圆形基管位置对于H型椭圆管翅片管束传热和流动特性影响

基于FLUENT软件,采用RNG k-ε湍流模型对H型椭圆翅片管束的传热与流动进行数值模拟,分析圆形基管位置对H型椭圆翅片管束的传热和流动的影响。结果表明:圆形基管位置往后移,翅片管束Nu减小,圆形基管处于第一排时,管束传热明显优于后三排位置,其Nu相较于第四排B4型翅片管束的Nu高16%,全椭圆基管A型翅片管束的Nu高15%。圆形基管位置后移,翅片管束f越小,但差别较小。在综合热力性能方面,圆形基管处于第一排时,管束表现最优。     

叉排板束换热器传热特性数值研究

为提高换热器的传热性能,设计了叉排板束换热器,利用Fluent软件中的RNG k-ε模型数值研究了叉排板束的传热特性。分析了叉排板束排数对于整体Nu的影响以及板束的局部传热特性,比较了不同横纵比对整体Nu的影响,并给出不同Re下叉排板束的Nu经验公式。实验结果表明：叉排板束整体传热性能随板排数的增多而增强,当达到一定排数后传热性能趋于稳定,不同Re下趋于稳定的排数不同,当Re=4.3×105时进入稳定阶段需13排,当Re=4.3×103时进入稳定阶段仅需7排;叉排板束局部传热性能在各板排中先增大后减小,在第2~4排局部Nu达到峰值,板的局部传热性能在两个直角处以及撞击点位置大大增强;板束在横纵比为5时传热性能最佳,横纵比大于或小于5时,传热性能均会减弱;给出Re在1~500,500~1 000,1 000~200 000范围内板束整体Nu拟合公式,当Re>30 000时,与叉排圆管束相比,叉排板束传热性能提高25%     

空冷凝汽器椭圆翅片椭圆管束外空气的流动与传热特性

研究空冷凝汽器椭圆翅片椭圆管管束外空气的流动与传热特性,对火电站空冷岛的设计与运行具有重要意义.通过CFD模拟,获得了椭圆翅片椭圆管管束外冷却空气的流场和温度场,计算得到了空冷凝汽器冷却空气对流换热平均Nu和摩擦系数f随Re的变化规律,并采用最小二乘法拟合得到了相应的关联式.结果表明:随冷却空气流动Re的增大,Nu增大,f减小.     

H形翅片管束传热和阻力特性的试验与数值模拟

根据大型电站锅炉省煤器的运行工况,对单H形和双H形翅片管束气侧的传热与阻力特性进行了模化试验研究,并利用Fluent软件对H形翅片管束的流场和温度场进行了数值模拟,得到单H形和双H形翅片管束的传热与阻力特性变化规律.结果表明:H形翅片管束的传热和阻力特性与气体的Re有关,随着气体Re的增大,气侧Nu不断增大,传热性能提高,而Eu则逐渐减小,并趋于定值;在相同Re下,单H形翅片管束气侧Nu大于双H形翅片管束气侧Nu,而气侧Eu则小于双H形翅片管束气侧Eu;数值计算结果与试验结果误差较小,采用数值计算方法能比较准确地分析H形翅片管束的流动与传热特性.     

热流对考虑自然对流吸热管内熔盐对流传热影响

以熔盐为传热工质,对考虑自然对流条件下吸热管内熔盐的流动与传热进行了数值研究。结果表明:均匀热流下自然对流促进管内下侧和熔盐向管中心流动,弱化管内上侧熔盐向管中心流动;吸热管内下侧Nu数大于上侧Nu数,管内最大Nu数出现在底部,最小Nu数出现在顶部,吸热管内下侧Nu数与上侧Nu数的差值随着Re数增大而减小,但其平均Nu数变化较小,且其平均Nu数与不考虑自然对流影响的管内平均Nu数基本相等。非均匀热流下吸热管加热的上下位置对吸热管内单侧Nu数影响较大,但对平均Nu数无影响。同一Re数,吸热管上侧Nu数随着热流增高而最小。     

膜片管通道流动与换热过程的数值模拟

采用SIMPLE算法模拟膜片管通道中的流动与换热,分析流场中出现的非线性现象以及不同管束排列方式对换热的影响。物理模型长度为185. 6 mm,高度为92. 8 mm,圆管直径为32 mm。烟气入口温度为400 K,上下两侧固体壁面温度为300 K。假设流动与换热进入充分发展阶段,雷诺数(Re)的取值范围是3 000～25 000,通入不同流速的烟气与两侧的壁面进行换热。结果表明:采用雷诺应力模型(RSM)所得的努塞尔数(Nu)与实验关联式结果最吻合,而且相对误差在5%～17%间;采用直接模拟(DNS)模拟时,稳态到非稳态的临界Re是100;在同一Re时,随着管间距减小,Nu是逐渐增加的,当Re取为25 000,管束水平间距和竖直间距均取为43. 2 mm时,通道换热能力达到最大且相应的Nu是195. 23。     

高粘度流体横掠麻面管的传热与流动特性研究

采用三维数值模拟方法,研究不同Re(381、572、763、954、1144)下凹坑直径d(1.8、2.0和2.2 mm)、深度h(0.9、1.0和1.1 mm)、轴向距离p(10、12和14 mm)、周向距离l(5.236、6.283和7.854 mm)与布置型式(叉排、顺排)对高粘度润滑油横掠麻面管流动与传热的影响。结果表明:外壁周期性凹坑的存在使得麻面管油侧换热增强,同时减阻效果明显;相比于光管,当Re=381～1 144时,麻面管油侧Nu增加了28.6%～55.4%,阻力系数f减小了0.59%～26.9%,综合换热性能指标η为1.05～1.59。     

管间距对开缝翅片管换热器传热与阻力特性的影响

为了获得管间距对开缝翅片管换热器传热与阻力特性的影响规律,对5种不同翅片管换热器进行了数值模拟研究,并进行了模化试验验证。结果表明:开缝翅片管束的传热和阻力特性与翅片侧气体的Re数有关,随着Re数增大,翅片侧Nu数增大,摩擦因子f逐渐减小;纵向间距S2对开缝翅片管换热器的综合流动传热性能的影响较大。数值模拟与试验结果偏差较小,采用数值模拟方法能够比较准确地分析开缝翅片管换热器的传热与阻力特性。     

螺旋管内水和蒸汽局部传热特性研究

以高温气冷堆蒸发器为背景,采用FLUENT软件模拟了单相水和蒸汽在不同尺寸螺旋管内部的流动和传热过程,研究了壁面局部传热特性。计算结果表明,远离螺旋中心线一侧局部传热较强而靠近螺旋中心线一侧传热较弱,壁面Nu周向分布非常不均匀。管径与螺旋直径之比是主要影响因素,当其值增大时截面温度极值点向螺旋中心线外侧移动,加剧了温度分布和Nu分布的不均匀性。在层流向湍流过渡区内,Re的增大使截面各点温度梯度均有所增加,同时也增大了Nu周向分布的不均匀程度,但在旺盛湍流区内Re对Nu分布无明显影响。壁面热边界条件形式对局部Nu周向分布没有显著影响。给出了局部Nu的估算式。     

圆管内置涡流发生器强化传热数值模拟

恒壁温条件下,采用RNG k-ε湍流模型的增强壁面处理(EWT),对圆管内置一种新涡流发生器雷诺数(Re)在25953～51906范围内的流体流动及传热特性进行数值模拟。通过计算努塞尔数(Nu)、摩擦阻力系数(f)与综合性能评价指标(PEC),分析涡流发生器的强化传热性能;得到横截面速度场、温度场及流线图分析强化传热形成原因。结果表明:同一Re,涡流发生器数量越多Nu越大、偏心安装Nu大于中心安装、顺置安装Nu大于倒置安装,同时考虑压力损失,发现偏心安装具有最优的强化传热性能;在涡流发生器附近,流体流速变大,同时涡流发生器产生2层旋流和涡流对壁面形成冲刷作用,破坏传热边界层,并使壁面不易结垢,达到强化传热和自清洁的双重效果。     

Convective Heat Transfer and Pressure Drop over Elliptical and Flattened Tube

A numerical study on the effect of the effect of elliptical and flattened tube bundle geometry on the convective heat transfer and pressure drop is presented in this article. The analysis has been carried out to evaluate the performance of these bundle geometries in the design of a compact and effective single phase shell and tube heat exchanger. The temperature, velocity, and pressure drop profiles are obtained from solving the mass, momentum, and energy conservation equations. The comparison is made for inline and staggered bundle with different pitch to diameter ratio and inlet velocity for elliptical and flattened tubes. The pitch to diameter ratio is varied from 1.25 to 2.5 for Reynolds number ranging from 200 to 2000 which is in the laminar flow region. The heat transfer coefficient over the staggered and inline tube bundle decrease with an increase in pitch. The same kind of variation is also observed for the pressure drop in the case of both elliptical and flattened tube bundle. The study shows that the transverse pitch with respect to cross flow affects more than the longitudinal pitch.     

Experimental Investigation on Flow Boiling Heat Transfer and Pressure Drop of HFC-134a inside a Vertical Helically Coiled Tube

An investigation on flow boiling heat transfer and pressure drop of HFC-134a inside a vertical helically coiled concentric tube-in-tube heat exchanger has been experimentally carried out. The test section is a six-turn helically coiled tube with 5.786-m length, in which refrigerant HFC-134a flowing inside the inner tube is heated by the water flowing in the annulus. The diameter and the pitch of the coil are 305 mm and 45 mm, respectively. The outer diameter of the inner tube and its thickness are respectively 9.52 and 0.62 mm. The inner diameter of the outer tube is 29 mm. The average vapor qualities in test section were varied from 0.1 to 0.8. The tests were conducted with three different mass velocities of 112, 132, and 152 kg/m²-s. Analysis of obtained data showed that increasing of both the vapor qualities and the mass fluxes leads to higher heat transfer coefficients and pressure drops. Also, it was observed that the heat transfer coefficient is enhanced and also the pressure drop is increased when a helically coiled tube is used instead of a straight tube. Based on the present experimental results, a correlation was developed to predict the flow boiling heat transfer coefficient in vertical helically coiled tubes.     

Heat transfer on tube bundles embedded horizontally in a liquid‐fluidized bed: 2nd report: On tube bundles of fundamental layouts including in‐line layouts

Heat transfer coefficients were measured on tube bundles of fundamental layouts including in‐line layouts embedded horizontally in a liquid‐fluidized bed. Tested tube layouts were single tubes, transverse single tube rows, longitudinal single tube rows, and in‐line arranged tube bundles. A total of 7 kinds of particles were used. Comparisons of the experimental data showed a good agreement with the heat transfer correlation developed for staggered layouts, when the average liquid velocity through each tube bundle was used as the reference velocity for the particle Reynolds number. Distribution of the local heat transfer coefficient was also investigated around tubes. © 2009 Wiley Periodicals, Inc. Heat Trans Asian Res; Published online in Wiley InterScience ( www.interscience.wiley.com ). DOI 10.1002/htj.20245     

Numerical evaluation of a heat exchanger with inline tubes of different size for reduced fouling rates

This paper describes the numerical evaluation of a novel cross flow tube bundle heat exchanger that combines tubes of different diameter in an inline arrangement for the purpose of reducing gas side particulate fouling rates while preserving acceptable levels of heat transfer and pressure drop performance. Three arrangements are compared: a common inline tube bundle heat exchanger with cylinders of equal diameter and two other arrangements that consist of alternately placed cylinders with a diameter ratio of d/D = 0.5, at two different transverse spacings. Numerical calculations are performed in order to study heat transfer, pressure drop and fouling rates from flue gases with suspended ash particles. The alternating tube sizes achieve a suppression of the vortex shedding mechanism that has previously been shown to enhance downstream particle deposition. Results show that, compared to the standard arrangement, the tube bundle with unequal cylinders placed at the largest transverse spacing achieves a significant (～30%) reduction in particle deposition rate without sacrificing acceptable values of heat transfer per unit volume and low pressure drop.     

Enhanced Boiling Outside 8 × 3 Plain and Coated Tube Bundles

Experiments were conducted for pool boiling on the outside of 8 × 3 (eight rows and three columns) plain and coated tube (surface roughness = 8.279 μm) bundles for three different pitch distances with the distinct objective to study the behavior and the enhancement of boiling heat transfer in horizontal staggered tube bundles (of plain and coated tubes for different equilateral triangular arrangements) with heat flux values ranging from ～12 to 45 kW/m². At higher heat fluxes, coated and plain tube bundles had almost similar bundle average heat transfer coefficients at a given pitch distance, while at lower heat fluxes, the coated tube bundles have higher bundle average heat transfer coefficients as compared to that of the plain tube bundle. The coated tube bundles with the minimum pitch to diameter ratio of 1.4 exhibited the maximum bundle average heat transfer coefficients. The present study concludes that the bundle factor needs to be considered in the design of flooded evaporators.     

Air side performance at low Reynolds number of cross-flow heat exchanger using crimped spiral fins

A total of 23 cross-flow heat exchangers having crimped spiral configurations is studied. The effect of tube diameter, fin spacing, transverse tube pitch, and tube arrangements are examined. For the inline arrangement, the pressure drop increases with the rise of tube diameter but the associated heat transfer coefficient decreases with it. The increase of fin height also gives rise to considerable increase of pressure drop and decrease of heat transfer coefficients for the inline arrangement. However, for the staggered arrangement, the effect of the fin height on the pressure drop is much smaller than that of the inline arrangement due to the major contribution to the total pressure drops from the blockage of the airflow from staggered arrangement. Effect of the fin spacing on the air side performance is strongly related to the transverse tube pitch for both inline and staggered arrangements. Correlations of the present crimped spiral fins in both staggered and inline arrangements are developed. The proposed correlations give fairly good predictive ability against the present test data.     

Heat transfer and pressure loss penalty for the number of tube rows of staggered finned-tube bundles with a single transverse row of winglets

The objective of this research is to investigate the heat transfer and pressure loss penalty for various numbers of transverse rows in staggered finned-tube bundles with a single transverse row of the winglet pairs beside the front row of the tube bundles. Experiments were performed for two, three, four and five rows of staggered tube bundles. The pairs of winglets were placed with a heretofore-unused orientation for the purpose of augmentation of heat transfer and reduction of pressure loss penalty. This orientation is called as “common flow up” configuration. For three rows of tubes with a single transverse row of winglets beside the front row of the tubes, the heat transfer was augmented by 30-10%, and yet the pressure loss was reduced by 55-34% with the increase of the Reynolds number (based on two times channel height) from 350 to 2100. The reduction of the pressure loss penalty for three rows of tube bundles is the largest in comparison with the other numbers of rows.     

Turbulent heat transfer in a horizontal helically coiled tube

An experiment has been conducted in detail to study the turbulent heat transfer in horizontal helically coiled tubes over a wide range of experimental parameters. We found that the enhancement of heat transfer in the coils results from the effects of turbulent and secondary flows. With Reynolds number increasing to a high level, the contribution of the secondary flow becomes less to enhance heat transfer, and the average heat transfer coefficient of the coil is closer to that in straight tubes under the same conditions. The local heat transfer coefficients are not evenly distributed along both the tube axis and the periphery on the cross section. The local heat transfer coefficients on the outside are three or four times those on the inside, which is half of the average heat transfer. A correlation is proposed to describe the distribution of the heat transfer coefficients at a cross section. The average cross-section heat transfer coefficients are distributed along the tube axis. The average value at the outlet section should not be taken as the average heat transfer coefficient. © 1999 Scripta Technica, Heat Trans Asian Res, 28(5): 395–403, 1999     

Prediction of thermal and fluid flow characteristics in helically coiled tubes using ANFIS and GA based correlations

This study introduces the ability of Adaptive Neuro-Fuzzy Inference System (ANFIS) and genetic algorithm (GA) based correlations for estimating the hydrodynamics and heat transfer characteristics in coiled tubes. The experimental data related to the heat transfer and pressure drop in helically coiled tubes with deferent geometrical parameters (coil diameter and pitch) were used. In the experiments, hot water was passed in the coiled tubes, which were placed in a cold bath. Two ANFIS models were developed for predicting the Nusselt number (Nu) and friction factor (f) in the coiled tubes and the geometric parameters were employed as input data. Moreover, empirical correlations for estimating the Nu and f were developed by a phenomenological argument in the form of classical power–law correlations and their constants were found using the GA technique. The mean relative errors (MRE) of the developed ANFIS models for estimation of Nu and f are 6.24% and 3.54%, respectively. On the other hand, for empirical correlations, a MRE of 8.06% was found for prediction Nu while MRE of 5.03% was obtained for f. The results show that the ANFIS models can predict Nu and f with the higher accuracy than the developed correlations.     

Numerical and experimental investigations of heat transfer performance of rectangular coil heat exchangers

Both numerical and experimental investigations were conducted to understand convective heat transfer from a single round pipe coiled in rectangular pattern. The studied heat exchangers are composed with inner and outer coils so that the exterior flow is very similar to flow within tube-bundles. The inner and outer coils of the heat exchangers are in turn composed of bends and straight portions. Calculations and experiments were done for two cases with different outside flow arrangements. The results showed the effects of geometric arrangement with better heat transfer for the case 1 of staggered arrangement due mainly to its more tortuous flow characteristics and better mixing of the exterior fluid. The numerical and experimental results qualitatively agree well with each other. The numerical and experimental results showed that coiling a pipe so that an exterior fluid flows over or in tube bundle can help to induce the turbulence without increasing the velocity.