h) wereexamined while retaining converging length ratio. The effects on heat transfer performance oftube side, shell side and whole heat exchanger were studied. The numerical results indicatedthat the smaller rib length and the larger rib height, the better the performance of heat transferand the greater the flow resistance for both shell side and tube side. Performance EvaluationCriteria (η) was adopted to evaluate the overall heat transfer performance. When L=16.5mm,η was the largest for shell side, while when L=9mm it was the largest for tube side. The riblength remained15mm was unchanged, the effect of rib height was examined. The overallheat transfer performance was best when h=0.5mm for shell side, while when h=1.25mmfor tube side it was the best. The reason is that the recirculation region increased withincreasing of rib length and height for both shell side and tube side. With the increasing ofrecirculation region, the friction in the channel increased. However, the recirculation regionreduced the average intersection angle between the velocity vector and the temperaturegradient, which was one of the essential factors influencing heat transfer performance. ThePerformance Evaluation Criteria of the total heat exchanger when the rib length was15mmand the rib height was0.75mm was η=1.136-1.155against the Reynolds number of shellside in the range of27900-41900as compared with the smooth tube bundle heat exchanger.
Optimization structure research of shell and tube heat exchanger with regularly spacedtwisted tape in shell side was performed. The working fluid was air, and the tube wasconverging-diverging tube. Single-factor method was adopted in this optimization process.Two rounds of numerical simulations were performed to find the best structure parameters ofthe heat exchanger. After the initial round of research, the optimization structure parameterswas L=28mm, h=1.5mm, ratio=4.6, y=3.33, and w=180°. Then, the second round of researchwas performed. After above research, the optimization structure parameters can bedetermined. The parameters were L=28mm, h=1mm, ratio=4.6, y=3.33, and w=180°.
通过实验得到Re、纵向管间距（Sl）及管束排列方式对圆形翅片管换热器传热性能的影响数据，再利用数值模拟的方法分析这三个因素影响的原因。Re变化范围为4970~23620，Sl为66mm到130mm，而管束排列方式则为顺排和叉排。Nu及f均随Re的增加而增加，且增加趋势逐渐下降。增大管间距会提高顺排的传热性能，但是提高幅度随间距的增加而减小，在Sl=110mm时换热效果最好；而叉排则不同，增大间距反而会降低换热器的传热性能，叉排的换热效果在Sl=66mm时是最好的。相对于顺排，叉排的换热效果要更好。对于换热器传热性能的提高可以从场协同与回流区面积及尾流涡尺度三个方面的变化来进行分析，寻找换热器结构改善的途径。
在新型换热器——矩形自支撑矩形缩放管换热器的基础上，利用三维数值模拟的方法对换热器插入不同的插入物后，其流道内流动及传热特性进行了研究，Re数的变化范围为27900~41900。四种不同插入物分别为：圆环、扭带、旋流片和折板，并将加入不同插入物后换热器的综合性能与无插入物时的性能做对比，得出的结论如下：与无插入物时相比，壳侧的传热系数在分别加入圆环、扭带、旋流片及折板后依次增加了16.69~24.32%，31.07~33.08%，28.32~33.13%，38.01~46.74%，传热性能的提升伴随着阻力的增加，四种情况下阻力分别增加了74.02~89.5%，69.32~77.42%，54.35~65.74和68.49~87.16%，在综合考虑传热性能与摩擦阻力两方面的因素后发现，加入插入物后换热器的综合传热性能由高到低依次为插入折板、插入扭带、插入旋流片、插入圆环，无插入物时的综合性能是最差的。通过研究发现，提升矩形自支撑换热器传热性能的关键在于提高换热器两侧区域的传热性能。利用场协同理论进行分析后发现，减小速度场与温度场之间的夹角有利于提高换热器的传热性能。
在自支撑矩形缩放管换热器内插物研究的基础上，利用三维数值模拟的方法分别研究在缩放段长度比例保持不变的情况下，缩放节距及缩放肋高对换热器管程、壳程及整体综合传热性能的影响，并得出缩放管的优化尺寸。研究表明：对于换热器管程和壳程，缩放节距L越小，换热效果越好，阻力也越大，壳程在L=16.5mm时综合传热性能达到最佳，而管程则在L=9mm时综合传热性能最好；缩放肋高h越大，二者的换热效果越好，阻力也由于管子的粗糙程度增加而变大，此时综合传热性能管程在h=1.25mm时最好，壳程则在h=0.5mm时最好。引起这些变化的原因主要是由于随缩放节距与缩放肋高的增加，管程和壳程通道内的回流区不断增加，在回流区的增加造成阻力增加的同时，也改善了速度场与温度场的协同性，从而使二者的传热性能增强。最后将管程和壳程作为一个串联的整体进行综合考虑，得到整个换热器的综合传热性能在L=15mm，h=0.75mm时达到最佳，综合因子η=1.136-1.155（壳侧Re=27900-41900）。
以空气为工质，对缩放管间插入旋流片的管壳式换热器进行了单因素结构优化，经过第一轮优化后，得出换热器最佳尺寸参数为：缩放管节距L=28mm，肋高h=1.5mm，缩放比例ratioy=4.6，旋流片扭率y=3.33，旋流角度w=180°，旋流片间距Lp=896mm。在第一轮的优化研究基础上，又进行了第二轮结构优化，经过两轮的优化，最终得出换热器的最佳结构参数为：缩放管节距L=28mm，肋高h=1mm，缩放比例ratioy=4.6，旋流片扭率y=3.33，旋流角度w=180°，旋流片间距Lp=896mm。
Research on heat transfer enhancement of three different kinds of heat exchangers waspresented in this paper. They were annular-finned tube heat exchanger, self-supportedrectangle converging-diverging tube bundle heat exchanger, and shell and tube heat exchangerwith regularly spaced twisted tape inserted in shell side, respectively.
Experiments were performed for turbulent heat transfer and fluid flow characteristics ofannular-finned tube heat exchanger. The effects of three factors were examined: Re number,longitudinal tube spacing (Sl) and tube arrangements. Then3-D numerical simulations wereperformed to analyze the experimental results. The Reynolds number varied from4970to23620, and Slvaried from66mm to130mm. The tube arrangements were inline arrangementand staggered arrangement. It was found that Nusselt number and friction factor increasedwith the increase of Re for both inline and staggered arrangement, and the increasing trenddecreased. For inline arrangement, the heat transfer performance became better with theincrease of Sl, and it was the best when Slis110mm. However, it became worse with theincrease of Slfor staggered arrangement, and it was best when Slis66mm. Compared withinline arrangement, the heat transfer performance of staggered array was better. It was foundthat the effects of the three factors on the heat transfer performance of the annular-finned tubebanks can be well described by the field synergy principle, the area of recirculation region andthe wake vortex scale, i.e., the enhancement or deterioration of the heat transfer performancewas inherently related to the variations of the intersection angle between the velocity and thefluid temperature gradient, the area of recirculation region and the wake vortex scale.
Based on the new heat exchangers, self-support of rectangle converging-diverging(SS-RCD) tube bundle heat exchangers, three-dimensional numerical investigation wasperformed for turbulent heat transfer and fluid flow characteristics of the heat exchangers withdifferent inserts. The Reynolds numbers varied from27900to41900. The baselineconfiguration (without insert) was compared with four enhanced configurations (with inserts):Torus case, regularly spaced twisted-tape elements (RSTT) case, twisted tape (TT) case, andbaffle plate (BP) case. The inserts leaded to the variation of velocity distribution anduniformity of temperature. Compared with the baseline case, the air-side heat transfercoefficient of the four enhanced cases improved by16.69~24.32%,31.07~33.08%,28.32~33.13%, and38.01~46.74%, with an associated pressure drop penalty increase of74.02~89.5%,69.32~77.42%,54.35~65.74, and68.49~87.16%, respectively. The overallperformance was conducted by thermal enhancement factor. It is found that the BP case obtained the best overall performance, followed by TT case, RSTT case and Torus case, thebaseline case was the worst. The results indicated that the key point of enhancing heat transferof shell side is to improve the heat transfer performance on converging-diverging tube. Thenumerical results were analyzed from the view point of field synergy principle. It was foundthat the reduction in the average intersection angle between the velocity vector and thetemperature gradient was one of the essential factors influencing heat transfer performance.
Based on the above research,3-D numerical simulations were performed to get theoptimal structure of converging-diverging tube. The rib length (L) and height (h) wereexamined while retaining converging length ratio. The effects on heat transfer performance oftube side, shell side and whole heat exchanger were studied. The numerical results indicatedthat the smaller rib length and the larger rib height, the better the performance of heat transferand the greater the flow resistance for both shell side and tube side. Performance EvaluationCriteria (η) was adopted to evaluate the overall heat transfer performance. When L=16.5mm,η was the largest for shell side, while when L=9mm it was the largest for tube side. The riblength remained15mm was unchanged, the effect of rib height was examined. The overallheat transfer performance was best when h=0.5mm for shell side, while when h=1.25mmfor tube side it was the best. The reason is that the recirculation region increased withincreasing of rib length and height for both shell side and tube side. With the increasing ofrecirculation region, the friction in the channel increased. However, the recirculation regionreduced the average intersection angle between the velocity vector and the temperaturegradient, which was one of the essential factors influencing heat transfer performance. ThePerformance Evaluation Criteria of the total heat exchanger when the rib length was15mmand the rib height was0.75mm was η=1.136-1.155against the Reynolds number of shellside in the range of27900-41900as compared with the smooth tube bundle heat exchanger.
Optimization structure research of shell and tube heat exchanger with regularly spacedtwisted tape in shell side was performed. The working fluid was air, and the tube wasconverging-diverging tube. Single-factor method was adopted in this optimization process.Two rounds of numerical simulations were performed to find the best structure parameters ofthe heat exchanger. After the initial round of research, the optimization structure parameterswas L=28mm, h=1.5mm, ratio=4.6, y=3.33, and w=180°. Then, the second round of researchwas performed. After above research, the optimization structure parameters can bedetermined. The parameters were L=28mm, h=1mm, ratio=4.6, y=3.33, and w=180°.
引文
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