低温气液两相弹状流动中Taylor气泡的统计特征?I. Taylor气泡长度

为了研究倾角(q)和管径对低温气液两相流中Taylor气泡长度分布规律的影响,在6种管路倾角下,以液氮为工质,使用高速相机对4种内径透明抽真空Pyrex玻璃管内的弹状流动进行了可视化实验. 结果表明,低温弹状流动中Taylor气泡长度分布的统计特征可由对数正态分布函数描述,Taylor气泡长度分布的标准偏差受到液膜射流直接影响,并随q减小先增大后减小. Taylor气泡无量纲平均长度随管路轴向位置增大而线性增加,随管路内径增加呈指数下降趋势,随q减小而增大,最小值出现在70o≤q≤90o.     

低温气液两相流中Taylor气泡的合并

在自建的低温气液两相流实验平台的基础上,通过高速相机获得16 mm内径管路中30o~90o倾角下Taylor气泡之间的合并过程. 结果表明,已有的常温气液两相流中Taylor气泡的合并公式普遍高估了跟随气泡和领先气泡的速度比,与实验结果的最大误差为14.6%,对低温气液两相流不再适用. 新建的Taylor气泡合并过程速度拟合公式可将最大误差减小至4.7%. 此外,气泡间最小稳定距离在60o倾角附近最小,此时气泡间合并趋势最弱.     

运用单元系综平均方法研究"层流"泡状流压力场

在考虑真实流体粘度、忽略气泡尾迹区影响的前提下,通过对真实流体绕球形气泡的流场进行研究,运用单元系综平均方法推导出液相界面平均压力与液相平均压力差pli-pl的表达式,反映了液体粘度对该压力差的影响. 由于湍流泡状流相对雷诺数较大,无法忽略尾迹区对其气泡周围压力场的影响,因此该表达式只适用于"层流"泡状流.     

采用大涡PIV方法研究搅拌槽内湍流动能耗散率

在槽径为0.476 m的六直叶涡轮桨搅拌槽内,采用粒子图像测速仪(PIV)对桨叶区的流场进行了实验研究,得到了桨叶区的平均流速和湍流动能(k)分布,采用大涡PIV方法对湍流动能耗散率(e)分布进行了估算,计算了e与k的相关系数. 结果表明大涡PIV方法能有效地估算e分布;桨叶区的射流向上倾斜,两尾涡分布于射流两侧,射流的倾角和两尾涡中心间距随射流向壁面运动而变化,射流倾角先增大再减小,相位角q=40o时达到最大值13.2o,两尾涡中心间距先减小再增大,q=20o时达到最小值0.0387(用槽径T无因次化);湍流动能和湍流动能耗散率峰值均位于尾涡靠近射流的区域;湍流动能和湍流动能耗散率的平均相关系数为0.363,射流核心区相关系数小于周边区域.     

旋转管式膜分离器流场测试

采用理论和实验结合的方法系统地研究了旋转管式膜分离器内的流场特征.理论部分讨论了膜器内流体运动的稳定性,得出无轴向流和渗透流时Taylor涡的流线以及有轴向流和渗透流时临界Taylor数的表达式.实验部分采用激光粒子成像测速系统(PIV)对膜器环隙间的流场进行实测,分别测试了无轴向流和渗透流、有轴向流而无渗透流、轴向流和渗透流同时存在时膜器环隙间的流场.最后分析了环隙子午面流体的轴向和径向速度分布,理论和实验结果一致.     

双组水平喷嘴撞击流反应器流场POD分析

利用二维高速粒子图像测速技术研究双组分层水平对置撞击流湍流场,考察了双组喷嘴在不同Re、不同直径及上下径向射流不同工况下的流动结构,对速度场进行POD分解,提取流场中含能大尺度结构。结果表明,低阶本征模态拥有大尺度涡旋结构,流场涡旋结构明显,瞬时流场能量主要集中在一阶模态,易于描述整个流场的流动特征,脉动场的模态重构可以准确还原流场中的涡结构。L=3d工况下,不对称流场能量高于对称流场;低阶模态能量随喷嘴Re的增大而增大,而随喷嘴直径增大呈先递增后递减的趋势,直径d=10 mm的工况下所对应的一阶模态能量最高,涡强最大。     

双组水平喷嘴撞击流反应器流场POD分析

利用二维高速粒子图像测速技术研究双组分层水平对置撞击流湍流场,考察了双组喷嘴在不同Re、不同直径及上下径向射流不同工况下的流动结构,对速度场进行POD分解,提取流场中含能大尺度结构。结果表明,低阶本征模态拥有大尺度涡旋结构,流场涡旋结构明显,瞬时流场能量主要集中在一阶模态,易于描述整个流场的流动特征,脉动场的模态重构可以准确还原流场中的涡结构。L=3d工况下,不对称流场能量高于对称流场;低阶模态能量随喷嘴Re的增大而增大,而随喷嘴直径增大呈先递增后递减的趋势,直径d=10 mm的工况下所对应的一阶模态能量最高,涡强最大。     

幂律流体中平行上升双气泡间相互作用研究

采用流体体积(VOF)法对非牛顿幂律流体中平行上升双气泡间相互作用进行了模拟研究.结果表明:剪切变稀效应及气泡周围流场结构对气泡间相互作用的贡献分别随着气泡间距增大而减小,气泡间相互作用主要受气泡间流体涡旋结构控制.当初始间距很小时,气泡平行聚并发生;随着初始间距增大,双气泡行为转变为相互影响的平行上升;当初始间距增大...     

无挡板涡轮桨搅拌槽内湍流流动的分离涡模拟

采用分离涡模型对无挡板涡轮桨搅拌槽内的湍流流动进行了研究,重点分析了流场结构和速度分布,以检验该模型模拟搅拌槽内流体流动的有效性和正确性. 为了加快收敛,先采用标准k-e模型进行稳态流场计算,并以此结果为初始值进行分离涡模拟. 与现有文献大涡模拟及实验结果对比表明,分离涡模型能捕捉槽内流体的瞬时流动特征,获得的时均速度分布与大涡模拟及实验结果吻合较好,其中对切向速度分布的预测误差不超过7%,对径向速度分布的预测精度则低一些,局部误差接近12%. 分离涡模型适用于无挡板涡轮桨搅拌槽内湍流流动的模拟,能获得与大涡模拟相近的结果,且计算量更小(约为大涡模拟的1/3).     

剪切稠化流体内气泡上浮运动特性

剪切稠化流体是一种典型的非牛顿流体,研究气泡在其中的运动特性对优化设备结构、提高反应效率具有重要意义。文中采用流体体积(VOF)法,通过改变Gallilei数(Ga)、E?tv?s数(Eo)与流变指数(n),对牛顿流体(n=1)及剪切稠化流体(n>1)内气泡的形状、尾涡、终端速度和气泡周围液相黏度分布的变化进行了深入的数值研究。结果表明:气泡变形程度和尾涡尺寸随着Ga数或Eo数的增大而增加;剪切稠化效应会阻碍尾涡的形成,减小气泡的尾涡尺寸;气泡周围剪切速率的差异会导致气泡上方及尾部产生高黏度区域,该高黏度区域会随剪切稠化效应的增加而增大;气泡终端速度随Ga数的增大或流变指数n,Eo数的减小而增大。     

Analysis of dominant flow structures and their flow dynamics in chemical process equipment using snapshot proper orthogonal decomposition technique

Snapshot proper orthogonal decomposition (POD) technique has been applied to reveal the dominant flow structures, their dynamics and length scales in six widely used industrial equipments (stirred tank, bubble column, Taylor-Couette flow (annual contactor), ultrasonic reactor, jet reactor, and channel flow). The variation in length scale of structures within an equipment, with change in its operating conditions (Reynolds number and power input) or change in its geometric configuration (sparger and impeller designs), has been brought out in this work. The planar data set for POD analysis was obtained from particle image velocimetry (PIV) and large eddy simulation (LES) studies. The dominant spatial topology was analyzed by using the velocity and vorticity POD modes. The modes have revealed the following flow structures: the ascending streaks and bursts in channel flow, the vortex tube and leading edge vortices in jets, the irregular small chaotic vortices in Taylor-Couette flow, the variation in plume oscillation and flow structures in the vortical region of bubble column resulting from changes in sparger design, the high intensity vortices near the source of ultrasound in the ultrasonic reactor and the effect of impeller designs on dominant flow structures and near blade vortices in the stirred tank. The length scales of structures are obtained by applying image processing on the spatial modes. The dynamics of these flow structures in each of the items of equipment is captured by reconstructing the flow field using appropriate spatial and temporal modes that contribute to these structures. Further, a unique attempt has been made to correlate the length scale distribution with the mixing time.     

倾斜管内低温液弹和Taylor汽泡的长度分布

An experimental study was carried out to understand the phenomena of the boiling flow of liquid nitrogen in an inclined tube with closed bottom by using a high speed motion analyzer.The experimental tube is 0.018 m ID and 1.0 m in length.The range of the inclination angle is 45°-90° from the horizontal.The experiment focused on the effect of the inclination angle show that the mean liquid slug length and Taylor bubble length increase with the increasing x/D at various inclination angles.At the same x/D,the mean liquid slug length and Taylor bubble length increase first,and then decrease with decreasing inclination angles,with the maximum at 60°.In the vertical tube,standard deviation of the nitrogen Taylor bubble length increase with the increasing x/D.For the inclined tube,standard deviation of the nitrogen Taylor bubble length increases first,and then decreases with the increasing x/D.Standard deviation of the liquid slug length increases with increasing x/D for all inclination angles.     

Flow around individual Taylor bubbles rising in stagnant CMC solutions: PIV measurements

The flow around single Taylor bubbles rising in non-Newtonian solutions of Carboxymethylcellulose (CMC) polymer was studied using simultaneously particle image velocimetry (PIV) and shadowgraphy. This technique made it possible to determine the correct position of the bubble interface. Solutions of polymer with weight percentage varying from 0.1 to 1.0 wt% were used to cover a wide range of flow regimes. The rheological fluid properties and pipe dimension yielded Reynolds numbers between 4 and 714 and Deborah numbers for the higher concentration solutions between 0.001 and 0.236. The shape of the bubbles rising in the different solutions was compared. The flow around the nose of the bubbles was found to be similar in all the studied conditions. Velocity profiles in the liquid film around the bubble were measured and different wake structures were found. With increasing solution viscosity, the wake flow pattern varied from turbulent to laminar, and a negative wake was observed for the higher polymer concentration solutions.     

Flow patterns in the wake of a Taylor bubble rising through vertical columns of stagnant and flowing Newtonian liquids: An experimental study

The flow in the wake and near-wake regions of individual Taylor bubbles rising through stagnant and co-current vertical columns of Newtonian liquids was studied, employing simultaneously particle image velocimetry (PIV) and pulsed shadowgraphy techniques (PST). Experiments were made with water and aqueous glycerol solutions covering a wide range of viscosities , in an acrylic column of 32 mm ID.Different wake structures (laminar, transitional and turbulent) are identified, in both stagnant and co-current flow conditions. In stagnant liquids, the wake flow pattern is only dependent on the dimensionless group N_f. The different types of wakes obtained are in accordance with the critical N_f numbers proposed in previous works. For co-current flow conditions, the flow patterns in the wake depend on the Reynolds number based on the relative (to the bubble) average velocity of the upward liquid flow, the laminar-transitional and transitional-turbulent limits being for the first time experimentally determined.The wake flow patterns are quantified by means of instantaneous and average flow fields. Values for the wake length and wake volume are also presented and compare well with correlations found in literature. Study of the flow in the near-wake zone enabled determination of the distance needed to recover the undisturbed liquid velocity profile.The detailed study of the flow in the wake and near-wake regions is an important contribution to better understanding the interaction and coalescence mechanisms between Taylor bubbles.The data reported are relevant to the validation of numerical simulation codes in the vertical slug flow regime.     

毛细管内气液Taylor流动的气泡及阻力特性

采用相对坐标系方法,研究毛细管(d 2mm)内充分发展垂直上升气液Taylor流动,分析两种工作介质下Taylor气泡的形状、上升速度、液膜厚度以及压降特性。结果表明:随着两相表观速度(V_tp)增大,Taylor气泡长度增大,气泡尾部曲率半径增大。气泡长度及内部回流区随着气泡体积分数(ξ_g)增大而增大,量纲1液膜厚度与气泡上升速度与毛细数(Ca)正相关,模拟结果与经验公式吻合较好。摩擦阻力因子(f_c)随V_tp与ξ_g的增大而降低,N₂/乙二醇为工质的Taylor流动f_c低于单相情况,而N₂/水为工质的Taylor流动f_c高于单相情况。Kreutzer等的流型依赖公式以及Lockhart等的分离模型可较好预测本文的两相压降,模拟结果与预测值的误差在±10%以内,常规通道所推荐C 5仍然适用于本文毛细管情况。     

Origin of the negative wake behind a bubble rising in non-Newtonian fluids

The present work aims at understanding the behavior of individual bubbles in non-Newtonian fluids. By means of a Particle Image Velocimetry (PIV) device, the complete flow field around either a single non-spherical bubble rising in polyacrylamide (PAAm) solutions or a solid sphere settling down in the same fluids shows for the first time the similar coexistence of three distinct zones: a central downward flow behind the bubble or the sphere (negative wake), a conical upward flow surrounding the negative wake zone, and an upward flow zone in front of the bubble or the sphere. This excludes then the possible influence of the interface deformation on the negative wake. A theoretical lattice Boltzmann scheme coupled to a sixth-order Maxwell model was developed for computing the complex flow field around a solid sphere. The good agreement with the experimental measurements provides evidence that the physical mechanism responsible for the negative wake in such fluids could be related to the fluid's viscoelastic properties.     

弹状流液弹区含气率分布的试验研究

采用光纤探针法和高速摄影法对垂直上升气液两相弹状流的液弹区含气率分布进行了试验研究,测试管径为15 mm。一种基于机器学习的图像处理技术用来识别气液两相界面,通过搭建气泡边界提取的神经网路系统,使用构建的气泡边界数据库对模型进行多次迭代训练,该方法可以有效地识别多种复杂类型的气泡边界。试验得到了弹状流液弹区的径向含气率分布曲线,结果表明,壁峰分布是液弹区含气率分布的主要形式,其中泰勒气泡的尾迹效应对分布形式有重要影响,尾迹的旋涡中心和含气率分布的峰值相对应。针对弹状流液弹区径向含气率分布的两个主要特征——中心局部含气率和壁峰位置,分别提出了相应的预测公式,且与本文的试验数据吻合良好。     

垂直及倾斜上升管内气液两相弹状流壁面切应力的模拟

用VOF模型对垂直及倾斜上升管内弹状流壁面切应力进行数值模拟。计算结果表明,垂直上升流动时,液膜厚度始终小于对应位置倾斜上升弹状流的液膜厚度,壁面切应力从气弹头部至尾部逐渐增大至恒定不变,在尾流区呈杂乱无章状态。倾斜上升流动时,气泡头部顶点偏向管中心线上方,倾角越小,相同轴向位置处测得的液膜厚度越大。当FrTB较小时,倾斜管内弹状流上管壁面的切应力曲线在液膜区有明显波动,而下管壁面在对应区域的切应力分布则比较光滑。随着FrTB的增大,上下壁面切应力分布曲线越来越靠近。