垂直套管环隙内汽液固三相流动沸腾传热的实验研究

符号表C。固体颗粒在液q热通量kw／mZu。固体颗粒与液体中的含量voL％，液体汽化游热kJ／kg体的滑移速度m／s小固体颗粒直径mm或mTi流体温度”CP；液体的密度kg／m’D实验段当量直径mm或mTw加热壁面温度“CP。固体颗粒的密度kg／m’h传热膜系数kw／m’K。1循环液速m／sH液相粘度mPa。k液体导热系数W／inK1前言自MatchL．P．等人首次将固体颗粒引入换热器应用于地热利用山后，对这种流化床换热器的研究开始增多【‘－‘］。研究结果均表明，固体颗粒的引入，可显著强化传热，并有较好的防垢抗垢性能。本文的研究是在液体在垂直套管环…     

交错排列柱状微结构射流冲击强化换热实验研究

对电子芯片在FC-72工质中浸没喷射沸腾换热进行了实验研究。通过干腐蚀技术在硅片表面加工出交错排列的柱状微结构(30μm×60νm,50μm×60μm,50μm×120μm,30νm×120μ1,宽×高),硅片尺寸为10 mm×10mm×0.5 mm,过冷度为35 K,喷射速度V分别为0.5,1,1.5 m/s。喷嘴数目分别为1,4和9,直径分别为3,1.5和1mm。喷嘴出口到芯片表面的距离分别为3,6和9 mm。实验表明,交错排列柱状微结构的换热效果要好于光滑芯片,临界热流密度随着喷射速度的增加而增加。在雷诺数及其他工况相同的情况下,不同喷嘴数目对换热的影响不同,当n=4时,所有芯片的壁面温度最低,临界热流密度最高,其次是n=9,换热效果最差的是n=1。在雷诺数及其他工况相同的情况下,所有芯片的换热性能在喷射距离s=3 mm时最好,其壁温最低,临界热流密度最高,随着喷射距离的增加,其壁面温度逐渐升高,临界热流密度逐渐减小。     

快速流化床颗粒团絮的识别和表征研究

本文针对内径D=0.1m、高H=3 m的三维可视快速流化床上升管,建立了图像采集及处理系统,对平均粒径d_s=0.25 mm的石英砂(颗粒密度ρ_p=2650 kg/m~3,堆积密度ρ_(pa)=1590 kg/m~3)在颗粒循环量G_s=40～70 kg/(m~2s),流化风速U_g=4.35 m/s下形成的颗粒团絮进行了研究,提出了一套针对三维快速流化床近壁面颗粒团絮的识别和表征方法并优化了计算参数。结果表明,该方法能够准确识别不同类型("U"形、倒"U"形、条形)的颗粒团絮;颗粒团絮的尺寸随上升管高度增加和固体循环通过减小而增大,颗粒团絮数量随上升管高度增加和固体循环通量减小而减少;随固体循环通量变化,"U"形和倒"U"形的颗粒团絮下落速度的平均值均为1 m/s左右。     

柱状微结构浸没喷射沸腾强化换热实验研究

对电子芯片在FC-72工质中浸没喷射沸腾换热进行了实验研究。通过干腐蚀技术在硅片表面加工出50μm×60μm,50μm×120μm(宽×高)的柱状微结构,硅片尺寸为10 mm×10 mm×0.5 mm,过冷度分别为25、35 K,喷射速度V_j分别为0.5、1.0、1.5 m/s。实验表明,临界热流密度随着喷射速度和过冷度的增加而增加,增加过冷度和喷射速度可减小气泡脱离时的尺寸,增加气泡脱离频率,因此提高了临界热流密度并且降低了壁面温度。此外,在单相对流换热区对流换热占据主导地位,热流密度随着壁面过热度线性增加;在核态沸腾换热区,对流换热与核态沸腾换热同时影响着换热过程。当喷射速度较小时,核态沸腾区曲线的斜率比单相对流区曲线的斜率大得多,显示出浸没喷射沸腾的优良换热性能。     

堆积多孔介质中流动沸腾换热的实验研究

为了研究堆积多孔介质中流动沸腾换热特性,以横截面积为10 mm×10 mm、长100mm的铜管中充满直径为0.4～1.0 mm、孔隙率为0.31～0.37的钢珠的多孔介质为对象,对水在流过此多孔介质时沸腾换热现象进行了研究,获得了流速、热流密度、粒径和加热方位等对换热性能影响的规律:随着流速的增大,沸腾换热系数增大;随着热流密度增大,沸腾换热系数降低;随着热流密度的变化,小颗粒多孔介质的壁面过热度的变化量比大颗粒多孔介质要大得多;从下表面加热比从上表面加热的壁面过热度要低,约2～3 K,更有利于沸腾换热。     

快速流化床气固流动结构及其转变

本文建立了由内径100 mm、高3 m的上升管、两级下降管和两级旋风分离器构成的可视化快速流化床试验系统。采用平均粒径d_p=215μm,颗粒密度ρ_p=2600 kg/m~3,堆积密度ρ′_p=1700 kg/m~3,最小流化速度u_(mf)=0.04 m/s的石英砂,在表观气速U_g=0~5 m/s、静止床高与床径比H_0/D=1~4和循环通量G_s=0~120 kg/(m~2s)的操作范围内,研究了上升管中静止床高、表观气速和固体循环通量对快速流化床内气固流动结构及其转变的影响,并绘制了流动结构转变图。     

孔隙直径对R134a管外沸腾换热影响研究

在工况温度分别为6℃和10℃,对R134a在光管和三根双侧强化管(F38,F46,F56)外进行池沸腾换热试验研究。结果表明:两种工况下,R134a在光管外沸腾表面传热系数与Cooper公式计算值相对偏差均在±15%以内,R134a在强化管外沸腾表面传热系数变化趋势与光管Cooper公式基本一致。受试验管外表面孔隙直径的影响,当热流密度小于50k W/m2(或壁面温差小于2K)时,孔隙直径越小,沸腾换热效果越好;反之,当热流密度大于50k W/m2(或壁面温差大于2K)时,孔隙直径大的强化表面沸腾换热效果要优于小孔隙直径表面。     

微圆管内液体流动与换热特性的实验研究

以去离子水作为工质,在当量直径300-1570μm的微圆管(1cr18Ni9Ti)内进行层流流动与换热特性的实验研究。实验结果表明当壁面粗糙度超过1％时摩擦系数随着壁面相对粗糙度的增加而增加。在给定外壁面热流密度的条件下,当雷诺数小于100时,管壁轴向导热对换热特性的影响随着壁厚与内径比的增加而增大;当雷诺数大于100时,轴向导热的影响随着雷诺数的增加逐渐减弱,充分发展区的Nu数接近常规值4．36。     

非均匀高压电场强化R11池沸腾传热实验研究

利用EHD技术进行了工质R11的池内平板沸腾强化传热实验研究。在该实验中,换热面为一平板并接地作为0电极,高压电极为平行于换热面的线状电极。实验的热流密度为1~25 kw/m2,电压为0~±25 kV,得出了正、负电压下换热系数、壁面过热度、EHD强化系数和热流密度之间的变化关系,为进一步揭示EHD强化传热的机理提供了依据。     

高质量流速下立式螺旋管内汽液两相传热特性研究

对高质量流速下立式螺旋管内高压汽液两相流沸腾传热特性进行了试验研究,参数范围为:系统压力8.0～15.0MPa;质量流速2500～4000kg/m2s;壁面热流密度200～1000kW/m2;实验段为Φ14的不锈钢管弯制而成的螺旋管直径比为D/d=30.1的管圈,总长为2.335m,考察了热流密度和质量流速对两相传热的影响,分析核态沸腾和两相强制对流沸腾机理在螺旋管内两相传热中所起的作用,得到了局部传热系数的分布特性和平均传热系数计算关联式,首次发现高质量流速区域内螺旋管内汽液两相传热效果亦趋近于相同条件下直管内的换热系数,并对已有的结论进行了分类比较分析.     

气液固三相流载气蒸发的抗垢性能

分析了化工设备换热面上碳酸钙碱性污垢生成及其影响因素,认为液体在加热壁面上的过热是导致碳酸钙碱性污垢沉积的重要原因,降低料液在加热壁面上的过热度可收到明显的防垢抗垢效果。在蒸发器加热管内引入少量的惰性气体(载气)与流态化固体颗粒,使之形成气液固三相流载气蒸发,可显著强化传热,降低料液在加热壁面上的过热度。以碳酸钙模拟工业硬水的实验结果表明,气液固三相流载气蒸发过程表现出明显的防垢抗垢效果,且具有一定的在线清洗作用。     

流态化固体颗粒对对流沸腾传热的强化

在对流沸腾系统中引入固体颗粒,固体颗粒在液体中呈流态化,从而形成气液固三相对流沸腾过程。对气液固三相流对流沸腾过程的传热特性进行了实验研究,结果表明流态化固体颗粒对液体的对流沸腾传热具有显著的强化作用。基于固体颗粒撞击沸腾气泡时的受力分析,获得了固体颗粒穿透气泡并使气泡破碎的条件,分析了流态化固体颗粒强化沸腾传热的机理。实验结果与理论分析符合良好。     

HEAT TRANSFER COEFFICIENTS FOR TUBES SUBMERGED IN CIRCULATING FLUIDIZED BED

Convective heat transfer coefficients were measured experimentally for a tube immersed vertically in a circulating fluidized bed. Circulating fluidized beds operate in the dilute transport regime of two-phase (solid/gas) flow. The dominant mechanism for heat transfer to surfaces is particle-induced convection. In this study, experiments were carried out in a circulating fluidized bed of15 cm diameter and 11 m height. An instrumented tube of 9.5 mm diameter and 1.3 m length was placed vertically at the centeriine of the fluidized bed to measure convective heat transfer coefficients at several different elevations in the bed. Three types of particles, with mean diameters ranging from 68 to 2S1 urn, were used in the experiments at superficial gas velocities in the range of 1.3 to 8.2 m/s. Results showed that the convective heat transfer coefficients with solid/gas two-phase circulation were two to three times greater than those for single-phase gas convection at the same velocity. For a given gas velocity, the coefficients increased with increasing solid mass flux, but decreased with elevation. It was demonstrated that the heat transfer coefficients for the immersed tube and for the bed wall could be correlated with different functional dependence on the two-phase suspension density.     

循环流化床膜式壁传热试验与模型

本文研究循环流化中膜式壁的传热规律．采用电加热膜式壁传热测量元件试验研究了固体颗粒悬浮密度，膜式壁传热测板长度和空截面流化气速对传热系数的影响．对颗粒团壁面更新传热模型中的重要参数颗粒团壁面覆盖率进行探讨，提出适宜于循环流化床密相区和稀相区中的K、Y值．     

循环床中气固两相局部传热传质规律的研究

本文对含湿颗粒在循环床中干燥过程的传热传质规律进行了实验研究。本文发展的一种利用双热电偶参考标定法，获得了气、固两相沿床高的局部温度。对气体表观流速，固体循环率，颗粒初始含湿量对传热传质的影响进行了分析和讨论。所获得的循环床中传热传质系数的实验关联式，可供干燥颗粒、造粒、粒面包裹等工业设计参考使用。     

Electrostatic behavior of different fines added to a Faraday cup fluidized bed

Experiments were performed in a Faraday cup fluidization column to determine the changes in the electrostatic charges on various fine particles after their addition to gas–solid fluidized beds to better understand their role in influencing electrostatic charge generation/dissipation. The charges transported by different fines (Larostat 519 antistatic agent, glass beads (GB), silver-coated GB, catalyst and silica particles) were determined after their injection into an initially charged bed of much larger mono-sized particles (GB or polyethylene) for a range of relative humidities. Entrained fines carry significant charges out of the column, therefore leaving a net charge behind, with the polarity and quantity of charge depending on the size, physical properties and chemical structure of the particles, and on the moisture content of the fluidizing gas.     

New technique for electrostatic charge measurement in gas–solid fluidized beds

Electrostatic charge generation within gas–solid fluidized bed reactors has been a concern to industry for many years. Over the years, numerous methods for measuring this phenomenon within a fluidization column have been proposed. This paper focuses on the design of a new method that minimizes effects such as extra charging due to particle handling and bed hydrodynamic disruption due to the location of the measurement device. In addition, the new method provides the bulk charge of the bed particles rather than a local measurement. The device is flexible and can be adapted to a range of fluidization columns. The new method developed consisted of a Faraday cup placed within the windbox of a fluidization column. The distributor plate was designed in such a way that it can be automatically opened to drop the charged fluidizing particles into the Faraday cup below. The new measurement technique was validated by conducting fluidization experiments in a system consisting of a 0.10 m in diameter carbon steel column with glass beads as the fluidizing particles. The technique was proven to be suitable for measuring the total net electrostatic charges in gas–solid fluidized beds.     

Ultrasonic measurement and characterization of a low concentration system of solid particles in liquid,in high shear flow

The objective of this paper is ultrasonic measurement and characterization of solid particles in liquid (20–40 μm glass beads in water) in high shear flow (1.5–2 m/s). Ultrasonic time dependent signals as well as frequency spectra are analyzed, for simultaneous determination of average particle concentration and average flow speed. As a result, the distribution of sound energy in such concentrated systems at given flow speeds is measured. Influence of flow turbulence is demonstrated in measurements. Also, characteristic behaviors of liquid–particle mixtures like particle clustering and influence of gas bubbles have been investigated. Experimental results are complemented with a discussion of factors that influence measurement uncertainty.     

Heat recovery by perforated-plate multistage fluidized bed exchangers

An experimental and theoretical study of a perforated plate multistage fluidized bed heat exchanger for particle heating or cooling is presented. Based on experimental data (with three-stage and four-stage columns), two design correlations are proposed for predicting loading and flooding for Froude numbers ranging from 100 to 400. The heat transfer is described using a residence time distribution model which takes into account the solid and gas bypasses and the solid entrainment. Predicted values are compared to experimental data in the range 373–773 K for estimating the three parameters.