大型速冻设备蒸发器高效传热技术的试验研究

不同结构型式蒸发器的传热系数不同,选择7种不同结构的蒸发器模型,分析比较翅片形状、管径大小以及管子排列方式对蒸发器传热系数的影响,得出在不结霜工况下,传热系数最高的蒸发器结构是连续整体带波纹翅片叉排变节距结构的结论。对这种结构的蒸发器进行试验测试,得到与理论计算相符的传热系数值。     

Averaged heat transfer during periodic fluctuations of the heat transfer intensity of the surface of a plate,a cylinder,or a sphere

Processes of heat transfer with periodically varying intensity on the surface of heated bodies of three typical geometries (plate, cylinder, sphere) are considered. The true heat transfer coefficient, which varies in time by the law of a periodic step function having two free parameters — amplitude and asymmetry, is specified on the heat transfer surface. Resultant relations are obtained for calculating the experimental heat transfer coefficient, which is the quantity measured in a traditional heat transfer experiment and used in applied calculations.Moscow Power Engineering Institute. Translated from Inzhenerno-Fizicheskii Zhurnal, Vol. 68, No. 2, pp. 225–228, March–April, 1995.     

R134a单元式风冷冷风空调机蒸发器设计

以理论模型为基础，对R134a单元式风冷冷风机组翅片管式蒸发器进行设计。应用管内流动沸腾换热模型仿真分析R134a的质量流量对沸腾换热的影响，利用外掠翅片管束换热关联式计算管外翅片侧表面换热系数，进而得出翅片管蒸发器总传热系数，利用计算结果进行设计。     

Observations on the characteristics of a fluidized bed for the thermal shock testing of brittle ceramics

The heat transfer characteristics of a fluidized bed used as a quenching medium for the thermal stress testing of brittle ceramics, were determined by measurements of the thermal shock behaviour of rods of a soda-lime—silica glass. The heat transfer coefficient was found to be strongly dependent on the mean particle size of the powder and air flow rate, and was relatively independent of the position within the bed. The results indicate that the heat transfer coefficient during thermal shock fracture may have a value lower than that obtained under heat transfer conditions which more closely resemble steady state. The heat transfer data inferred from the quenching experiments with the glass gave excellent agreement between calculated and measured values for the thermal shock behaviour for rods of a polycrystalline aluminium oxide. It is concluded that fluidized beds are excellent inert quenching media with variable heat transfer coefficient controlled by particle size and flow rate.     

Development of a slug flow absorber working with ammonia–water mixture: part II—data reduction model for local heat and mass transfer characterization

This study deals with a data reduction model for clarifying experimental results of a counter-current slug flow absorber, working with ammonia–water mixture, for significantly low solution flow rate conditions. The data reduction model to obtain the local heat and mass transfer coefficient on the liquid side is proposed by using the drift flux model to analyze the flow characteristics. The control volume method and heat and mass transfer analogy are employed to solve the combined heat and mass transfer problem. As a result, it is found that the local heat and mass transfer coefficient on the liquid side of the absorber is greatly influenced by the flow pattern. The heat and mass transfer coefficient at the frost flow region is higher than that at the slug flow region due to flow disturbance and random fluctuation. The solution flow rate and gas flow rate have influence on the local heat and mass transfer coefficient at the frost flow region. However, it is insignificant at the slug flow region.     

Heat transfer in a subcooled evaporating liquid film

An investigation is performed of heat transfer in films of water and FC-72 liquid falling down a 60×120 mm heater. Heat transfer mode maps are constructed. Zones of structure formation and regions of emergence of breakdown of liquid film are identified, as well as regions of boiling in jets. An averaged coefficient of heat transfer was used in analyzing the experimental data. It is demonstrated that thermocapillary forces have a complex and ambiguous effect on heat transfer. The emergence of extensive stable dry spots causes a decrease in the average coefficient of heat transfer. On the other hand, an increase in the path length of film and in the amplitude of wave motion leads to the washing out of the dry spots and to an increase in the relative intensity of heat transfer. The regularities of heat transfer in the region of flow of film with breakdowns for weakly and intensely evaporating liquids differ significantly. An enhancement of heat transfer is observed under conditions of significant evaporation during structure formation in the thermocapillary mode.     

Heat transfer coefficient during two-phase flow boiling of HFC-134a

This paper reports a study of the evaporation of HFC-134a inside smooth, horizontal tubes. Tests were performed with the pure refrigerant and with oil-refrigerant mixtures. The heat flux was varied from 2 to 10 kW m⁻². The inner diameter of the tubes was 12 mm. Two evaporators were used, 4 and 10 m long, and the oil content was varied from 0 to 2.5 mass percentage (synthetic oil, EXP-0275). Oil-free HFC-134a had a higher heat transfer coefficient than HCFC-22 at the same heat and mass fluxes. The effect of oil in the refrigerant is dependent on the heat flux. At 2 and 4 kW m⁻² the heat transfer coefficient had a maximum value for an oil content of around 0.5 mass percentage; no increase is registered for a heat flux of 6 kW m⁻². The heat transfer coefficients for the pure refrigerant were also compared with two existing correlations. The measured heat transfer coefficients averaged over the evaporator deviate less than 40% from the correlation according to Pierre. The heat transfer coefficients at the short evaporator lie within 20%. The correlation given by Jung overestimates the heat transfer coefficient by approximately 50%.     

Heat transfer and pressure drop of HFC134a-oil mixtures in a horizontal condensing tube

The paper reports the results of condensation heat transfer and pressure drop from tests with pure and oil-contaminated refrigerant HFC134a in a horizontal tube (10 m in length, 6 mm ID). The experimental results are compared with prediction from correlation. The heat transfer coefficient in the case of oil-contaminated refrigerant is shown to depend strongly on the definition of the saturation temperature. Using the pure refrigerant saturation temperature (hence disregarding the influence of oil on the vapour pressure), the results for average heat transfer coefficient show only minor effect of the oil contents. If the saturation temperature of the refrigerant—oil mixture is used, there is thus a significant degradation of the heat transfer coefficient (as expected) with increasing oil concentrations.     

Condensation of R407C in a horizontal microfin tube

This paper describes experimental results that show the effects of mass velocity and condensation temperature difference on the local heat transfer characteristics during condensation of R407C in a horizontal microfin tube. The experiments were performed at the saturation temperature of 40 °C, the refrigerant mass velocity of 50, 100, 200 and 300 kg m⁻² s⁻¹, and the condensation temperature difference of 1.5, 2.5 and 4.5 K. A superficial heat transfer coefficient for the vapor phase was obtained by subtracting the heat transfer resistance of condensate film estimated by using a previously developed theoretical model of film condensation of pure vapor from the overall heat transfer resistance. On the basis of the analogy between heat and mass transfer, an empirical equation for the superficial vapor phase heat transfer coefficient was developed. The heat transfer coefficient predicted by the combination of the previously developed theoretical model of film condensation of pure vapor and the empirical equation of the superficial vapor phase heat transfer coefficient agreed with the measured values with the r.m.s. error of 9.2%.     

Condensation of pure refrigerants R12, R134a and their mixtures on a horizontal tube with capillary structure: An experimental study

We experimentally studied free convection condensation heat transfer of pure refrigerants R12, R134a, and their mixtures on a horizontal single tube. Approximately equimolar mixtures of these refrigerants are azeotropic. The outside surface of the tube used had a capillary structure. The tube was integrated in an experimental set-up in a way that allowed its rotation around the axis. Movable thermocouples inserted in the tube wall enabled the determination of the average surface temperature. This temperature, the vapour bulk temperature, and the heat flux obtained from condensate collection served for the determination of the heat transfer coefficient. The condensation heat transfer of the pure refrigerants examined is observed to change with the driving temperature difference largely in accordance with the Nusselt theory. The experimental values of the heat transfer coefficient on the tube used, however, are by a factor of 2 larger than those on a smooth tube according to this theory. Under comparable conditions, the refrigerant R134a shows by 10 to 15% better heat transfer than R12. The heat transfer of mixtures decisively depends on the compositions of their phases. Basically, the stronger the compositions of the phases differ from each other, the lower the heat transfer coefficients; they always lie below those of R134a. In the range of low temperature difference, the heat transfer coefficient of mixtures increases with the temperature difference. This is the region of the so-called partial condensation. At a larger temperature difference, a local total condensation of the mixtures takes place and the heat transfer qualitatively follows the Nusselt theory.     

Three-dimensional flow with heat transfer of a viscoelastic fluid over a stretching surface with a magnetic field

The present research study deals with the steady flow and heat transfer of a viscoelastic fluid over a stretching surface in two lateral directions with a magnetic field applied normal to the surface. The fluid far away from the surface is ambient and the motion in the flow field is caused by stretching surface in two directions. This result is a three-dimensional flow instead of two-dimensional as considered by many authors. Self-similar solutions are obtained numerically. For some particular cases, closed form analytical solutions are also obtained. The numerical calculations show that the skin friction coefficients in x- and y-directions and the heat transfer coefficient decrease with the increasing elastic parameter, but they increase with the stretching parameter. The heat transfer coefficient for the constant heat flux case is higher than that of the constant wall temperature case.     

一种新型高效传热铜管的冷凝传热性能实验研究

建立无润滑油实验台，以R22。R134a和R410A为工质。测试新型铜管Turbo-DWT和常规内螺纹铜管Turbo—A的冷凝传热性能，并进行比较。从实验数据可知。新管型Turbo-DWT的冷凝传热系数高于Turbo-A约42％，且压降低于Turbo-A约65％（R134a）。三种制冷荆相比，R22的传热系数最高，R410A的压降最小。Turbo-DWT是一种更高效的冷凝传热管，且适用于各种冷媒。     

两种不同工质在微通道内沸腾换热特性的实验研究

为研究流体物性、流动和换热过程的状态参量对微通道内沸腾换热特性的影响规律,本文采用去离子水和无水乙醇在当量直径为0.293 mm的矩形微通道进行了不同质量流量和热流密度条件下的沸腾换热实验研究,通过对实验数据的计算和处理,分析总结了流体的热物性、质量流量、热流密度、干度和Bo数等参量对沸腾换热系数的影响规律。结果表明:沸腾换热系数随着热流密度、干度和Bo数的增大而降低,核态沸腾占主导地位;相同的质量流量和热流密度条件下,去离子水的沸腾换热系数明显高于无水乙醇的沸腾换热系数,并且前者的换热系数随质量流量的增大而增大,而后者变化不明显。根据考虑了通道尺寸效应及流体物性参量总结出的换热系数关联式进行了计算,计算结果对去离子水和无水乙醇的平均绝对误差分别为14.2%和16.6%,可认为该关联式适用于微通道内沸腾换热系数的预测。     

R134a单元式风冷冷风机组冷凝器设计

单元式风冷冷风空调机组普遍采用波纹翅片管冷凝器。对冷凝器进行设计的关键是确定制冷工质在铜管内的冷凝换热系数及空气在翅片侧的表面换热系数，同时也需要考虑空气流过冷凝器的压降，以便选择风机。采用数学模型及换热关联式计算相关参数，在此基础上对R134a单元式风冷冷风空调机组的冷凝器进行设计。     

滴形管外含不凝气体自然对流凝结换热性能研究

本文在自然对流情况下,基于双膜理论和边界层理论,考虑气液界面热阻,建立了滴形管外气液膜厚度及传热系数的数学模型,得到不同初始参数下气液膜厚度、气液膜热阻、气液界面热阻、凝液量和传热系数沿管壁的分布规律。结果表明:其他条件不变,随着混合气压力的增大(由81 325 Pa增至121 325 Pa),液膜厚度增大约7%,传热系数减小约30%。随着不凝气体质量分数的增加(由0.1%增至10%),气膜厚度减小约52%,凝液量减少约85%,传热系数减少约82%。虽然气膜厚度减小,但气膜内不凝气体质量分数增加约58%,气膜热阻增加约61%。对于当量直径相同的滴形管,其他条件不变,滴形管下半部分曲率越大,越易发生液膜分离,传热系数越大。     

R717在小管径水平光管内流动沸腾换热及压降特性

氨制冷剂存在可燃性和毒性,因此减少其在制冷系统中的充注量极为重要。小管径换热管通常可以提供更高的表面传热系数,这可以作为提升换热器紧凑性同时减少系统中充注量的有效方法。本文搭建了氨制冷剂管内流动沸腾换热及压降测试实验装置,测试了氨制冷剂在4 mm水平光管内的流动沸腾换热及压降,并分析了干度、质量流速及热流密度对换热及压降特性的影响。结果表明:流动沸腾换热表面传热系数随着干度的增加而增大,同时质量流速和热流密度越高,流动沸腾换热表面传热系数越大。此外,氨制冷剂在管内的两相摩擦压降也随着干度的增加而增大,在固定干度下,质量流速的升高导致压降增大。     

R290在水平微细圆管内沸腾换热特性研究

本文研究了R290在内径为1 mm、2 mm和4 mm水平微细圆管内的沸腾流动换热特性,在饱和温度为15℃条件下,质量流速为50～600 kg/(m²·s)、干度为0～1、热流密度为5～20 k W/m²时,对沸腾传热系数的影响进行了分析。通过实验发现,增大质量流速对传热系数具有增强作用,质量流速对传热系数的影响在低干度区域比高干度区域小。在热流密度方面,传热系数随着热流密度的增大而增大,且在1 mm和2 mm管内观察到了临界干度对传热系数的影响,这时传热系数有断崖式下降的趋势。在管径对于传热系数的影响方面,通过对不同管径换热特性的横向对比,发现在一定工况下传热系数随着管径的减小有所上升。此外本文还对R290已有的部分关联式进行了适配性验证。     

Experimental investigation on convective heat transfer mechanism in a scroll compressor

This paper describes an experimental study on the convective heat transfer inside the scroll compressor. An experimental refrigeration system is composed with extensive instrumentations in the compressor that is operated at variable speeds. The 13 thermocouples installed inside the compressor monitor the temperatures of the scroll wrap during compression process of refrigerant. The temperature and the pressure of refrigerant at suction, and the pressure at discharge ports are measured, and applied to the numerical simulation as the operating condition parameters. The temperature measured at the discharge port is used to verify the simulation result with relevant heat transfer coefficient. This paper describes the effect of motion of the orbiting scroll on the convective heat transfer in the scroll wraps. Separate experiments are performed to investigate the heat transfer in such a peculiar physical condition. With this experimental result, the effect of the oscillation of the wall on the heat transfer is quantitatively analyzed and applied to the simulation of compression process in scroll compressor. The whole consecutive compression processes in the scroll compressor is simulated in detail by solving equations of mass and energy balance for the refrigerant. The modified heat transfer coefficient correlation considering the effect of motion of the orbiting scroll predicts the discharge temperature better than other typical heat transfer coefficients.     

Determination of convective heat transfer parameters by measuring the temperature of a material

On the basis of solving the inverse problem of heat conductivity, a technique is presented for calculating the heat transfer coefficient and temperature of a steady-state gas flow by measuring temperature on the surface or in the depth of an inert material without the operation of numerical differentiation and smoothing of experimental data. The sensitivity of the solution to change in the convective heat transfer parameters is analyzed. We determine the measurement times at which experimental data contain maximum information on the sought parameters and the influence of measurement error on their determination is minimum. On the basis of approximation of the solution, the approximated formula for calculating the heat transfer coefficient is obtained. Application of the technique makes it possible to increase the accuracy in determining the convective heat transfer parameters by termocouple measurements.     

Experimental measurements for condensation of downward-flowing R123/R134a in a staggered bundle of horizontal low-finned tubes with four fin geometriesMesures expérimentales de la condensation lors de l'éoulement vertical d'un mélange de R123 et de R134a sur un faisceau de tubes en quinconce munis de quatre types d'ailettes

Experiments were conducted to obtain row-by-row heat and mass transfer data during condensation of downward-flowing zeotropic mixture R123/R134a in a staggered bundle of horizontal low-finned tubes. The vapor temperature and the mass fraction of R134a at the tube bundle inlet were about 50°C and 14%, respectively. The refrigerant mass velocity ranged from 9 to 34 kg m⁻² s⁻¹, and the condensation temperature difference from 1.9 to 12 K. Four kinds of low-finned tubes with different fin geometry were tested. The highest heat transfer coefficient was obtained with a tube which showed the highest performance for R123. However, the diference among the tubes was much smaller for the mixture than for R123. The heat transfer coefficient and the vapor-phase mass transfer coefficient decreased significantly with decreasing mass velocity. The mass transfer coefficient increased with condensation temperature difference, which was due to the effect of suction associated with condensation. On the basis of the analogy between heat and mass transfer, a dimensionless correlation of the mass transfer coefficient was developed for each tube.