充分发展圆管湍JJL的实验研究

采用粒子数字图像测速(digital particle image velocimetry,DPIV)和定量流动显示技术(quantitative flow visualization,QFV)对充分发展的圆管湍流进行了研究.测量结果和直接数值模拟(direct numerical simulation,DNS)结果进行了比较,结果表明作者开发的DPIV技术取得了满意的精度.在此基础上对圆管湍流的动力学机理进行了研究,分析了上抛和下扫在湍流生成中的贡献以及流动显示结构内的脉动速度分布,测量结果显示在圆管湍流的近壁区存在横向强脉冲现象和流动显示所能观察到的结构为上抛占主导地位的结构.     

空间发展圆管转捩的直接数值模拟

利用直接数值模拟研究圆管流动中由局部壁面引入的周期性吹吸(PSB)扰动沿流向的空间发展,流动的雷诺数Re选定为3000.在临界幅值的PSB扰动下,在较短的圆管内,圆管中的扰动沿流向快速增长,在足够长的圆管内,扰动沿流向持续增长发生转捩,流动发展到湍流阶段.     

旋转圆管湍流的大涡模拟数值研究

采用大涡模拟(LES)方法,并结合动力学亚格子尺度应力(SGS)模型,通过数值求解柱坐标系下的滤波Navier-Stokes方程,研究了绕管轴旋转圆管内的湍流流动特性. 为验证计算的可靠性,以及动力学SGS模型对于旋转湍流的适用性,将大涡模拟计算所得的结果,与相应的直接模拟(DNS)结果和实验数据进行了对比验证,吻合良好. 进一步对旋转圆管湍流的物理机理进行了探讨,研究了湍流特性随旋转速率的变化规律. 当旋转速率增加时,湍流流动有层流化的发展趋势. 基于湍动能变化的关系,分析了旋转效应对湍流脉动生成的抑制作用.     

纵向微结构超疏水壁面湍流边界层减阻实验研究

使用时间分辨的二维粒子图像测速技术 (2D-PIV),测量了超疏水壁面(SHS)在槽道中的湍流边界层。基于边界层厚度的摩擦雷诺数在119至173之间。SHS具有微米级的流向沟槽结构,并在展向上均匀分布。实验发现SHS的摩擦系数均小于光滑壁面,且随雷诺数的增加而减少。当摩擦雷诺数约为150并且气体比例分数为0.65时,阻力比存在一个合理的“极小区域”。所有SHS的阻力比均与摩擦雷诺数呈显著负相关关系,并随着无量纲粗糙度宽度的增加而降低。同时还发现无量纲粗糙度宽度等于4为临界位置,此时初始阻力比会随着无量纲粗糙度宽度的增加沿三次多项式迁移。本文通过分析摩擦雷诺数、气体比例分数以及无量纲粗糙度宽度,提出了包含一种新的无量纲特征参数的减阻模型,该模型展示了与摩擦雷诺数、气体比例分数以及无量纲粗糙度宽度有关的函数关系。本研究结果可以加强关于SHS减阻各相关因素之间的联系,同时为微米级结构的设计提供合理的预测和优化方案。     

气固两相流动的湍流脉动扩散数学模型及其应用

本文提出了气固两相流动的湍流扩展数学模型，本模型用k-ε双方程模型求解气相湍流场，并根据气流脉动的频谱、能谱曲线提出了随机富工级数来模拟气相脉动速度，用拉氏方法描述颗粒的运动，故称为脉动频谱随机颗粒轨道模型。本文还给出了本模型在气固多相射流和流化床内应用的实例。     

环形通道内湍流旋流流动的数值模拟

本文应用一种考虑湍流－旋流相互作用及湍流脉动各向异性的新的代数Ｒｅｙｎｏｌｄｓ应力模型,对环形通道内的湍流旋流流动进行了数值模拟,研究了改主为旋流流数,进口轴向速度及半径比等参数对环形通道内湍流流动的影响,以及对强化环形通道内传热的作用。     

固体颗粒对沟槽湍流边界层影响的实验研究

本文采用粒子图像测速技术(particles image velocimetry, PIV)研究固体颗粒对放置在平板湍流边界层中的平壁和沟槽壁面减阻效果的影响. 实验对清水和加入粒径为155 μm聚苯乙烯颗粒的流法向二维速度场信息进行采集, 对不同工况下的平均速度剖面、雷诺应力和湍流度等统计量进行对比, 分析流体在边界层中的行为. 运用空间局部平均结构函数提取了不同工况湍流边界层喷射−扫掠行为的空间拓扑结构并进行比较. 结果发现, 在不同的壁面条件下, 粒子加入后的对数律区中无量纲速度均略大于清水组, 雷诺切应力有所降低, 湍流度有所减弱. 对于不同流场速度下的沟槽而言, 颗粒的加入均降低了壁面附近的阻力, 而颗粒单独作用于光滑壁面的减阻效果并不明显. 加入粒子后的相干结构数目有所增加, 法向脉动速度下降. 沟槽壁面附近的相干结构数目有所增加, 法向脉动速度在自由来流速度较大时有所上升, 在速度较小时有所下降. 这表明不同减阻状况下的沟槽均能将大涡破碎成更多的涡, 并且粒子的加入强化了这种破碎作用.

     

各向同性湍流内颗粒碰撞率的直接模拟研究

对 Re_{lambda } 约为51均匀各向同性湍流内 St_{k}(=tau_{p}/tau_{k}) 为 0 ~10.0 的有限惯性颗粒的碰撞行为进行了直接数值模拟,以研究湍流对有限惯性颗粒碰撞的影响. 结果表明,具有一定惯性颗粒的湍流碰撞率完全不同于零惯性的轻颗粒 (St_{k}=0) 和可忽略湍流作用的重颗粒 (St{k} to infty) , 其变化趋势极其复杂：在Stk为 0~1.0 之间,颗粒的碰撞率随 St 的增加而近乎线性地剧烈增长,在Stk≈1.0 3.0(对应的StE=τp/Te≈0.5)附近,颗粒碰撞率出现两个峰值,在Stk>3.0以后,颗粒的碰撞率随惯性增大而逐渐趋向于重颗粒极限;在峰值处,有限惯性颗粒的平均碰撞率的峰值较轻颗粒增强了30倍左右. 为进一步分析湍流作用下颗粒碰撞率的影响因素,分别使用可能发生碰撞的颗粒对的径向分布函数和径向相对速度来量化颗粒的局部富集效应和湍流掺混效应,表明 St_{k} approx 1.0 时局部富集效应最为强烈,使得颗粒的碰撞率出现第1个峰值;湍流掺混效应则随着颗粒Stk的增大而渐近增大;局部富集和湍流掺混联合作用的结果,使得颗粒碰撞率在 St_{k} approx 3.0 附近出现另一个峰值.     

自由剪切湍流中颗粒-拟序结构相互作用研究进展

从实验和数值模拟两方面评述了颗粒-湍流拟序结构相互作用的近期研究进展.关于Stokes数不同对颗粒行为和拟序结构影响的试验研究,从单点激光多普勒测量到粒子图像全场测速,并与流场显示定性方法结合,揭示了不同Stokes数范围颗粒-拟序结构相互作用的规律.基于涡方法、直接数值模拟和大涡模拟等的模拟研究,进一步揭示颗粒-拟序结构的相互耦合作用和外界激励的调制作用等规律,同时推动了算法的发展.      

不同参数下环形通道内湍流旋流流动的模拟

应用一种合理考虑湍流一旋流相互作用及湍流脉动各向异性的新的代数ＲｅｙｎｏｌｄＳ应力模型,对环形通道内的湍流旋流流动进行了数值模拟．研究了旋流数、进口轴向速度和内外半径比等参数对环形通道内湍流旋流流动的影响,以及由此产生的流场变化对强化环形通道内传热的作用．     

Measurement of mixing processes with combined digital particle image velocimetry and planar laser induced fluorescence

A combined digital particle image velocimetry (DPIV) and planar laser induced fluorescence (PLIF) approach was developed to measure both the time mean and turbulent mass transport in mixing processes. The system couples the two well-known techniques to enable synchronized planar measurements of flow velocities and concentrations in a study area. The potential interference effect between the seeding particles for DPIV and the fluorescent dye excitation for PLIF was carefully investigated. The performance of the system was verified with the experimental results of a turbulent round jet discharging into a stagnant environment. Comparison between the measurements obtained in the present study with the large body of existing information on pure jets is satisfactory. The key advantage of the shorter duration required with this approach compared to point-based techniques is highlighted.     

纵向涡对近壁湍流结构的影响

在封闭水槽中用氢气泡方法观察了纵向涡对近壁湍流结构的影响,涡的下洗侧出现了展向距离较宽、流动较稳定的快斑区,流向速度快;涡的上洗侧出现了含有慢斑的区域,流动结构复杂,流向速度慢,纵向涡使下洗侧速度较快的流体流向壁面,使上洗侧速度较慢的流体远离壁面。     

Degradation effects of dilute polymer solutions on turbulent drag reduction in pipe flows

An important practical problem in the application and study of drag reduction by polymer additives is the degradation of the polymer, for instance due to intense shearing, especially in recirculatory flow systems. Such degradation leads to a marked loss of the drag-reducing capability of the polymer.Three different polymer types were tested on degradation effects in a closed pipe flow system. The polymers used were Polyox WSR-301, Separan AP-273 and Superfloc A-110, dissolved in water in concentrations of 20 wppm each. The flow system consisted of a 16.3 mm pipe of 4.25 m length. Two different pumps were used: a centrifugal pump and a disc pump. Different solution-preparation procedures were tried and the experiments were performed at different flow rates.Superfloc A-110 proved to be both the most effective drag reducer and most resistant to degradation. Because of very fast degradation, Polyox WSR-301 was found to be unsuitable for being used as a drag reducer in re-circulatory systems. The disc pump proved to be much better suited for pumping the polymer solutions than the centrifugal pump. The degradation curve of the combination Superfloc/disc pump showed a plateau-like region with reasonable drag reduction, which makes it possible to perform (laser Doppler) measurements under nearly constant circumstances during a sufficient time.     

湍流管径问题算法的改进

本文采服无量纲参数（ｇＪＯ＾３／ｖ＾５）及ＫｓＶ／Ｑ）由最小二乘法以指数函数拟合Ｐｒａｎｄｔｌ及Ｋａｒｍａｎ公式，得出分别适用于光滑区和粗糙区的管径算式。再对以上两式作粘性关联偶合，得出适用于湍流过渡区的管径算式。可直接求出管径，避免繁复试算和迭代。计算结果与Ｐｒａｎｄｔｌ，Ｋａｒｍａｎ及Ｃｏｌｅｌｒｏｏｋ－Ｗｈｉｔｅ等经典公式能精确吻合，较Ｓｗａｍｅｅ－Ｊａｉｎ湍流管径算式误差减少一半以上。     

Laser-Doppler measurements of laminar and turbulent flow in a pipe bend

Laser-Doppler measurements are reported for laminar and turbulent flow through a 90° bend of circular cross-section with mean radius of curvature equal to 2.8 times the diameter. The measurements were made in cross-stream planes 0.58 diameters upstream of the bend inlet plane, in 30, 60 and 75° planes in the bend and in planes one and six diameters downstream of the exit plane. Three sets of data were obtained: for laminar flow at Reynolds numbers of 500 and 1093 and for turbulent flow at the maximum obtainable Reynolds number of 43 000. The results show the development of strong pressure-driven secondary flows in the form of a pair of counter-rotating vortices in the streamwise direction. The strength and character of the secondary flows were found to depend on the thickness and nature of the inlet boundary layers, inlet conditions which could not be varied independently of Reynolds number. The quantitative anemometer measurements are supported by flow visualization studies. Refractive index matching at the fluid-wall interface was not used; the measurements consist, therefore, of streamwise components of mean and fluctuating velocities only, supplemented by wall pressure measurements for the turbulent flow. The displacement of the laser measurement volume due to refraction is allowed for in simple geometrical calculations. The results are intenden for use as benchmark data for calibrating flow calculation methods.     

湍流边界层中马蹄形涡的形成方式

本文使用一种新的流动显示方法——激光片光运动法和几种实验技巧对湍流边界层中的马蹄形涡进行了观测,发现并描述了其形成的四种方式:二次不稳定式、组合式、变形式和突发式。对这四种马蹄形涡的形成及发展进行了研究和比较。实验结果表明,这些马蹄形涡在尺度、运动速度和变形上是有差别的。     

槽道湍流近壁结构的DPIV观测实验

采用DPIV系统(由两台CCD相机组成)对槽道湍流进行速度场时间历程的观测实验,通过对大量测量结果的综合分析,取得了槽道湍流近壁结构的空间结构及其时间演化过程特征的结果,可以揭示上扫下掠、湍流瞬时速度型等现象与大尺度涡演化的物理关系,解释若干湍流大尺度结构的特征机理,还表明DPIV系统提供了一种定量观测湍流的时空结构特征的手段.     

On the Lower Critical Reynolds Number for Flow in a Circular Pipe

Flow in a circular pipe is investigated experimentally at Reynolds numbers higher than that at which the resistance coefficients calculated from the Blasius formula for laminar flow and from the Prandtl formula for turbulent flow are equal. The corresponding Reynolds number based on the mean-flow velocity and the pipe diameter is about 1000. The experiments were performed at a high level of inlet pulsations produced by feeding gas into the pipe through a hole with a diameter several times smaller than the pipe diameter. In our experiments the critical Reynolds number was determined as the value, independent of the distance from the inlet, at which the ratio of the axial to the mean-flow velocity as a function of the Reynolds number deviated from 2. At the maximum ratio of the pipe cross-sectional area to the area of the hole through which the gas entered the pipe, equal to 26, the critical Reynolds number was about 2300. After a fivefold increase in the hole area the critical Reynolds number increased by approximately 4%.At Reynolds numbers below 2000, after at a high level of the inlet pulsations an almost laminar flow had developed in the pipe, a perturbation was introduced by inserting a diametrically oriented cylindrical rod with a diameter 10–20 times smaller than the pipe diameter. In these experiments, at Reynolds numbers higher than 1000, at a distance from the rod equal to 50 pipe diameters the axial to mean-flow velocity ratio was less than 2, approaching this value again at large distances from the rod. The insertion of the rod led to a decrease in the critical Reynolds number by approximately 12%.     

Experiments in Turbulent Pipe Flow with Polymer Additives at Maximum Drag Reduction

In this paper we report on (two-component) LDV experiments in a fully developed turbulent pipe flow with a drag-reducing polymer (partially hydrolyzed polyacrylamide) dissolved in water. The Reynolds number based on the mean velocity, the pipe diameter and the local viscosity at the wall is approximately 10000. We have used polymer solutions with three different concentrations which have been chosen such that maximum drag reduction occurs. The amount of drag reduction found is 60–70%. Our experimental results are compared with results obtained with water and with a very dilute solution which exhibits only a small amount of drag reduction. We have focused on the observation of turbulence statistics (mean velocities and turbulence intensities) and on the various contributions to the total shear stress. The latter consists of a turbulent, a solvent (viscous) and a polymeric part. The polymers are found to contribute significantly to the total stress. With respect to the mean velocity profile we find a thickening of the buffer layer and an increase in the slope of the logarithmic profile. With respect to the turbulence statistics we find for the streamwise velocity fluctuations an increase of the root mean square at low polymer concentration but a return to values comparable to those for water at higher concentrations. The root mean square of the normal velocity fluctuations shows a strong decrease. Also the Reynolds (turbulent) shear stress and the correlation coefficient between the stream wise and the normal components are drastically reduced over the entire pipe diameter. In all cases the Reynolds stress stays definitely non-zero at maximum drag reduction. The consequence of the drop of the Reynolds stress is a large polymer stress, which can be 60% of the total stress. The kinetic-energy balance of the mean flow shows a large transfer of energy directly to the polymers instead of the route by turbulence. The kinetic energy of the turbulence suggests a possibly negative polymeric dissipation of turbulent energy. This revised version was published online in July 2006 with corrections to the Cover Date.     

Turbulent flow past a bubble and an ellipsoid using shadow-image and PIV techniques

An experimental investigation on flow around an oscillating bubble and solid ellipsoid with a flat bottom was conducted. A single air bubble (equivalent diameter D_e=9.12 mm) was attached to a small disk (1 mm) at the end of a needle and suspended across a vertical square channel (100 mm) by wire wherein water flowed downward at a constant flowrate. The solid ellipsoid (D_e9.1 mm) was suspended across the square channel in the same manner. The equivalent diameter-based Reynolds and Eotvos number range, 1950<Re<2250 and 11<Eo<11.5, placed the bubble in the ‘wobbly’ regime while the flow in its wake was turbulent. A constant flowrate and one bubble size was used such that flow in the wake was turbulent. Velocity measurements of the flow field around the bubble or solid were made using a one CCD camera Digital Particle Image Velocimetry (DPIV) system enhanced by Laser Induced Fluorescence (LIF). The shape of the bubble or solid was simultaneously recorded along with the velocity using a second CCD camera and an Infrared Shadow Technique (IST). In this way both the flow-field and the boundary of the bubble (solid) were measured. The velocity vector plots of flow around and in the wake of a bubble/solid, supplemented by profiles and contours of the average and root-mean-square velocities, vorticity, Reynolds stress and turbulent kinetic energy, revealed differences in the wake flow structure behind a bubble and solid. One of the significant differences was in the inherent, oscillatory motion of the bubble which not only produced vorticity in the near-wake, but as a result of apparent vorticity stretching distributed the turbulent kinetic energy associated with this flow more uniformly on its wake, in contrast to the solid.