周向非均匀热流下吸热管熔盐传热数值研究

在塔式太阳能光热发电技术中,非均匀受热吸热管内熔盐流动与传热过程是光-热能量转换的关键环节。建立了周向非均匀加热的吸热管物理模型,通过Fluent软件开展数值计算。采用标准的k-ε,RNG湍流模型求解三维流动N-S方程及能量方程,获取吸热管内熔盐传热特性。结果表明,吸热管周向壁温和努赛尔数呈现明显的非均匀分布特性。对比了数值结果与经验公式计算结果,建议采用Gnielinski公式计算周向非均匀加热条件下吸热管内熔盐对流传热。     

高温熔盐吸热器的传热研究和系统设计

本文对非均匀辐射热流密度太阳能熔盐吸热器传热过程进行了模拟研究,得到了熔盐吸热器内部的温度、传热性能等特征参数。结果表明在轴向和径向上熔盐流体温度和管壁的温度都非常不均匀,同时其综合传热性能要高于按照Sieder-Tate公式的计算值。并对10 MW塔式太阳能热发电的熔盐吸热器进行了设计和分析。     

太阳入射热流对吸热器换热的影响

空间太阳能热动力发电系统是非常有前景的未来空间能源供应系统。吸热器的入射热流分布将影响到换热管的传热以及系统的寿命，采用焓法处理相变区的传热，建立了太阳能热动力发电系统吸势器换热管三维换热模型，计算得到在轨道周期内对应三种入射热流的换热管的温度场、工质的出口温度变化、相变材料熔化率等重要的结果，并进行了比较、分析。     

半周加热半周绝热的熔盐吸热管传热特性研究

建立了描述半周加热、半周绝热的不均匀热流边界条件下熔盐吸热管内热传导与热对流换热的数值模型,模型考虑了管壁导热和熔盐的变物性.采用Fluent软件,通过求解三维N-S方程和能量方程,对熔盐吸热管的传热过程进行了模拟,并在熔盐吸热传热实验平台上进行了试验研究.模拟计算与实验结果基本一致.揭示了熔盐吸热管在高温、高热流密度条件下的管内流速和温度分布规律及其换热特性,为塔式太阳能热发电熔盐吸热器的设计和运行控制提供了重要依据.     

混合气体管内对流凝结传热研究

研究了混合气体在垂直圆管内的对流凝结传热。利用修正的膜模型与Nusselt凝结理论建立了换热数学模型，预测了壁面温度对膜厚度和界面温度的影响，计算了凝结液膜厚度，并与报相热阻法进行比较，研究结果表明该模型更接近实验果，提出了混合气体对流凝结换热与Nusselt凝结的不同。     

聚光太阳能吸热管的吸热传热特性

基于太阳能选择性吸收涂层的辐射性能,建立聚光太阳能吸热管光热耦合传输的数理模型,理论研究聚光太阳能吸热管的吸热传热特性。研究表明,吸热管壁温度随着聚光能流密度增加而线性升高,而吸热效率在中等聚光能流密度时达最大值。太阳能选择性吸收涂层性能对吸热传热有重要影响,具有低红外发射系数涂层的系统吸热效率明显较高,而红外辐射能量损失率则在中等聚光能流密度时最小。管内强迫对流可以显著提高吸热管效能,吸热效率随流速增加而提高,而管壁温度则显著下降。     

柴油机非水冷却介质自然对流沸腾传热特性的研究

对于采用非水冷介质的高温冷却水及少冷却柴油机的研究，目前尚需了解冷却介质温度的提高，及冷却介质的性质差异，对柴油机的传热及零部件热状况的影响。本模拟柴油机工作条件，对机油，柴油及不同配比的乙二醇水溶液等液体的自然对流沸腾热特性进行了试验研究，揭示了各种因素对传热的影响，通过对试验数据的回归分析得出了３种非水冷却介质自然对流沸腾传热关系式。     

竖管内空气强迫与自然对流换热实验

对竖直圆管内空气强迫对流换热与自然对流换热进行了实验，从量级上表明了两者的不同，由实验得到了用雷诺数表示的自然对流换热关联式，与现有的大空间自然对流换热公式作了比较。     

柴油机非水冷却介质自然对流沸腾传热特性研究

对于采用非水冷介质的高温冷却及少冷却柴油机的研究，目前尚需了解冷却介质温度的提高及冷却介质的性质差异，对柴油机的传热及零部件热状况的影响。本文模拟柴油机工作条件，对机油、柴油及不同配比的乙二醇水溶液等液体的自然对流沸腾传热特性进行了试验研究，揭示了各种因素对传热的影响，通过对试验数据的回归分析得出了３种非水冷却介质自然对流沸腾传热关系式。为机油、柴油及乙二醇水溶液用于柴油机高温冷却及少冷却提供了理论依据。     

Bounds on natural convective heat transfer in a porous layer with fixed heat flux

Using the background field variational method, bounds on natural convective heat transfer in a porous layer heated from below with fixed heat flux are derived from the primitive equations. The enhancement of heat transfer beyond the minimal conduction value (the Nusselt number Nu) is bounded in terms of the non-dimensional forcing scale set by the ‘effective’ Rayleigh number (Rˆ) according to Nu ≤ 0.354Rˆ^1/2 and in terms of the conventional Rayleigh number (Ra) defined by the temperature drop across the layer according to Nu ≤ 0.125Ra. It is presented that fixing the heat flux at the boundaries does not change the linear dependence between Nusselt number and Rayleigh number at high Rayleigh number region.     

Effect of fins on forced convection heat transfer around a tube

Effect of fins on heat transfer around a tube was investigated experimentally. A test tube of 30 mm diameter was installed in a test section of an open‐type wind tunnel as a single tube, or as a center tube in a single tube row and in a tube bundle of staggered layout. Fins made of paper were put on the test tube having certain fin spacing. It was clarified from the experiment that the local heat transfer coefficient around the tube degrades with decreasing fin spacing, especially on the downstream side of the tube, and the minimum fin spacing where the effect of the fin begins to appear is the largest for the single tube and the smallest for the tube bundle. © 2003 Wiley Periodicals, Inc. Heat Trans Asian Res, 32(5): 445–454, 2003; Published online in Wiley InterScience ( www.interscience.wiley.com ). DOI 10.1002/htj.10098     

Radiant and convective heat transfer for flow of a transparent gas in a short tube with sinusoidal wall heat flux

The present analysis accounts for combined convective and radiant heat transfer to a fluid flowing in a short tube with prescribed wall heat flux. The heat flux distribution used was of sine shape with maximum at the middle of the tube. This solution is known to represent the axial power variation in a nuclear reactor core. The tube wall and gas bulk temperatures were obtained by successive substitutions for the wall and gas energy balance equations. The integrals were approximated by Sympson's rule and initial guesses for the iterative process were based upon limiting cases for pure radiation and pure convection. The results of the combined solution compared with the pure radiation approach show a decrease of 30 percent for the maximum wall temperature using black surface ($\text{ε=1}$). For this same situation, the increase in the gas temperature along the tube shows a reduction of 58 percent when compared to the pure convection solution.     

Influence of helical tube dimensions on open channel natural convection heat transfer

Natural convection heat transfer of a helical tube was investigated experimentally for varying tube diameter, length, height, pitch, radius, and number of turns, in order to determine an appropriate characteristic length to describe the phenomenon. Mass-transfer rates of a CuSO₄–H₂SO₄ electroplating system were measured by replacing the heat transfer system according to the analogy concept. When the pitch-to-diameter ratio was larger than 5 and the pitch-to-radius ratio was smaller than 2.3, the heat transfer rates were very close to those of a horizontal cylinder, and decreased with the diameter of the tube while remaining unaffected by the total length and height. The natural convection heat transfer of the Nth turn of a helical tube was measured for varying pitch-to-diameter ratio and number of turns, and the results were formulated as an empirical correlation.     

Laminar Natural Convective Heat Transfer in the Enclosed Evacuated Collector Tube with East—West Symmetric Heat Input

INTR0DUCTI0NNaturalconvectioninenclosureshasbeenfoundinavariety0fapplications,suchassolarcollectors,nu-cleartechn0logies,thecoolingofelectronicalcircuits,etc.Amongthemnaturalconvectioninsideanen-closedrectangularcavityisthemostclassicalproblem.Correspondinglyagreatdealofexperimentalandnumericalworkhasbeendoneinsuchafieldwiththe"clean"boundaryCPnditi0nsofuniformwalltem-perature(UWT)anduniformheatflch(UHF).Re-celltlymoreattelltionispaidontheconvectioninthecirculartube.HwangandLai[11inves…     

Exergy transfer characteristics of forced convective heat transfer through a duct with constant wall heat flux

The examination of exergy transfer characteristics caused by forced convective heat transfer through a duct with constant wall heat flux for thermally and hydrodynamic fully developed laminar and turbulent flows has been presented. The exergy transfer Nusselt number is put forward and the dependence relationships of the exergy transfer Nusselt number on the heat transfer Nusselt number, Reynolds number and Prandtl number are obtained. Expressions involving relevant variables for the local and mean convective exergy transfer coefficient, non-dimensional exergy flux and exergy transfer rate, etc. have been derived. By reference to a smooth duct, the numerical results of exergy transfer characteristics for fluids with different Prandtl number are obtained and the effect of the Reynolds number and non-dimensional cross-sectional position on exergy transfer characteristics is analyzed. In addition, the results corresponding to the exergy transfer and energy transfer are compared.     

Second law optimization of convective heat transfer through a duct with constant heat flux

A second law analysis is carried out on convective heat transfer from a fluid flowing in a duct with constant heat flux. The entropy generated is expressed as a function of the initial temperature difference and the frictional pressure drop. Since the loss in available energy is directly proportional to the entropy generated, an optimum value of the initial temperature difference is found where the entropy generated is the minimum. A similar optimum is found for the ratio of heat transfer to pumping power. An optimum fluid velocity which corresponds to the minimum loss of available power is recommended.     

Coupled heat and mass transfer in natural convection under flux condition along a vertical cone

Concentration induced buoyancy forces superimposed on thermally induced ones, in flows generated adjacent to a vertical cone are studied analytically. The surface of the cone is subjected to uniform mass and/or heat flux. Numerical results are presented for the diffusion of common species into air when concentration buoyancy forces assist as well as oppose thermal buoyancy forces. The local Nusselt number and the local wall shear stress are found to increase and decrease as the buoyancy force from species diffusion aids or opposes, respectively, the thermal buoyancy force. The local Sherwood number increases with the increase of the thermal buoyancy force. At high Schmidt numbers tangential mass flow rates reach constant asymptotic values of increasing magnitude with the increase of the buoyancy force ratio.     

Modeling of forced convective heat transfer of a non-Newtonian nanofluid in the horizontal tube under constant heat flux with computational fluid dynamics

In this paper, convective heat transfer effect on the non-Newtonian nanofluid flow in the horizontal tube with constant heat flux was investigated using computational fluid dynamics (CFD). For this purpose, non-Newtonian nanofluid containing Al₂O₃ and Xanthan aqueous solution as a liquid single phase with two average particle sizes of 45 and 150 nm and four particle concentrations of 1, 2, 4 and 6 wt.% and two concentrations of Xanthan aqueous solutions (0.6,1.0 wt.%) were used. Effect of particle size and concentration of Xanthan solution on convective heat transfer coefficient was investigated in different Reynolds numbers (500 < Re < 2500) for various axial locations of tube. The results showed that heat transfer coefficient and Nu number of non-Newtonian nanofluid increased with increasing concentration of Xanthan solution. By applying the modeling results, an equation was obtained for Nusselt number prediction using the dimensionless numbers. The results showed that the correlated data were in very good agreement with predicted data. The maximum error was around 5%.     

An analytical study of pulsating laminar heat convection in a circular tube with constant heat flux

Pulsating laminar convection heat transfer in a circular tube with constant wall heat flux is investigated analytically. The results show that both the temperature profile and the Nusselt number fluctuate periodically about the solution for steady laminar convection, with the fluctuation amplitude depending on the dimensionless pulsation frequency, ω*, the amplitude, γ, and the Prandtl number, Pr. It is also shown that pulsation has no effect on the time-average Nusselt numbers for pulsating convection heat transfer in a circular tube with constant wall heat flux.