水平管内油气水三相间歇流向环状流转换的研究

对水平管内油-气-水三相间歇流向环状流转换特性进行了理论和实验研究,建立了间歇流向环状流转变的界限方程。结果表明：间歇流向环状流转变的主要因素是气相折算速度和液相折算速度,含油率与管径的影响不大。计算结果与实验结果基本吻合。     

振动状态下水平管内气液两相流流型转变的实验研究

对振动状态下水平管内气液两相流流型进行了实验研究,分析了不同振动频率、振动幅度对流型转变的影响。研究发现:随着振动频率或振动幅度的提高,在液相折算速度相同的情况下,环状流的形成需要更高的气相折算速度,而在气相折算流速相同时,泡状流的形成需要更高的液相流量;振动频率或幅度的提高使各个流型的走势分布发生变化,整体看是以弹状-波状流为中心向外有不同程度的扩张;振动频率与振动幅度两者对流型转变的影响基本相同。     

水平微细管内CO2流动沸腾流态研究

针对CO_2水平微细管内流动沸腾换热流态及流态转变特性进行实验研究。实验工况:热流密度(5~35 k W/m~2)、质量流率(50~600 kg/(m~2·s))、饱和温度(-40~0℃)、管径(0.5~1.5 mm)。实验表明:CO_2在微细管内实际流态分别是泡状流、弹状流、间歇流、层流、波状流、混状流、环状流和雾状流;干涸过程中的流态主要为环状流-雾状流、波状流-雾状流的过程及不稳定的环状流;通过理论计算获得CO_2微细管内流动沸腾换热流态图,流态图显示热流密度对高干度区域流态转变有显著影响,质量流率大小直接决定了换热过程所经历的流态;不同饱和温度工质热物性不同改变了流型;理论分析所采用的流态形式与实际CO2在微细管内所具有的流态类型基本一致。     

受热工况截面平均空泡率对漂移流模型分布参数C0的影响分析

空泡率是汽液两相流动的基本参数之一.在计算空泡率的众多模型中,Zuer-Findlay漂移流模型目前应用最为广泛.根据受热工况下局部界面参数径向分布特性实验研究结果,并通过对现有实验数据的处理,分析了受热工况下垂直上升两相流漂移流模型分布参数C0随截面平均空泡率的变化规律.证实了从过冷沸腾泡状流到饱和沸腾弹状流工况,随着空泡率的增加,分布参数C0从一个小于1的值增加到1.0～1.2.     

圆管内油-气-水三相弹状流液弹区流动特性的研究

利用液弹内气体平衡关系，建立油－气－水三相流液弹平均含气率的物理模型。同时利用光导纤维探针法，详细测定各种工况下稳态弹状流液弹的含气率局部分布规律；并通过变换探针的径向位置，研究液弹含气率沿液弹长度的空间变化规律，从细观上揭示油、气、水三相弹状流流弹区流动特性。     

平行流热管管内流动与传热的数值模拟研究

为研究平行流热管的工作机理，本文基于Fluent软件中的VOF模型编写了蒸发冷凝相变的UDF程序，对不同功率下平行流热管管内两相流动和传热过程进行了数值模拟研究。模拟结果显示了初始阶段平行流热管管内的气液分布，启动阶段管内包括泡状流、弹状流、环状流等复杂流型的转变过程，稳定工作阶段工质在各并联管路中互激振荡流动。在高加热功率下，管内工质的互激振荡流动更为剧烈，热量输送距离更远。研究结果为平行流热管换热器的优化设计提供了参考依据。     

垂直上升管内气水两相流动截面含气率的测量

用水平－上升管组合法测量垂直上升内气水两相流动在泡状流和弹状流情况下截面含气率的值,应用理论模型对实验结果进行了预测,预测值与实结果吻合良好。证实了此方法在工程应用中是一种简单、准确、可行的测量方法。     

水平PDMS微通道内气-液弹状流特性观察

对以空气、甘油为工作流体在水平聚二甲基硅氧烷(polydimethylsiloxane,PDMS)微通道内产生的弹状流进行了可视化实验研究.实验结果表明,微通道中弹状流的气柱速度随着体积含气率增大而阶梯状减小.气柱长度在体积含气率小于0.06时几乎不发生变化;当体积含气率大于0.06时,随体积含气率的增大而呈线性增大.气柱间距随体积含气率的变化与气柱长度相反.气柱和微通道壁面之间存在稳定的薄液膜,当地薄液膜压力稳定,气柱流经当地时所造成的压力波动很小;当地静压随体积含气率的增大而减小.     

基于图像处理的小通道内气液两相流含气率的实验研究

采用高速摄像机对水力直径为1.15 mm的正三角形小通道内气液两相流流型进行实时拍摄和图像采集,提出一种利用数字图像处理技术检测小通道内气液两相弹状流体积含气率的方法。针对小通道内两相流型中气泡间相互无遮掩的优势,利用图像处理技术对各流型图像进行消噪、边缘提取、二值化、区域标记和填充等处理,根据提出的三维气相体积计算模型得到体积含气率。最后与漂移流模型计算结果进行比较,比较和实验结果都表明:对于弹状流,该方法得到的含气率与真实值的误差在±15%以内,具有较高的测量精度;并对实验数据进行回归分析得到了截面含气率公式,可用于微小通道内气液两相流参数的在线检测,为今后微小通道内的两相流动特性研究提供参考。     

常用湍流模型对某低速轴流压气机转子叶尖泄漏流的预测研究

为了研究常用湍流模型对轴流压气机转子叶尖泄漏流的预测能力,对某低速轴流压气机进行了实验研究及数值模拟,对比分析了不同湍流模型预测的转子叶尖泄漏流的流场分布、旋涡特性以及堵塞特性与实验结果的异同。结果表明：对于转子叶尖泄漏流的旋涡特性,在近失速点,k-ω模型预测的转子叶尖泄漏涡轨迹的斜率和位置在周向上的分布以及泄漏涡涡核的面积与实验结果最接近;对于转子叶尖泄漏流堵塞特性,在堵塞系数达到峰值之前,BSL模型的预测结果与实验结果最相近,而在堵塞系数达到峰值之后k-ε模型的预测结果与实验结果最相近,虽然k-ω模型预测的堵塞系数在整个流向位置都偏高,但堵塞系数沿流向的分布规律与实验结果吻合最好。     

An experimental study of the statistical parameters of gas–liquid two-phase slug flow in horizontal pipeline

Experiments were performed in a horizontal test loop with inner diameter 50 mm to study the gas–liquid slug flow. The translational velocities of elongated bubbles, lengths of liquid slugs and elongated bubbles, and slug frequencies were measured using two pairs of conductivity probes. Correlations are presented for elongated bubble translational velocity, length of elongated bubble and slug frequency, respectively. It was found that the translational velocity of elongated bubble is not only dependent on Froude number, but also is significantly affected by the distance from the entrance of pipeline in the higher mixture velocity range. Mean liquid slug length is relatively insensitive to the gas and liquid flow rates in the higher mixture velocity range, however in the lower mixture velocity range, the mean liquid slug length is affected by the mixture velocity. Mean slug frequency clearly increases as the liquid superficial velocity increases but it weakly depends on the gas superficial velocity.     

换热器各流路对壳侧气液两相流动特性的影响

针对工业中广泛应用的管壳式换热器，应用空气-水两相混合物实验研究了壳侧旁路，泄漏流对气液两相流体流动特性的影响，以Ishihara两相流动模型为基础，建立了以横掠管束的主流路为基础的错流区通用两相压降计算关联式，通过错流区，泄漏流的分相流动模型，分析计算了主流路，旁路，泄漏流中气液分布，也分析了泄漏流对壳侧单相，两相总流量在各个分流路的流量分配影响，研究表明，主流路和旁路中气液各自占相应总流量的比例在不同的流型下明显不同，且比例值的波动范围较大，气液流量的分布在壳侧是不均匀的，折流板/换热管之间的泄漏流对壳侧的两相流动特性影响较小，而折流板/壳体之间的泄漏流影响较大。     

Adiabatic two-phase flow in rectangular microchannels with different aspect ratios: Part II – bubble behaviors and pressure drop in single bubble

One of the major flow patterns in a microchannel is an elongated bubble flow, which is similar to a long slug bubble. Behaviors and pressure drop for a single bubble in a rectangular microchannel were studied. Based on the experiments in Part I of this paper, data for liquid superficial velocities of 0.06–0.8 m/s, gas superficial velocities of 0.06–0.66 m/s and AR of 0.92, 0.67, 0.47 and 0.16 were analyzed. The velocity, length, number, and frequency of the single bubble in the rectangular microchannel were obtained from image processing based on a unit cell model. The bubble velocities were proportional to total superficial velocity. As the aspect ratio decreased, the portion of the bubble area increased due to the corner effect. New correlation of the bubble velocity for different aspect ratio was proposed. Also, bubble and liquid slug length, the number of the unit cell and bubble frequency were analyzed with different aspect ratios. The pressure drop for the single bubble in the rectangular microchannels was evaluated using the information of the bubble behavior. The pressure drop in the single elongated bubble was proportional to the bubble velocity. The pressure drop in the single elongated bubble in the rectangular microchannel increased as the aspect ratio decreased.     

油水乳化液中长气泡漂移速度的研究

建立圆管内滞止液体中长气泡漂移速度动量分析模型。用高速动态分析仪测量不同含水率β下,滞止油水乳化液中弹状流流型时Taylor气泡的漂移速度。结合前人的实验数据,依据Wallis的流动分类准则,给出了油水乳化液中长气泡漂移速度的半经验性公式,揭示了流动特性不同的液体中,长气泡的运动规律。     

Shape of isolated bubble in intermittent flows in a horizontal pipe

An experimental study on the shape of a single bubble similar to those observed in a horizontal plug/slug flow was performed using visual observation and conductance probes. The results indicated that the shapes of the bubble nose and the bubble body depend on the Froude number defined by gas/liquid mixture velocity, whereas the shape of the back region of the bubble depends on both the Froude number and bubble length. The photographic images showed that the structural feature of the bubble head is related to the motion characteristics of the bubble. The transition from plug flow to slug flow occurs when the tail of the bubble changes from a staircase to hydraulic jump pattern with the increasing of the Froude number and bubble length. © 2007 Wiley Periodicals, Inc. Heat Trans Asian Res, 36(5): 276– 285, 2007; Published online in Wiley InterScience ( www.interscience.wiley.com ). DOI 10.1002/htj.20161     

Flow pattern of boiling in micro-channel by numerical simulation

Boiling flows of R-134a and R-22 fluids in a 0.50 mm circular channel have been simulated to analyze bubbly flow, bubbly/slug flow, slug flow and slug/semi-annular flow depending on bubble evolution. The vapor–liquid interface was captured using VOF method. We studied the behavior of bubble growth and coalescence related to flow pattern transitions (bubbly/slug flow to slug flow, slug flow to slug/semi-annular flow) and analyzed the effect of fluid properties on transition lines. Some parameters, including heat flux, mass velocity, ONB point, vapor velocity, bubble lifting diameter, growth rate and generation frequency, have been analyzed in detail. The results show that bubble growth and coalescence are important factors for flow pattern transitions. The flow patterns at the micro-channel outlet predicted by simulation were in agreement with phenomena observed in experiments for bubbly/slug flow, slug flow and slug/semi-annular flow. In addition, the peak bubble frequency at the outlet was predicted and the general shape of the bubble frequency distribution at the outlet from simulation was found to be consistent with the achieved experimental results.     

Experimental analysis of the unit cell approach for two-phase flow dynamics in curved flow channels

Flow behavior of gas–liquid mixtures in thin channels has become increasingly important as a result of miniaturization of fluid and thermal systems. The present empirical study investigates the use of the unit cell or periodic boundary approach commonly used in two-phase flows. This work examines the flow patterns formed in small tube diameter (<3 mm) and curved geometry flow systems for air–water mixtures at standard conditions. Liquid and gas superficial velocities were varied from 0.1 to 7.0 (～±0.01) m/s and 0.03 to 14 (～±0.2) m/s for air and water respectively to determine the flow pattern formed in three geometries and dispersed bubble, plug, slug and annular flow patterns are reported using high-frame rate videography. Flow patterns formed were plotted on the generalized two-phase flow pattern map to interpret the effect of channel size and curvature on the flow regime boundaries. Relative to a straight a channel, it is shown that a ‘C shaped’ channel that causes a directional change in the flow induces chaotic advection and increases phase interaction to enhance gas bubble or liquid slug break-up thus altering the boundaries between the dispersed bubble and plug/slug flow regimes as well as between the annular and plug/slug flow regimes.     

Numerical study on the formation of Taylor bubbles in capillary tubes

Numerical simulations have been carried out for the transient formation of Taylor bubbles in a nozzle/tube co-flow arrangement by solving the unsteady, incompressible Navier–Stokes equations. A level set method was used to track the two-phase interface. The calculated bubble size, shape, liquid film thickness, bubble length, drift velocity, pressure drop and flow fields of Taylor flow agree well with the literature data. For a given nozzle/tube configuration, the formation of Taylor bubbles is found to be mainly dependent on the relative magnitude of gas and liquid superficial velocity. However, even under the same liquid and gas superficial velocities, the change of nozzle geometry alone can drastically change the size of Taylor bubbles and the pressure drop behavior inside a given capillary. This indicates that the widely used flow pattern map presented in terms of liquid and gas superficial velocities is not unique.     

Numerical study of condensation flow regime transition in wavy microchannels

A numerical research on flow regime transition in wavy microchannels was conducted. The model was based on the volume of fluid approach and user-defined routines including interfacial mass transfer and latent heat. The observed droplet flow, annular–wavy flow, injection flow, and slug–bubbly flow were qualitatively compared against experimental data and transition lines were established. The effects of inlet vapor velocity, wall heat flux, and microchannel geometry characteristics on the annular length, occurrence frequency of injection flow, initial slug volume, and bubble detachment frequency were investigated.