文丘里式气泡发生器内气泡破碎机制分析

作为一种高效、安全的气泡发生装置,文丘里式气泡发生器在工业、化工等过程有广泛的应用,但对其内部气泡破碎过程和作用机制相关研究较少。前期研究发现,较大气泡进入文丘里管扩张段后会发生迅速减速,并对气泡碎化过程产生极大影响。基于大涡模拟方法,对文丘里式气泡发生器内的流动过程进行了数值模拟,发现在扩张段近壁面存在明显的涡流区,涡流区前端与上游来流发生强烈的碰撞,造成进入此区域的流体发生迅速减速,使得涡流区与主流交汇区附近静压急速增大;当此区域存在运动的气泡时,激增的压力梯度力以及附加质量力导致气泡运动速度迅速减小,并与周边流体形成了更强的相互作用;高流速条件下,会使气泡发生严重变形、甚至破碎。     

文丘里管式微气泡发生器内单气泡碎化行为的数值模拟

文丘里流道内部流场及气泡破碎过程的正确表征是提升文丘里管式微气泡发生器成泡性能和对其进行结构优化设计的基础和前提。本文借助计算流体动力学（CFD）商业软件ANSYS Fluent中的VOF多相流模型,数值模拟研究单气泡在三维流场中的变形及破碎行为,揭示文丘里流道尤其是扩张段内的流场分布和气泡碎化过程,并对文丘里管式微气泡发生器成泡粒径分布不均匀的原因进行分析讨论。CFD数值模拟结果表明,气泡碎化发生在文丘里管式微气泡发生器的扩张段内,湍流耗散率越大,碎化生成微气泡的粒径越小。扩张段内中心区域的湍流耗散率远小于边壁区域,湍流耗散率径向位置分布的差异将直接导致所生成微气泡粒径分布的不均匀。在轴心线方向上,单气泡由进水管注入时的碎化程度强于由喉管处注入;在径向方向上,单气泡由进水管偏心位置注入时的碎化程度强于由中心位置处注入。进水管内安放带导流叶片的轴向静止起旋元件,不仅可提高扩张段的平均湍流耗散率,降低生成微气泡的平均粒径,而且可以降低径向湍流耗散率的标准差,增强扩张段内径向湍流耗散率的均匀度,进而提高所生成微气泡粒径分布的均匀程度。     

轴向旋流式微气泡发生器的结构设计与数值模拟

设计了一种旋流式微气泡发生器,由环形注气机构和新型气泡破碎机构两部分组成,前者采用中心圆环+微孔板结构,后者由静止起旋元件和文丘里管组成,采用ANSYS FLUENT软件对新型气泡破碎机构的流道进行数值模拟,并与常规文丘里流道对比. 结果表明,新型气泡破碎机构流道内的水流速度、径向速度梯度、湍动能和湍能耗散率均大于常规文丘里流道,常规文丘里流道出口处产生的微气泡直径为新型气泡破碎机构的2倍. 采用响应曲面法优化静止起旋元件结构,优化后的叶片出口角度为35?,中心圆柱体直径为12.3 mm,叶片长度为10 mm,优化后的气泡破碎机构产生的微气泡直径为优化前的75%.     

流体振荡器气泡碎化特性数值模拟

为了探究流体振荡器中气泡碎化特性，采用重整化群(RNG) k-ε湍流模型和流体体积函数(VOF)多相流模型研究流体振荡器中的气液两相流。通过数值模拟分析了气泡在流场中的变形和破碎行为，考察不同流动参数对气泡破碎的影响。同时进行可视化实验，用实验结果验证了模拟的准确性。结果表明,流体振荡器可作为一种新型气泡发生装置。振荡频率越高，流体振荡器中的气泡碎化效果越好；随着液速增大，气泡变形程度加剧，破碎概率增加，生成子气泡也越多；剪切应力和涡流碰撞是导致气泡破碎的主要机制；射流振荡促使气泡向振荡腔壁面偏移，气泡初始直径越大，水平偏移量越大，越容易发生破碎。     

注气孔位置对文丘里管式微气泡发生器成泡特性的影响分析

尽管文丘里管式微气泡发生器的注气口位置会对气泡在文丘里流道内的碎化特征产生直接影响,但迄今缺乏针对性的深入研究。通过可视化实验方法,对比分析了注气口分别位于喉管处（结构1型）和进水管处（结构2型）时的气液流型、气泡破碎特征以及成泡特性。实验表明,气、液相流量对结构1型微气泡发生器内的气液流型影响显著,初始成泡区域随液相流量增加,环状流或泡状流向弹状流转变,而随气相流量增加则由泡状流或弹状流向环状流转变;结构2型微气泡发生器则在此过程中始终为泡状流,其对操作工况的适应范围大于结构1型。在相同工况下,结构1型微气泡发生器的成泡Sauter平均粒径小于结构2型,但随着液相Reynolds数的增大,二者间的成泡平均粒径差值随之减小。分析原因是由于弹状流流型下,延伸至扩张段区域的弹型泡的表面积更大,能量转化率更高,气泡界面失稳碎化的程度更显著。随着液相Reynolds数的增大,初始成泡体积减小,湍流破碎机理作用占据主导,掩盖了由于界面失稳引起的气泡破碎。结构1型微气泡发生器的成泡能耗高于结构2型,并且随液相Reynolds数的增大,两者之间的差值随之增大。综合来看,结构2型微气泡发生器能够在低能耗下实现高效成泡,面向工程应用将更具优势。     

微纳米气泡的特性表征研究

为进一步探究微纳米气泡发生系统的性能。基于喷射法原理,研究文丘里管内径、气泡发生器孔径和级数等因素对微纳米气泡粒径分布的影响。经实验测试,结果表明：当文丘里管内径由2.7 mm增至2.9 mm,气泡粒径随内径增加呈先减小后增大趋势,即气泡的平均粒径由10.88μm先减小至3.069μm,后增大至7.997μm;当气泡发生器孔径从0.7 mm增加至0.9 mm,气泡粒径随孔径增加呈递减趋势,即气泡的平均粒径由4.106μm减至2.954μm;当级数由1增至3级时,气泡粒径随级数增加基本保持一致。     

气泡微细化沸腾过程中气泡冷凝破裂现象

为了研究气泡微细化沸腾（MEB）时的气泡动力学行为,利用高速摄像仪（Fastcam SA5）观察15～60 K过冷度范围内,直径10 mm加热面上的沸腾过程。通过引入等效半径,分析核态沸腾、膜态沸腾和MEB区域的气泡行为特征。结果表明：MEB发生时的气泡行为,既不同于核态沸腾,也与膜态沸腾明显不同。在MEB区域,加热面上通常会形成一个大的、不规则气泡,但并不会脱离加热面,而是迅速破碎凝结;而且气泡生命周期相对较小,体积变化速率更快。量纲1分析发现,在MEB区域,随着壁面过热度和热通量的升高,气泡凝缩破裂过程受惯性控制影响程度逐渐增加。     

气泡微细化沸腾过程中气泡冷凝破裂现象

为了研究气泡微细化沸腾(MEB)时的气泡动力学行为,利用高速摄像仪(Fastcam SA5)观察15~60 K过冷度范围内,直径10 mm加热面上的沸腾过程。通过引入等效半径,分析核态沸腾、膜态沸腾和MEB区域的气泡行为特征。结果表明:MEB发生时的气泡行为,既不同于核态沸腾,也与膜态沸腾明显不同。在MEB区域,加热面上通常会形成一个大的、不规则气泡,但并不会脱离加热面,而是迅速破碎凝结;而且气泡生命周期相对较小,体积变化速率更快。量纲1分析发现,在MEB区域,随着壁面过热度和热通量的升高,气泡凝缩破裂过程受惯性控制影响程度逐渐增加。     

侵入式光纤照相法测量气泡尺寸分布

基于光纤内窥镜技术构建了以光纤内窥镜、图像采集系统和照明系统组成的侵入式照相装置,测量了由微气泡发生器和两种不同孔径的膜管产生的气泡的尺寸分布,并与取样照相法进行了比较. 结果表明,3种气泡生成装置产生的气泡直径在50~2000 mm;对50~200 mm气泡两种方法的测量结果相差不大,200~2000 mm的微气泡取样照相法测量值比侵入式照相法高,可能是因为取样时大气泡易发生聚并和破碎. 侵入式照相法能较准确测量较宽的气泡尺寸,适用于在线测量气液体系中分布较宽的气泡尺寸动态分布,也可用于其他测量方法及数值模拟方法的验证.     

新型预混式气动喷嘴结构设计及其工作原理

基于破碎理论设计了一种新型预混式气动喷嘴,气体作为旋流流体从切向流道通入旋流室,而待破碎液体则从喷嘴顶部中心管通入。首先采用CFD技术模拟了阶梯型、无扩张段和拉瓦尔型喷嘴的速度分布情况和喷射效果,确定最佳结构为拉瓦尔型。然后对四流道和双流道拉瓦尔型喷嘴的喷射效果进行了比较,发现流道多反而影响旋流效果。最后通过旋流气体与中心流入液体的相互影响和扩张段的减速增压作用进一步探索了双流道拉瓦尔型喷嘴的工作原理。     

A visualized investigation of bubble breakup in a swirl-venturi bubble generator

The dynamics and breakup of bubbles in swirl-venturi bubble generator (SVBG) are explored in this work. The three-dimensional movement process and breakup phenomena of bubbles are captured by one high-speed camera system with two cameras while the distribution of swirling flow field is recorded through Particle Image Velocimetry technology. It is revealed that bubbles have two motion trajectories, which are deeply related to bubble breakup. One trajectory is that mother bubble moves upward in an axial direction of the SVBG to the diverging section, and the other trajectory is that mother bubble rotates obliquely upward to another side-wall along the radial direction. Meanwhile, binary breakup, shear-off-induced breakup, static erosive breakup, and dynamic erosive breakup are observed. For relatively high liquid Reynolds number, vortex flow regions are extended and the bubble size is reduced. Furthermore, it is worth noting that the number of microbubbles increases significantly for intensive swirling flow.     

内置涡流发生器的管内过冷沸腾与强化换热的模拟

采用欧拉双流体模型结合RPI沸腾模型对高压管内过冷沸腾进行三维非稳态模拟,考察了涡流发生器对管内过冷沸腾的影响,模拟了高压下光管内的过冷沸腾、层流下内置涡流发生器的换热管内的流动和湍流下内置涡流发生器的换热管内的过冷沸腾。结果表明,内置涡流发生器的换热管在层流状态下换热能力明显提升,过冷沸腾时管内换热能力有一定提升,且壁面附近的气泡由于扰流作用被大量卷入锥形片内,降低了壁面附近产生气膜的可能性,延迟了过冷沸腾起始点的位置。     

Experiments on Bubble Breakup Induced by Collision with a Vortex Ring

The bubble breakup after collision with a vortex ring was validated as source of breakup parameters for population balance modeling. This system was chosen as a deterministic alternative to the stochastic nature of bubble breakup studies under turbulent flow. The vortex ring was characterized by combining experimental visualization and numerical simulations. Breakup frequency, mean number of daughter bubbles, and its size distribution were obtained by high‐speed camera recording of the collision process. The dependence of breakup parameters on the size of the mother bubble and Weber number was determined.     

流线型涡发生器与螺旋片强化换热器壳侧传热

为降低翅翼型纵向涡发生器与螺旋片复合强化的套管式换热器壳侧传热阻力,提出一种新型翅翼型纵向涡发生器,即流线型涡发生器。采用实验和数值模拟方法研究了流线型涡发生器与螺旋片复合强化的换热器壳侧的传热和阻力特性并与三角翼型涡发生器（DWP）的强化效果进行比较,考察了流线型涡发生器common-flow-down（CFD）和common-flow-up（CFU）两种安装方式的强化效果,分析了流线型涡发生器的减阻机理。结果表明,在涡发生器面积和迎流角相同的情况下,流线型涡发生器可以取得与三角翼型涡发生器相同（Re<8000）或略低（Re>8000）的传热系数,但其产生的流动阻力比三角翼型涡发生器低21%;在相同压降条件下,common-flow-up安装方式的综合传热效果优于common-flow-down;流线型涡发生器减阻机理在于提高了速度场与压力场的协同性。     

A unified theoretical model for breakup of bubbles and droplets in turbulent flows

Pressure has a significant effect on bubble breakup, and bubbles and droplets have very different breakup behaviors. This work aimed to propose a unified breakup model for both bubbles and droplets including the effect of pressure. A mechanism analysis was made on the internal flow through the bubble/droplet neck in the breakup process, and a mathematical model was obtained based on the Young–Laplace and Bernoulli equations. The internal flow behavior strongly depended on the pressure or gas density, and based on this mechanism, a unified breakup model was proposed for both bubbles and droplets. For the first time, this unified breakup model gave good predictions of both the effect of pressure or gas density on the bubble breakup rate and the different daughter size distributions of bubbles and droplets. The effect of the mother bubble/droplet diameter, turbulent energy dissipation rate and surface tension on the breakup rate, and daughter bubble/droplet size distribution was discussed. This bubble breakup model can be further used in a population balance model (PBM) to study the effect of pressure on the bubble size distribution and in a computational fluid dynamics‐population balance model (CFD‐PBM) coupled model to study the hydrodynamic behaviors of a bubble column at elevated pressures. © 2014 American Institute of Chemical Engineers AIChE J, 61: 1391–1403, 2015     

涡产生器翼高对管翅式换热器流动与传热的影响

采用数值模拟方法分析了三角形小翼式涡产生器翼高分别为1.5、1.75和2.0 mm时对圆管管翅式换热器空气侧传热及纵向涡强度的影响。结果表明：在相同Re下,随着翼高的增加,Nu、阻力系数 f 以及量纲1二次流强度Se_m都增大;所研究各模型的Se_m与Nu呈唯一对应关系,并且获得了Se_m与Nu的定量关系;以强化传热因子JF作为评价准则,得出翼高为1.75 mm时能够使换热器获得较优的综合强化传热效果。     

Generation of Coarse Bubbles and Flow Instability Control by Means of a Bubble Generator

A previously studied bubble generator was tested under new operating conditions to provide for millimeter‐sized bubbles. The basic element of the generator is a vortex chamber with water supplied through tangential ducts while gas (air) is introduced in the radial direction. Bubbles with average diameter of 0.5–2.2 mm were produced and registered by high‐speed photography. The correlation between the water‐air flow rate ratio and the characteristic bubble diameter was established and described by a relationship. Pressure oscillations in the exit section of the device were captured for two‐phase flows with fine and coarse bubbles. With a view to applications in membrane filtration and water treatment, the effect of a pin installed in the exit section of the vortex chamber on the pressure oscillations was studied. The pin results in a drastic increase in pressure amplitude, both in the flow without bubbles and in the case of gas supply.     

Liquid recirculation and bubble breakup beneath ventilated gas cavities in downward pipe flow

The dispersion of bubbles into down-flowing liquids is often encountered in a number of industrial applications involving pipe flow, bubble columns and loop reactors. Usually a gas horizontal sparging device is used to generate bubbles that are carried downward with the bulk liquid flow. At low gas flowrates discrete bubbles are formed. However, at higher gas flowrates a ventilated cavity attached to the sparger is formed. For downward pipe flow the liquid forms an annular jet, which entrains gas into the recirculation region immediately beneath the ventilated cavity. The rate of gas entrainment and the size of the bubbles produced is determined by the pipe diameter, liquid and gas volumetric flowrates and the strength of the recirculation region below the base of the ventilated cavity. In this study a model was developed to predict the liquid velocity field and bubble breakup in the recirculation region. The velocity profile was modelled using the potential flow solution of the Hill's vortex, where the strength of the vortex was assumed to be directly proportional to the velocity of the annular wall jet. The proportionality constant was found to be 0.38, based on predictions obtained using the commercial code CFX. The CFX velocity profile predictions for the central part of the recirculation region were very similar to the Hill's vortex velocity profile. Bubble breakup was modelled using a critical Weber number concept, based on the predicted velocity profile within the recirculation region. It was found that the prediction of bubble size was in general agreement with experimental observations when a critical Weber number of 4.7 was assumed. A digital high-speed video was used to observe the liquid and bubble motion at the base of the ventilated cavity. The video was used to obtain estimates of the recirculating liquid flow velocity, which compared reasonably well with predictions based on the Hill's vortex model. The video evidence also highlighted the unsteady nature of the flow, particularly the actual gas entrainment process, and possible reasons for this behaviour are presented.     

Slug bubble deformation and its influence on bubble breakup dynamics in microchannel

The deformation of moving slug bubbles and its influence on the bubble breakup dynamics in microchannel were studied. Three bubble morphologies were found in the experiment: slug, dumbbell and grenade shapes. The viscosity effect of continuous phase aggravates the velocity difference between the fluid near the wall and the bubble, resulting in that the continuous phase near the bubble head flows towards and squeezes the bubble tail, which causes the deformation of bubbles. Moreover, the experimental results show that the deformation of bubbles could significantly prolong the bubble breakup period at the downstream Y-junction. There exists the critical capillary number Ca_Cr for the asymmetric breakup of grenade bubbles, Ca_Cr increases with the rise of flow rate and viscosity of the continuous phase.