Y型微通道两相流内部流动特性

利用显微粒子图像测速技术、高速度数码显微系统及数值模拟方法研究了Y 型微通道内液滴的形成. 主要考虑了Y 型角度（45°,90°,135°,180°）、两相流量大小等因素的影响. 发现在挤压机制中,Y 型微通道内分散相液滴的形成主要受到来自连续相的剪切作用,Y 型角度越小,分散相所受到的剪切作用越大. 在液滴生成过程中,连续相速度剖面呈非对称抛物线型分布. 当Y 型角度小于180°时,角度的变化对液滴直径大小影响较小,但角度的减小会加快液滴的生成时间. 当Y 型角度为180°时,生成的液滴体积最大且生成时间最长. 毛细数对液滴直径和生成时间的变化同时产生影响,连续相毛细数的增大使得连续相在两相交汇位置处对分散相的作用力更集中,导致分散相更易破裂.      

Y型微通道两相流内部流动特性刘

利用显微粒子图像测速技术、高速度数码显微系统及数值模拟方法研究了Y 型微通道内液滴的形成. 主要考虑了Y 型角度（45°,90°,135°,180°）、两相流量大小等因素的影响. 发现在挤压机制中,Y 型微通道内分散相液滴的形成主要受到来自连续相的剪切作用,Y 型角度越小,分散相所受到的剪切作用越大. 在液滴生成过程中,连续相速度剖面呈非对称抛物线型分布. 当Y 型角度小于180°时,角度的变化对液滴直径大小影响较小,但角度的减小会加快液滴的生成时间. 当Y 型角度为180°时,生成的液滴体积最大且生成时间最长. 毛细数对液滴直径和生成时间的变化同时产生影响,连续相毛细数的增大使得连续相在两相交汇位置处对分散相的作用力更集中,导致分散相更易破裂.     

组装式微流控系统制备双重包裹微液滴的方法研究

介绍了一种组装式微流控系统制备单、双重包裹微液滴的方法。微系统中用三通接头构成T型微流体通道,使得分散相在连续相强烈的剪切力和压力差作用下断裂形成单个微米级液滴。在制备单个微液滴基础上,用毛细管将两个三通接头串联,通过调控三相流量,可产生双重包裹液滴。结合实验结果,分析了流体粘度比对液滴大小的影响,并得出液滴的尺寸与流量比之间的关系式,为制备不同尺寸的液滴提供了参考依据。对制备的样品进行统计分析,结果显示,液滴的多分散性指数均小于3.2%,表明微液滴的高度均匀性。此外,通过调节三相液体的流量不仅可以控制内外层液滴的大小,还可以调节内层包裹液滴的个数。本文提出的制备方法,设备组装拆卸简便,不需表面亲疏水性处理,装置利用率高,产生的单、双重包裹微液滴可满足高通量的测量分析要求。     

离散型湍流多相流动的研究进展和需求

离散型多相流动,指气体-颗粒(气-固)、液体-颗粒(液-固)、液体-气泡、气体-液雾以及气泡-液体-颗粒等两相或三相流动.这种类型的多相流动广泛存在于能源, 航天和航空, 化工和冶金,交通运输, 水利, 核能等领域.本文阐述了离散型多相流动的国内外基础研究,包括颗粒/液滴/气泡在流场中受流体动力作用力的研究, 颗粒-颗粒,液滴-液滴,气泡-气泡之间以及颗粒/液滴和壁面之间碰撞和聚集规律的研究,颗粒-气体和气泡-液体湍流相互作用的研究, 和数值模拟的研究,包括多相流动的雷诺平均模拟、大涡模拟和直接数值模拟的研究进展.最后, 归纳了目前尚待研究的需求.      

旋流喷嘴中空旋转射流近区域流动的研究

从理论上分析了旋流喷嘴喷出的中空射流近区域的液膜的运动,在只考虑液膜表面张力的作用下,应用质量守恒和动量定理,建立了描述液膜运动的非线性常微分（积分）方程组,该方程组可以用数值方法方便地求解,结果表明,液体离开旋流喷嘴后在自由空间形成的液膜呈葫芦形状,其速度和液膜厚度等都周期性地变化。本结果是在液厝受拓动失称碎成液滴前的最基本运动状态,可以在射流的近区域内实验观察到,也是进一步从理论液膜破碎雾化过     

液体的爆炸抛撒特征

针对液体爆炸抛撒过程设计了实验装置,利用高速摄像仪进行记录。通过研究不同中心装药量和 填充液体的抛撒过程,发现在壳体破裂后,液体沿裂缝处向外飞散。药量较小时,液体分散成树枝状形态,然 后破碎成液滴;药量较大时,则形成液体环状区。对于不同粘度的液体,环状区分别由小液滴及已雾化、汽化 的液体,或大液滴、液体丝及液膜等组成,抛撒过程中其宽度越来越大,大液滴、液体丝及液膜等也逐渐破碎成 细小的液滴。     

气液二相流研究概述

气液二相流研究液体和气体(或蒸气)两相介质共存条件下的流动特性。二相体系可以是液体中含有气体或(蒸气)泡或者气体,(或蒸气)中含有液体微滴,也可能因其中气泡或液滴的聚并,两相间形成更复杂的分布状态。气液二相流是自然界、日常生活中常见的现象,在许      

煤油液滴直径对两相旋转爆轰发动机流场的影响

为探究煤油液滴不同初始直径对气液两相旋转爆轰发动机流场的影响,假设初始注入的煤油液滴具有均匀直径,考虑雾化破碎、蒸发等过程,建立了非定常两相爆轰的Eulerian-Lagrangian模型,进行了液态煤油/高温空气爆轰的非预混二维数值模拟。结果表明：在初始液滴直径为1～70μm的工况范围,燃烧室内均形成了单个稳定传播的旋转爆轰波;全局当量比为1时,爆轰波前的空气区域大于液滴煤油的蒸气区域,导致波前燃料空气混合不均匀,波前均存在富油区和贫油区,两相速度差导致分离出的空气形成低温条带;当煤油液滴的初始直径较小时,波前的反应物混合过程主要受蒸发的影响,爆轰波可稳定传播;当直径减小至1μm时,煤油液滴在入口处即蒸发,旋转爆轰波表现为气相传播的特性,爆轰波结构平整;当煤油液滴的初始直径较大时,波前的反应物混合过程主要受液滴破碎的影响;对于相同的燃料质量流量,在不同初始煤油液滴直径工况下,煤油液滴最大的停留时间均占爆轰波传播时间尺度的80%以上;爆轰波前燃料预蒸发为气相的占比越高,爆轰波的传播速度越高;初始液滴直径为10～70μm的工况范围内,爆轰波的速度随初始直径的增大先升高后降低。     

椭球液滴撞击超疏水表面反弹过程数值分析

液滴在自由落体或受外力作用时常发生椭球形变,对其撞击超疏水壁面的运动形态及形成二次液滴有较大影响.本文假定具有不同轴向半径比值(AR)的椭球形液滴,采用耦合水平集-体积分数(CLSVOF)方法对椭球形液滴撞击超疏水平壁面进行数值模拟研究,对椭球形液滴撞击超疏水平壁面反弹过程运动形态和AR对二次液滴形成的影响进行分析.研究表明,不同AR液滴撞击超疏水壁面后反弹过程具有一定相似性,同时存在明显差异.液滴反弹过程中会拉伸形成长液柱,其未扰动界面直径随AR的增大而减小.在Plateau-Rayleigh不稳定性影响下,长液柱会发生破碎形成二次液滴,但较低的AR对二次液滴的形成有较明显的抑制作用,当AR小于临界值0.6时,反弹过程中液滴内部压力均匀稳定,最终不产生二次液滴.     

液滴冲击液面过程中变形特征的实验研究

用高速相机拍摄了液滴以不同速度冲击液面的运动过程,测量了冲击过程中典型时刻液坑、中心液柱、次生液滴和次生液柱的几何尺寸,对这些几何尺寸的最大值与韦伯数(We)的关系进行了回归分析,结果表明:空间上,液坑的最大垂直深度、液坑的最大水平长度、中心液柱的最大高度、次生液滴等效直径和次生液柱的最大高度随We数增加呈线性增加;次生液滴等效直径是初始液滴等效直径的1.2～2倍;当200We220时,次生液滴冲击液面没有次生液柱生成,当360We713时,有次生液柱形成,220≤We≤360为过渡区;时间上,We数越大,运动过程中液坑的大小和中心液柱的高度变化越快,液坑和中心液柱持续时间越长,中心液柱达到最大高度的时刻以及破碎生成次生液滴的时刻也越晚。     

流动聚焦装置中液滴的形成:喉部尺寸的影响

在本文中,研究了液滴在一个流动聚焦微流体设备中的形成过程,分析了喉部长度和宽度以及连续相的流速和分散相的粘度对液滴尺寸的影响。在固定的分散相流速(Qd)下,连续相流速(Q_c)对于液滴尺寸有重要的影响。当Q_c0.7mL/h,液滴尺寸在喉部长度到达一个临界值之前先趋于增加,之后随着喉部尺寸的继续增加逐渐下降;当Q_c0.7mL/h,液滴尺寸随着喉部长度的增加而降低。而越大的喉部宽度会产生越大尺寸的液滴。在Q_c继续增长的过程中通常会出现从挤压模式到滴模式的转变,最终液滴尺寸呈现出随着Q_c的增加指数降低的特征。归因于流速控制破碎机制,低粘度分散相下,液滴尺寸随粘度的增加而增加。     

Pressure drop in two phase slug/bubble flows in mini scale capillaries

A segmented two phase slug/bubble flow occurs where a liquid and a gas are pumped into the same tube over a range of Reynolds numbers. This segmented two phase flow regime is accompanied by an increase in pressure drop relative to the single phase flow where only one fluid is flowing in a capillary. This work experimentally and theoretically examines the pressure drop encountered by the slug/bubble flow with varying slug lengths in mini channels. In the experimental work the dimensionless parameters of Reynolds number and Capillary number span over three orders of magnitude, and dimensionless slug length ranges over two orders of magnitude to represent flows typical of mini- and micro-scale systems. It is found, in agreement with previous work, that these dimensionless groups provide the correct scaling to represent the pressure drop in two phase slug/bubble flow, although the additional pressure drop caused by the interface regions was found to be ∼40% less than previously reported.     

Noise generated by cavitating single-hole and multi-hole orifices in a water pipe

This paper presents an experimental study of the acoustical effects of cavitation caused by a water flow through an orifice. A circular-centered single-hole orifice and a multi-hole orifice are tested. Experiments are performed under industrial conditions: the pressure drop across the orifice varies from 3 to 30 bar, corresponding to cavitation numbers from 0.74 to 0.03. Two regimes of cavitation are discerned. In each regime, the broadband noise spectra obtained far downstream of the orifice are presented. A nondimensional representation is proposed: in the intermediate ‘developed cavitation’ regime, spectra collapse reasonably well; in the more intense ‘super cavitation’ regime, spectra depend strongly on the quantity of air remaining in the water downstream of the orifice, which is revealed by the measure of the speed of sound at the downstream transducers. In the ‘developed cavitation’ regime, whistling associated with periodic vortex shedding is observed. The corresponding Strouhal number agrees reasonably well with literature for single-phase flows. In the 'super cavitation’ regime, the whistling disappears.     

Flow regime transitions due to cavitation in the flow through an orifice

This paper presents both experimental and theoretical aspects of the flow regime transitions caused by cavitation when water is passing through an orifice. Cavitation inception marks the transition from single-phase to two-phase bubbly flow; choked cavitation marks the transition from two-phase bubbly flow to two-phase annular jet flow.

It has been found that the inception of cavitation does not necessarily require that the minimum static pressure at the vena contracta downstream of the orifice, be equal to the vapour pressure liquid. In fact, it is well above the vapour pressure at the point of inception. The cavitation number [σ = (P₃ − P_v)/(0.5 pV²); here P₃ is the downstream pressure, P_v is the vapour pressure of the liquid, ρ is the density of the liquid and V is the average liquid velocity at the orifice] at inception is independent of the liquid velocity but strongly dependent on the size of the geometry. Choked cavitation occurs when this minimum pressure approaches the vapour pressure. The cavitation number at the choked condition is a function of the ratio of the orifice diameter (d) to the pipe diameter (D) only. When super cavitation occurs, the dimensionless jet length [L/(D - d); where L is the dimensional length of the jet] can be correlated by using the cavitation number. The vaporization rate of the surface of the liquid jet in super cavitation has been evaluated based on the experiments.

Experiments have also been conducted in which air was deliberately introduced at the vena contracta to simulate the flow regime transition at choked cavitation. Correlations have been obtained to calculate the critical air flow rate required to cause the flow regime transition. By drawing an analogy with choked cavitation, where the air flow rate required to cause the transition is zero, the vapour and released gas flow rate can be predicted.     

Effect of diameter on two-phase pressure drop in narrow tubes

The effect of tube diameter on two-phase frictional pressure drop was investigated in circular tubes with inner diameters of 0.6, 1.2, 1.7, 2.6 and 3.4 mm using air and water. The gas and liquid superficial velocity ranges were 0.01-50 m/s and 0.01-3 m/s, respectively. The gas and liquid flow rates were measured and the two-phase flow pattern images were recorded using high-speed CMOS camera. Unique flow patterns were observed for smaller tube diameters. Pressure drop was measured and compared with various existing models such as homogeneous model and Lockhart-Martinelli model. It appears that the dominant effect of surface tension shrinking the flow stratification in the annular regime is important. It was found that existing models are inadequate in predicting the pressure drop for all the flow regimes visualized. Based on the analysis of present experimental frictional pressure drop data a correlation is proposed for predicting Chisholm parameter “C” in slug annular flow pattern. For all other flow regimes Chisholm’s original correlation appears to be adequate except the bubbly flow regime where homogeneous model works well. The modification results in overall mean deviation of pressure drop within 25% for all tube diameters considered. This approach of flow regime based modification of liquid gas interaction parameter appears to be the key to pressure drop prediction in narrow tubes.     

Evaluating cavitation regimes in an internal orifice at different temperatures using frequency analysis and visualization

Experiments on a water cavitating orifice were conducted to investigate the influence of pressure and temperature on flow regime transition due to cavitation. The thermal effects could be important in cases with cryogenic cavitation or hot fluid injection. The investigations were based on CCD observations and a pressure fluctuations frequency analysis.The high-speed photographic recordings were used to analyze the cavitation evolution and individuate the frequency content of the two-phase flow by processing the pixel-intensity time-series data.The cavitating structures showed different behaviors and characteristics with variations in operating conditions, as the pressure inside the orifice and the flow temperature .The flow regime map for the cavitating flow was obtained using experimental observations to analyze the occurrence of the different two-phase flow regime transitions at various operating conditions.As the pressure at the orifice inlet increased, at the same downstream pressure, cavitation inception occurred. The decrease of the cavitation number brought a significant increase in cavitation zone extension. As the pressure drop inside the orifice increased, the cavitation was characterized by an evident increase in cavitation zone length to the outlet of the orifice. With a further cavitation number decrease, the transition to jet cavitation was evident.The temperature influenced both the cavitation intensity and the cavitation number at which different two-phase flow regime transitions occurred, which tended to increase with temperature.The vapor fraction was estimated using an image processing algorithm.The frequency content given by the pressure fluctuations was analyzed and compared with the frequency spectra obtained from the visual observations. The behavior of the different cavitating flows could be correlated to the frequency spectrum of the pressure fluctuations measured upstream and downstream of the orifice. The cavitation number reduction and consequent increase in cavitating area width were related to a corresponding significant increase in the amplitude of typical frequency components. The transition to jet cavitation was characterized by a significant increase in the first peak in the frequency spectrum; weaker spectral peaks were also present at high cavitation numbers.     

Origin of regime transition to turbulent flow in bubble column: Orifice- and column-induced transitions

The possible events during bubble formation on an orifice were investigated using a rectangular bubble column (30 cm × 30 cm × 100 cm). The gas flow rate through a single orifice was adjusted from 0.1 dm³/min to 5.0 dm³/min covering a high flow rate regime. At the high gas flow rate, the bubble formation process was complicated by diverse events, such as wake effect, channeling, and orifice-induced turbulent flow. The detachment period could be used to discern the bubble formation steps because it was strongly affected by the above events. The bubble size distribution around the orifice was also analyzed to gain a clearer understanding of the bubble formation process. Above the rate of 3.0 dm³/min through a single orifice, the detachment period converged to a value of 25 ms irrespective of the orifice diameter. The bubble size distribution also showed little difference in this range of gas flow rate. This could be explained by the development of turbulent flow around the orifice. A 0.15 m in-diameter bubble column was tested to investigate the effect of orifice-induced turbulent flow on the regime transition in which the homogeneous flow regime is converted into the heterogeneous flow regime in the column. Obvious distinction between the orifice- and column-induced transitions was observed.     

Experimental investigation on the distribution uniformity and pressure drop of perforated plate distributors for the innovative spray-type packed bed thermal storage

As an innovative thermal energy technology, the spray-type packed bed has advantages of high efficiency and low cost. A liquid distributor is the key component for the spray-type packed bed for scattering heat-transfer liquid drops evenly. In this study, the distribution performance and pressure drop of the perforated plate distributors of different orifice diameters were studied experimentally. The experimental results indicate that orifice diameter has a greater effect on the distribution performance compared to flow rate. With an increase in flow rate, the flow pattern through the distributor changes from the uncovered drop to the covered drop and then to the jet flow. The covered drop pattern shows the best performance with a good distribution and a small pressure drop simultaneously, which is the design and optimization principle of the distributor for a spray-type packed bed.     

Approximate elongation flow properties utilising the opposed orifice technique – Correction for shear and inertia

Mackay et al. (1995) have presented an approximate technique to determine the elongation viscosity from pressure drop measurements in a simple stagnation flow device. In the present paper we describe experiments using a high viscosity Newtonian oil, aimed at probing some of the assumptions made by Mackay et al. We find that Trouton ratios calculated using the original analysis are well above the value of three expected for Newtonian fluids. Finite element simulations of the flow field show this is due to the net pressure drop having a substantial shear contribution, which should be corrected for before the Trouton ratios are evaluated. Interestingly, most of the shear correction is due to shear on the inside of the orifice near the exit from the central flow region. The shear contribution to the pressure drop occurs for all flow rates, however, at large flow rates there is also an inertial correction to the pressure drop. In this paper we describe an approximate method that corrects for both shear and inertial effects. With these effects recognised and corrected for, the measured Trouton ratios are reduced to around three. Received: 15 December 1997 Accepted: 16 March 1998     

Nonlinear dynamics and conformational changes of linear entangled polymers using the Rolie-Poly model with an “effective” maximum contour length

The extended Rouse-CCR tube model for linear entangled polymers recently proposed by the authors (Kabanemi and Hétu, J Non Newtonian-Fluid Mech 160:113–121, 2009), designed to capture the progressive changes in the average internal structure (kinked state) of polymer chains, is here used to analyze, by means of a time-dependent three-dimensional finite element method, chain segment dynamics, pressure drop, and stability of flow through a 4:1:4 constriction in a tube. The model predicts an enhancement of the pressure drop in the stretch-dominated flow regime, which is also observed experimentally. This excess pressure drop was not associated with the onset of flow instability. The model also predicts kinked configurations within chain segments in the entry section to the constriction tube, at the inception of flow, and prior to the development of upstream vortices. It is also shown how these kinked configurations within chain segments influence pressure drop transients.