汽气混合流凝结液膜形成机理研究

汽气混合流体凝结放热过程中凝结所形成的液膜厚度对换热效果的影响较大,因此通过探讨液膜厚度沿管壁的变化,有利于分析强化换热过程。以圆管为例,对汽气混合流体凝结所形成的液膜机理、沿管壁的分布规律及换热性能进行分析,并建立相应的物理及数学模型。通过给定初始条件进行计算,结果表明：液膜沿管壁向下流动过程中其厚度逐渐增加、换热性能逐渐降低;同时分析了管壁温度、汽气混合流体速度及管径等主要参数对液膜的形成及换热性能的影响,为强化凝结换热过程提供了理论基础。     

滴形管换热性能的实验研究

采用特殊形状和表面的管子是最为常用、有效的强化换热手段。本文基于滴形管换热器回收天然气锅炉排烟余热,提出了烟气侧的换热系数实验关联式。通过改变换热管间的排列间距,在不同烟气流量下,对圆管和滴形管的换热性能及影响因素进行了分析。与实验数据比较,验证了实验关联式可正确反映凝结换热的特性。结果表明:不同烟气量通过滴形换热管的压损小于圆管,约为圆管的0.33~0.38倍;烟气温度降大于圆管;冷却水通过滴形管的温升高于圆管;换热系数滴形管比圆管的提高约7%,表明滴形管的换热性能优于圆管。因此对于有凝结换热过程发生时,滴形换热管具有强化换热的作用。     

蒸发式冷凝器不同型式换热板外表面换热特性研究

采用Fluent对管-板型、平板型及S型3种蒸发式冷凝器换热板外表面传热特性进行对比研究.将模拟所得到的温度场和空气进出口平均焓值分别代入相关的试验关联式,计算液膜与换热板外表面间的局部对流换热系数及液膜与空气界面间的平均对流换热系数,进一步利用刘易斯关系式计算液膜与空气间的传质系数.结果表明:管-板型液膜平均厚度最大...     

蒸发薄液膜非等温界面处电场强化传热的数值分析

电场能够强化微通道中延展弯月面处蒸发薄液膜区域非等温界面处的换热。分析在扩展的拉普拉斯方程及Wayner界面传质方程的蒸发毛细弯月面薄液膜区热质传输模型的基础上,加入电场力后电场强化蒸发薄液膜的换热效果。运用数值方法,讨论电场力对薄液膜固有弯月面处的曲率、蒸发质量流量、液相压力梯度、热流密度和传热系数的影响。数值计算结果表明,电场的存在可以显著提高微通道中薄液膜区域的换热系数,进而提高换热效率。     

R22和R417A在水平强化管外的凝结换热实验研究

用实验的方法研究了非共沸工质R417A在水平强化换热管管外的凝结换热性能,并与R22做了对比.试验管为两种强化换热管-斜翅管和矩翅管.结果表明:对于斜翅管,同等的壁面过冷度下,R417A的凝结换热系数大于R22的管外换热系数;对于矩翅管,同等的壁面过冷度下,R22的凝结换热系数大于R417A的凝结换热系数;在工质R417A下,两种强化管的凝结管外换热系数随壁面过冷度的变化率都比R22大,其原因应该与R417A作为一种非共沸制冷剂的温度滑移特性有关.从强化换热的角度考虑,对于表面张力较小的工质,选用斜翅管更有利.     

两种池沸腾强化换热管的传热性能实验研究

对两种用于池沸腾换热的强化管在蒸发温度为5℃的工况下进行了水平管外传热性能的实验研究.两种管子为管内外双侧强化管,管外表面同属于TURBO-B类的强化换热管,但表面形状有区别.利用威尔逊图解法确定这两种管型的管内外换热系数的关联式,同时,根据实验测得的数据对这两种管型的换热性能进行比较.结合金相显微镜拍摄的外观形状,分析尺寸结构对强化换热管的换热性能的影响.结果得出:在相同工况下,准三角形形状的管内螺纹换热性能要比梯形好,且管内螺纹数越多,换热性能越好;在一定热流密度范围内,管外换热系数随着热流密度的增加而变大,这主要与管子外表面结构的凹穴半径、凹穴开口尺寸、次级表面通道的宽度和形状等因素有关,且翅顶表面刻画的浅槽有利于池沸腾换热.     

立式蒸发式冷凝器强化传热实验研究

在立式蒸发式冷凝器水蒸汽排汽冷凝实验基础上,对圆管、插入螺旋线圆管和波纹管3种管形的立式蒸发式冷凝器进行强化传热研究.结果表明:采用插入螺旋线圆管或者波纹管都可以起到强化传热的效果,总传热系数K比圆管分别高8.7%、12.9%,但要付出增加空气流动阻力作为代价;Rwa是整个传热过程的控制热阻,它具有改变总热阻的最大潜力;插入螺旋线对降低气-液界面的热阻尤为明显,降幅达20.65%;波纹管对降低凝结换热侧的热阻尤为明显,降幅达35.85%.     

R134a在水平强化管外凝结换热的实验研究

对氟利昂R134a在水平单管外的凝结换热性能进行了试验研究,试验管为光管和三根强化管,采用热阻分离法得到蒸气侧凝结换热系数。试验结果表明:光管管外Nusselt理论值与实验数据偏差小于10%。强化管No.1-3的传热性能均好于光管,当Re=40000时,No.1-4管的总传热系数分别为:5295,5818,5904,1502W/m2.K。在相同热流密度条件下,No.1-3管的管外换热系数分别是光管的7.0-8.8倍,9.0-10.8倍,9.9-12.0倍。管外强化后,管内外的换热系数已比较接近。     

甲烷气在V型纵槽管上凝结换热强化

主要研究甲烷气膜状凝结过程及强化。建立了甲烷气膜状凝结试验台，进行了甲烷在光管和Ｖ型纵槽管上膜状凝结换热试验。结果表明光管的数据与Ｎｕｓｅｌｔ解基本一致，而Ｖ型纵槽管上膜状凝结换热系数较光管提高了３～８倍。     

圆锥槽结构强化低压水蒸气的膜状凝结实验研究

通过在冷凝面上构造圆锥槽结构,使冷凝液膜内部形成结构梯度,利用圆锥槽内冷凝液膜产生的轴向拉普拉斯压差使冷凝液自发向圆锥槽半径减小的方向运动,实现冷凝液快速排出,从而强化低压蒸气膜状凝结。实验结果表明,冷凝流量较小时,圆锥槽内凝结液膜能快速排出,膜状凝结换热得到增强,而光滑表面由于接触角滞后造成冷凝液块钉扎在冷凝面,造成传热热阻增大,凝结换热恶化;而在较大冷凝流量下,圆锥槽表面冷凝液膜变厚,液膜内部轴向压力梯度减小,轴向输运能力减弱,光滑表面冷凝液块脱离频率增加,同时合并路径上的其他液块与液珠,加快表面更新频率,造成蒸气在光滑表面的冷凝速率略大于圆锥槽表面。     

R404A和R407C在水平强化管外的凝结换热实验研究

实验研究了近共沸制冷工质R404A与非共沸制冷工质R407C在水平强化换热管管外的凝结换热性能。采用"Wilson图解法"对实验数据进行处理。结果表明:对于R404A和R407C,强化管外的凝结换热系数随着壁面过冷度的增加而增大,呈现出与纯工质冷凝时不同的变化趋势,这主要是近共沸或非共沸工质凝结过程中,某些组分的凝结会遇到其它组分的凝结气膜热阻所造成的;随着过冷度增加,易挥发组分开始凝结,气膜变薄,冷凝传热系数增大。R407C在强化换热管管外的凝结换热系数比R404A要小70%左右,这是由于R407C的温度滑移较R404A要大,管外形成的凝结扩散气膜造成的影响更大。R407C在高热流密度工况下的换热效果提升明显,故应尽量工作在高热流密度区域。     

Heat Transfer between a Gas-Droplet Medium and a High-Temperature Surface

A one-dimensional problem is treated, which is associated with heat conduction under conditions of contact between a finely divided gas-droplet medium with a highly heated surface when the temperature of the gas phase exceeds significantly the temperature of the liquid phase. Criterional equations are obtained for the calculation of the coefficient of heat transfer from a surface to a gas-droplet medium. Estimates are made of the time of complete evaporation of droplets and of the thickness of vapor-gas layer in the vicinity of the surface. The obtained results may be used to investigate the processes of cooling a metal.     

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。     

An experimental study of the fluid flow and heat transfer characteristics in micro-condensers with slug-bubbly flow

Experiments were conducted to study the condensation flow pattern in silicon micro-condensers using water as the medium. Slug-bubbly flow was found to be one of the dominant flows in the micro-condenser and it was a major factor in determining the heat transfer and pressure drop properties of the fluid inside the micro-condenser. The transition from the slug-bubbly flow to a mixed flow pattern was studied. A correlation was obtained to predict when the transition of the flow pattern would occur. Only slug-bubbly flow existed under low steam mass flow rate and high heat transfer rate conditions. As the steam mass flow rate increased or the heat transfer rate dropped, the mixed flow pattern would then appear. In the slug-bubbly flow regime, the heat transfer coefficient and pressure drop in the micro-condensers were investigated in detail. It was found that micro-condensers with smaller channels could exhibit higher heat transfer coefficients with the same Reynolds number. The condensation heat transfer coefficient was higher than that in the tubes with the diameter of centimeter. Pressure drops in the micro-condensers with smaller channels were higher due to the increased transition loss. At the same time, the pressure drop in the micro-condenser was found to be lower than what could be predicted using the macro-scale correlation. Increasing the heat flux would create a longer bubble–film region and fewer unit cells in the micro-condenser resulting in an increased heat transfer coefficient and a decreased pressure drop.     

Influence of cooling conditions on the local parameters of heat and mass transfer in condensation heat-utilization units

Based on the earlier developed model of calculation of the local parameters of heat and mass transfer in deep cooling of flue gases (a vapor-gas mixture) in a bundle of tubes of a condensation heat-utilization unit, the distribution of the parameters of a condensing vapor-gas mixture both along the length of the tubes and in the depth of the tube bundle in a crossflow under various cooling conditions corresponding to the working parameters of heat-utilization units at industrial thermoelectric plants (TEP) and in boiler houses has been obtained. A comparison of the calculated values of the heating efficiency of the indicated heat-utilization unit with the results of tests of the condensation heat-utilization unit at the Ul’yanovsk TEP-3 (Russia) has demonstrated their satisfactory agreement.     

Film condensation heat transfer of helium in a vertical tube

Helium was condensed on the wall of a vertical copper tube (14 mm in diameter, 32 mm long) in the experimental range: vapour temperature in the tube ? 4.1–5.0 K; heat flux ? 0.5–86 mW cm^?2; temperature differences across a liquid film ? 0.01–1.3 K ;film Reynolds numbers ? 3–380.It was found that the heat flux increased linearly with the film temperature difference, yielding a constant heat transfer coefficient of about 0.065 W cm^?2 K^?1. The discrepancy between the experimental results and the laminar condensation theory is also considered.     

Heat transfer associated with vapor condensation from vapor-gas mixtures

Reports results of a theoretical analysis and experimental investigation of heat transfer accompanying vapor condensation from vapor-gas mixtures. Gives a dimensionless equation for estimating the surface necessary for vapor condensation in the presence of an inert gas.     

Numerical Study on the Effects of Gravity and Surface Tension on Condensation Process in Square Minichannel

A volume of fluid (VOF) method is adopted to simulate the condensation of R134a in a horizontal single square minichannel with 1 mm side length. The effect of gravity, surface tension and gas-liquid interfacial shear stress are taken into account. The result denotes that condensation is first appeared at the corner of channel, and then the condensation is stretched at the effect of surface tension until the whole channel boundary covered. The effect of gravity on the distribution of the liquid film depends on the channel length. In short channel, the gravity shows no significant effect, the distribution shape of steam in the cross section of the channel is approximately circular. In long channel, due to the influence of gravity, the liquid converges at the bottom under the effect of gravity, and the thickness of the liquid film at the bottom is obviously higher than that of the upper part of the channel. The effect of surface tension on condensation is also analysed. The surface tension can enhance the condensation heat transfer significantly when the inlet mass flux is low. Whilst, at high mass flux, the enhancement of surface tension on heat transfer is unobvious and can be neglected.