降膜式蒸发器用高效传热管换热性能试验研究

通过试验对降膜式蒸发器用高效传热管的换热性能进行研究,并将其与之相对应的池沸腾换热性能进行比较.由比较数据可知:样管池沸腾换热性能均随热流密度的增大而增强,降膜蒸发性能在一定热流密度下随喷淋流量的增大而增强;在恒定热流密度和恒定喷淋流量下,光管降膜燕发性能低于池沸腾性能,强化管降膜蒸发性能高于池沸腾性能;池沸腾性能高的强化管降膜蒸发性能也强.     

水平管降膜蒸发器的研究进展

介绍应用于制冷空调系统的水平管降膜蒸发器的基本原理与结构,给出管间流动模式及传热预测模型的研究现状,分析布液器及管阵布置方式对其性能的影响,为设计制造降膜蒸发器提供一定的参考。     

水平管降膜蒸发器用制冷剂分布器设计参数讨论

针对水平管降膜蒸发器用筛板式制冷剂分布器的操作流量、开孔数目、开孔大小、孔口流出系数、分布均匀度等设计参数展开讨论,由此总结了制冷剂分布器各设计参数的确定方法,以及制冷剂分布器的理论设计思路;针对筛板式制冷剂分布器设计参数的讨论也适用于其他类型的分布器。     

制冷剂充注量及布管方式对降膜式蒸发器性能影响的试验研究

水平管降膜蒸发器由于其较少的冷媒充注量和较高的换热性能在制冷空调领域得到广泛的应用。本文以R134a为工质,对冷媒充注量和两流程下管程布置方式对采用降膜式蒸发器性能的影响进行了试验研究,并与满液式蒸发器进行对比。结果表明:随着冷媒充注量的增加降膜式蒸发器换热性能逐渐提升,但提升趋势逐渐缓慢;冷冻水进出水管采用下进上出的方式机组性能优于上进下出;同等能力下,采用降膜式蒸发器机组的冷媒充注量比满液式蒸发器可减少34%。     

水平管降膜式蒸发器的研究进展及新技术

降膜式蒸发器以其高换热性能、低制冷剂充注量,以及紧凑的结构等优点,被广泛应用于工业过程的各个领域。本文以大型冷水机组中降膜式蒸发器的应用为例,从换热效率、制冷剂充注量、结构成本等几个方面与满液式蒸发器进行对比,探讨降膜蒸发技术在实际应用方面的优势、局限性和解决之道,并介绍大型冷水机组中蒸发器发展趋势以及一些新技术的应用,以期为未来设计方向和实际生产提供参考依据。     

水平管降膜式蒸发器管间流型转换试验研究

为了分析水平管降膜式蒸发器管间流型的转换规律,设计一种多层布液器,采用可视化方法研究开孔规格、布液高度和管间距对管间流型转换的影响。试验结果表明,在一定流量下,流型转换的临界雷诺数与布液孔径、布液孔间距、布液高度、管间距、流动介质有关。根据试验数据拟合得到临界雷诺数Re与伽利略数Ga的关系,发现柱状流到柱-膜状流的过渡区域比较大。     

空气源螺杆式热泵机组制冷剂迁移特性的试验研究

对使用降膜式蒸发器的空气源螺杆式热泵机组在制热运行模式下的各种制冷剂迁移现象进行试验研究,包括停机过程、开机准备工况以及除霜切换工况。试验结果表明,使用降膜式蒸发器后,上述过程存在明显的制冷剂迁移现象。针对此类特性,提出可能的改进建议,以达到机组可靠运行的目的。     

冷水机组用降膜式蒸发器研究进展综述

降膜式蒸发器以其高效的换热性能、有效减少制冷剂充注量等优点,被逐步应用于冷水机组。与其相关的研究受到行业越来越多的关注,成为相关领域的一个研究热点。本文分析当前降膜式蒸发器应用于空调冷水机组面临的技术挑战,包括制冷剂分配和换热性能影响因素,并给出改进降膜式蒸发器性能的研究方向。     

制冷空调系统水平管降膜蒸发研究

在制冷剂面临严峻的环境保护控制要求的背景下,研究表明,降膜蒸发由于其较低的制冷剂充注量在制冷空调行业具有重大的应用潜力。本文主要从降膜蒸发管外液膜的流动模式和强化传热2个方面,对水平管降膜蒸发的国内外研究现状进行研究分析。分析表明,管外液膜存在滴状流、射（柱状）流和片状流等模式,而且强化传热须区分高低热流密度情况。为了进一步探究降膜蒸发的机制,从换热和可视化的角度开展强化管外降膜蒸发的特性实验研究。     

制冷用水平降膜式蒸发器研究进展

降膜式蒸发器目前在牛奶、制药、化工、海水淡化等行业取得了较为广泛的商业应用,它从上世纪90年代以后开始应用于制冷空调系统。目前针对制冷用水平降膜式蒸发器的研究目的主要是明确各个参数对蒸发器传热性能的影响以及他们之间的联系,由于降膜式蒸发器的独特结构和内部传热传质的复杂性,这些研究尚处于初步阶段。在介绍其工作原理的基础上,针对水平降膜式蒸发器,着重讨论了布液器的结构与高度、管束(包括管径、管排数、管道表面形状)、制冷剂(流型、流量)等参数对其性能的影响。由于经验关联式在实际应用中的巨大优势,还总结了前人提出的关联式及其适用的范围,文章将为制冷用降膜式蒸发器的进一步研究和应用提供参考。     

水平管外R404A降膜蒸发传热的实验研究

搭建了降膜蒸发实验台,研究了水平单管外的降膜蒸发传热特性。测试管为外径19mm、有效实验长度为2500mm的光滑管和强化管。实验采用R404A作为管外降膜蒸发工质,与管内热水进行换热。布液采用喷嘴喷淋的方式,通过21个喷口当量直径为2mm的喷嘴完成。分别在变饱和温度(0、5、10、15℃)、变热流密度(从8到30kW/m2)和变喷淋量(从0.07到0.11kg/(m·s)时进行实验,研究了降膜蒸发换热性能相应的变化情况,得到R404A的管外降膜蒸发换热的一些规律,这对降膜蒸发器的设计及应用具有一定的参考作用。     

The heat transfer performance of horizontal tube bundles in large falling film evaporators

The performance of the horizontal heat transfer tube bundles in falling film evaporators in large compression refrigeration systems was investigated with numerical simulation in this paper. Four types of tubes, including plain tubes, and enhanced surface tubes of Turbo-B, Turbo-BII and Turbo-EHP, were employed in the simulation. Some factors, such as tube kind, tube pass arrangement, dry patch area on tube surface, liquid refrigerant flow rate, and number of flooded tubes, were analyzed based on simulated results. In the study, the maldistribution of liquid refrigerant flow caused by the distributor apparatus was discussed, which severely affects the performance of falling film evaporators according to the simulation. Some calculated results were verified by the experiment. These discussions and results can be used to guide the design of falling film evaporators under realistic flow conditions.     

水平管内气液两相流型及换热的研究进展

通过系统介绍水平管内凝结的气液两相流型,以及不同坐标形式的流型图,得出水平管内环状流、波状流和雾状流之间转换的判据。另外,列举了水平光滑管和内螺纹管内凝结换热的经验型关联式,为计算管内凝结换热提供依据。并提出了下一步研究工作的建议。     

Experimental investigations of R134a and R123 falling film evaporation on enhanced horizontal tubes

Falling film evaporation is an efficient heat transfer mode in refrigeration and air conditioning industries. In this paper, the falling film evaporation performances of R134a and R123 outside four enhanced tubes and a smooth tube are tested. The results reveal that: with the decrease of film flow rate the falling film heat transfer coefficients of both R134a and R123 on the five tubes exhibit two general stages (a plateau stage and a sharp drop stage); for R134a the plateau is quite uniform while for R123 a mild decrease occurs with the decrease in film flow rate. The four enhanced tubes behave differently in heat transfer performances for R134a and R123. R134a provides around 2–3 times of heat transfer coefficients of R123 for all tubes.     

Condensation of pure and near-azeotropic refrigerants in microfin tubes: A new computational procedure

Microfin tubes are widely used in air cooled and water cooled heat exchangers for heat pump and refrigeration applications during condensation or evaporation of refrigerants. In order to design heat exchangers and to optimize heat transfer surfaces, accurate procedures for computing pressure drops and heat transfer coefficients are necessary. This paper presents a new simple model for the prediction of the heat transfer coefficient to be applied to condensation in horizontal microfin tubes of halogenated and natural refrigerants, pure fluids or nearly azeotropic mixtures. The updated model accounts for refrigerant physical properties, two-phase flow patterns in microfin tubes and geometrical characteristics of the tubes. It is validated against a data bank of 3115 experimental heat transfer coefficients measured in different independent laboratories all over the world including diverse inside tube geometries and different condensing refrigerants among which R22, R134a, R123, R410A and CO₂.     

Prediction of heat transfer coefficient during condensation of water and R-134a on single horizontal integral-fin tubes

This paper presents a few salient features of an investigation carried out to study the heat transfer augmentation during condensation of water and R-134a vapor on horizontal integral-fin tubes. The experimental investigation was performed on two different experimental set-ups for water and R-134a. The test-sections were manufactured by machining fins over plain copper tubes of 24.4 ± 0.6 mm outside diameter. The performance of two types of finned tubes viz. circular integral-fin tubes (CIFTs) and spine integral-fin tubes (SIFTs) was studied for the condensation of water and R-134a. These tubes were positioned one by one inside the test-condenser to perform the experiments. All together the experiments were conducted for the condensation on 10 different test-section tubes. With the help of the experimental results, authors have developed an empirical equation. This equation predicts the condensing heat transfer coefficient from their own experimental data for the condensation over CIFTs and SIFTs within a range of ± 15% and experimental data of other thirteen investigators in a range of ± 35% for condensation of water and different refrigerants.     

Condensation heat transfer coefficients of R22, R407C, and R410A on a horizontal plain, low fin, and turbo-C tubes

In this study, condensation heat transfer coefficients (HTCs) were measured on a horizontal plain tube, low fin tube, and Turbo-C tube at the saturated vapor temperature of 39 °C for R22, R407C, and R410A with the wall subcooling of 3–8 °C. R407C, a non-azeotropic refrigerant mixture, exhibited a quite different condensation phenomenon from those of R22 and R410A and its condensation HTCs were up to 50% lower than those of R22. For R407C, as the wall subcooling increased, condensation HTCs decreased on a plain tube while they increased on both low fin and turbo-C tubes. This was due to the lessening effect of the vapor diffusion film with a rapid increase in condensation rate on enhanced tubes. On the other hand, condensation HTCs of R410A, almost an azeotrope, were similar to those of R22. For all refrigerants tested, condensation HTCs of turbo-C tube were the highest among the tubes tested showing a 3–8 times increase as compared to those of a plain tube.     

Prediction of two-phase pressure gradients of refrigerants in horizontal tubes

Two-phase pressure drop data were obtained for evaporation in two horizontal test sections of 10.92 and 12.00 mm diameter for five refrigerants (R-134a, R-123, R-402A, R-404A and R-502) over mass velocities from 100 to 500 kg/m² s and vapor qualities from 0.04 to 1.0. These data have then been compared against seven two-phase frictional pressure drop prediction methods. Overall, the method by Müller-Steinhagen and Heck (Müller-Steinhagen H, Heck K. A simple friction pressure drop correlation for two-phase flow in pipes. Chem. Eng. Process 1986;20:297–308) and that by Grönnerud (Grönnerud R. Investigation of liquid hold-up, flow-resistance and heat transfer in circulation type evaporators, part IV: two-phase flow resistance in boiling refrigerants. Annexe 1972-1, Bull. de l'Inst. du Froid, 1979) were found to provide the most accurate predictions while the widely quoted method of Friedel (Friedel L. Improved friction drop correlations for horizontal and vertical two-phase pipe flow. European Two-phase Flow Group Meeting, paper E2; June 1979; Ispra, Italy) gave the third best results. The data were also classified by two-phase flow pattern using the Kattan-Thome-Favrat (Kattan N, Thome JR, Favrat D. Flow boiling in horizontal tubes. Part 1: development of a diabatic two-phase flow pattern map. J. Heat Transfer 1998;120:140–7; Kattan N, Thome JR, Favrat D. Flow boiling in horizontal tubes. Part 2; new heat transfer data for five refrigerants. J Heat Transfer 1998;120:148–55; Kattan N, Thome JR, Favrat D. Flow boiling in horizontal tubes. Part 3: development of a new heat transfer model based on flow patterns. J. Heat Transfer 1998;120:156–65) flow pattern map. The best available method for annular flow was that of Müller-Steinhagen and Heck. For intermittent flow and stratified-wavy flow, the best method in both cases was that of Grönnerud. It was observed that the peak in the two-phase frictional pressure gradient at high vapor qualities coincided with the onset of dryout in the annular flow regime.