液-固流化床中单个变形气泡的上升速度

以气泡在上升运动过程中的受力分析为基础,建立了描述单个变形气泡在液－固流化床中上升速度的理论模。应用该模型分别对球形和球帽形气泡在液－固流化床中的上升速度进行了计算,并将计算民在不同的床内压力,温度与颗粒相体积分数下气泡上升速度的实验测量数据进行了比较。     

SEBS高黏度溶液气液鼓泡塔的流体力学研究

针对SBS加氢反应器开发与设计,以SEBS-1650己烷溶液为液相,采用差压法和床层塌落法研究了气液鼓泡塔中高黏度溶液的流体力学行为,考察了黏度对低表面张力溶液的气含率、大小气泡气含率、大小气泡上升速度和比表面积等因素的影响。结果表明,随黏度增加,大气泡增多,气含率明显降低,塔内流型处于湍流区;由床层塌落曲线确定鼓泡塔内存在三种类型的气泡：大气泡、小气泡及细小气泡,随黏度增加,小气泡与细小气泡逐渐减少;黏度对大小气泡的上升速度略有影响,比表面积随黏度增加而明显降低。根据实验结果给出了大小气泡气含率与平均气含率的计算公式。     

单气泡沿倾斜绝热表面运动特性的LBM方法研究

气泡沿斜面运动现象在工业生产中广泛存在,采用格子Boltzmann方法(LBM)研究单个气泡沿倾斜绝热表面的运动过程,考察气泡的初始直径、斜面倾角、Eotvos数(Eo)对气泡的变形和气泡形心与斜面垂直距离的影响,探讨相同初始直径的气泡沿斜面运动的稳定终态速度与倾角和Eo之间的关系。通过模拟得出气泡沿斜面的运动规律:斜面倾角越大,气泡前后端不对称性越大;气泡在上升过程中,形心轨迹与斜面保持平行;当倾角大于45°时,形心与斜面的垂直距离和Eo变化一致,当小于45°时,变化相反;相同初始直径气泡的稳定终态速度随倾角和Eo的增加而增加。     

不同固相黏度模型对鼓泡床气泡行为的数值模拟

基于双流体模型,应用Fluent软件包对带有单喷嘴的二维鼓泡床中气泡行为进行数值模拟。采用常固相黏度模型(CPV)和基于颗粒动理学的固相黏度模型(KTGF),通过计算气泡的形成、气体泄漏率、气泡直径及气泡上升速度对不同模型进行比较研究,其中编程实现了KTGF模型中的Lun等模型与Hrenya和Sinclair模型模块。通过与文献中的实验数据进行对比发现KTGF模型普遍优于CPV模型,其中Lun等模型与Hrenya和Sinclair模型的模拟值最接近实验数据。     

黏弹性流体中单气泡上升速度的研究

为了揭示黏弹性流体中单气泡的运动规律,采用高速摄像技术对聚丙烯酰胺(PAA)溶液中单气泡的运动行为进行了研究。通过Matlab 10.0利用自编程序得到了气泡的上升速度,考察了溶液流变性质和表面活性剂对气泡上升速度的影响。结果表明:气泡的上升速度随体积的增大而增大,并发生速度跃迁现象,发生跃迁时的临界体积随溶液黏弹性的增大而减小,随表面活性剂浓度的增大而增大。气泡形状的变化与速度跃迁相关,当气泡体积低于临界体积时,气泡的形状为球形或椭球型,当气泡体积高于临界体积时,气泡出现了尖端尾部,且尖端尾部两侧界面向气泡内部凹进。提出了预测气泡速度跃迁的临界条件,预测值与实验值重现性较好。     

鼓泡塔反应器的两级气泡模型参数研究

为了研究鼓泡塔反应器两级气泡模型在高黏度下的适用性,采用动态气体逸出法,在内径为286 mm,总高为7 200 mm的鼓泡塔中考察了液体黏度(1.2×10-3—210.4×10-3Pa·s)和操作条件对塔内总气含率,大、小气泡相含率和大、小气泡上升速度等两级气泡模型参数的影响。结果表明:床层总气含率随表观气速的增加而增大,大气泡相含率受液体黏度的影响较小,受表观气速的影响较大;小气泡相含率随黏度的增加而迅速下降,在高气速时受表观气速的影响较小。大、小气泡上升速度均随液体黏度的增加而降低,但随表观气速的升高有着不同的变化关系:前者明显升高,后者略有降低。大气泡直径随着黏度增大而稍有增大,小气泡直径随着黏度增大急剧减小。     

基于图像处理的气固流化床中气泡行为的分析

以数字图像处理为基础,实现对流化床中气泡的成长、聚合和分裂行为的分析.利用高速摄像机拍摄气固两相流的气泡运动图像,从中选取气泡上升、聚舍和分裂三种典型图像序列.经过图像处理后,分别对其进行气泡识别和参数的获取.然后根据获取的数据,首先分析了气泡上升过程中面积、形心、等效直径等参数的变化趋势和变化规律,接着对聚合中的聚合...     

基于传质强化的微气泡塔盘流动特性实验的研究

筛板塔塔内件的作用主要是增大气液比表面积,改变气液接触形式,以提高塔内传质、传热。研究者提出了新型微气泡塔盘,通过在筛板上方的泡沫层内增加破泡组件,利用破泡组件使大气泡破裂为小气泡,增加气液接触面积,提高气液传质、传热效果。利用自行设计的筛板塔和微气泡塔盘实验平台及PIV测速系统,测定了塔板上气泡的直径分布和上升速度。实验结果显示:与普通筛板相比较,微气泡塔盘上气泡的上升速度较小,气泡停留时间更长,且径向分布更平坦;气泡直径也仅为筛板的1/16,气液接触的比表面积增大,更利于传质过程的进行。     

气液外环流反应器中气泡行为的实验研究

详细考察了气液外环流反应器中上升管、下降管的气泡行为随轴向、径向的变化规律. 由于外环流反应器的结构特点,发现在上升管底部存在偏流,并对分布板区气泡行为随角向的变化规律进行了研究. 分析实验结果得出,气含率和气泡速度均随表观气速的升高而升高;在上升管内,气含率和气泡速度自中心向边壁逐渐降低,而沿轴向变化很小;在分布板区,由于受分布器及下降管的影响,使气含率和气泡速度在不同角向存在不同的径向分布. 在下降管中,气含率自中心向边壁逐渐降低,而气泡速度则基本不变;且下降管中的气体循环率随表观气速的升高而升高.     

气泡长大法测定表面活性剂溶液的表面扩展黏度

在理论分析的基础上 ,采用计算机图像采集技术 ,实时记录气泡的长大过程 ,用图像分析技术确定气泡边缘形状 ,建立了根据气泡图像测定表面扩展黏度的实验装置 .直接测量动表面张力随时间的变化 ,并通过动表面张力与气泡表面积变化率的关系 ,确定溶液的表面扩展黏度 .测定了十二烷基硫酸钠溶液的表面扩展黏度 ,并与不同表面变形速率下的文献值进行比较 ,说明了表面活性剂溶液的表面流变现象 .     

大孔径高气速单孔气泡形成

在内径为190mm的鼓泡塔内,研究了空气-去离子水系统在大孔径高气速条件下的单孔气泡形成。考察了五个不同的孔径,分别为4、8、10、15及21mm,孔口气速范围为0.8~154.8m·s^-1。以CCD摄像记录气泡的形状及尺寸,根据气泡长径比的变化,得到气泡初始形态转变时的临界孔口气速：当孔口气速低于20m·s^-1时,孔口气泡近似于球形,长径比小于1.1;当孔口气速大于50m·s^-1时,气泡呈现椭球形,长径比大于1.5。并对气泡尺寸与孔径及孔口气速进行关联,所得关联式对孔径大于3mm、孔口气速在10~80m·s^-1范围内所形成的气泡尺寸预测效果较好。     

特征时间对剪切稀化流体气泡上浮特性的影响

非牛顿气液两相流广泛存在于工农业生产中,气泡和液相间的接触非常复杂,对相间的传递效率具有重要的影响。为了理解气泡在非牛顿流体中的运动特性,基于连续表面张力模型与Carreau本构模型,本文运用volume of fluid（VOF）法研究了单气泡在剪切稀化流体内自由上浮的运动特性。研究发现：气泡的动力学特性与液相的特征时间λ密切相关,液相的剪切稀化程度越强（流变指数n越小）或表面张力越小（Eo数越大）时,特征时间λ对气泡变形和尾涡的影响越大。在给定的剪切稀化程度和表面张力下,λ越大,气泡终端速度越大,其尾涡强度和尺度也越大,导致气泡周围液相高剪切速率区和低表观黏度区的范围越宽。此外,当液相的表面张力较小时,在气泡尾部出现了黏度盲区;并且随着λ的增大,黏度盲区逐渐脱离气泡尾部并破碎;黏度盲区的出现减小了气泡周围液相低表观黏度区的面积,增大了气泡上浮过程的摩擦阻力,降低了气泡的终端速度。     

Buoyancy-driven motion of bubbles in square channels

The motion of air bubbles in square capillaries moving under the influence of gravity is studied over a range of Reynolds numbers. The steady shapes and velocities of the bubbles as a function of the bubble size are determined experimentally at moderate Bond and capillary numbers. Bubbles are nearly spherical at lower bubble volumes and become prolate losing their fore and aft symmetry at larger bubble volumes. At higher Weber numbers, a reentrant cavity develops at the rear of bubble. The critical Weber number at which this shape transition occurs lies between 0.89 and 1.38. At small Weber numbers, the terminal velocity of bubbles increases monotonically with bubble volume and eventually reaches a plateau value, which is independent of the bubble size. At higher Weber numbers, a maxima develops in the velocity-volume curve at moderate bubble sizes which grows in magnitude as the Weber number increases. Even at small bubble volumes with nearly spherical shape, the terminal velocity of the bubbles is less than the Hadamard-Rybczynski velocity due to the wall drag. The speed and the maximum bubble width for air bubbles rising in a square channel is higher than that of an air bubble rising in a circular channel with the same hydraulic diameter. The experimental data compares well with predicted trends in the viscous and inertial limits for long bubbles.     

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.     

树脂中气泡运动速度的影响因素

孔隙是影响复合材料性能的重要因素之一,而孔隙的形成与复合材料制造过程中所产生的气泡密切相关.为了有效地减少复合材料成型过程中的气泡、控制制品的孔隙含量,了解气泡在纯树脂中的运动过程是十分必要的.本文借助图像跟踪和数码采集照相系统,研究了气泡体积、树脂粘度、外压、树脂种类和树脂流动状态对单个气泡运动规律的影响.结果表明,气泡的运动速度随着气泡体积的增加、树脂粘度的减小及外界压力的减小而增大.此外,树脂种类和树脂流动状态对气泡的运动速度也有较大的影响.该研究结果将为复合材料成型过程中气泡运动模型的建立提供实验依据.     

采用压力传感技术测量鼓泡床中流体力学参数

引　言鼓泡床以其良好的传热、传质、相间充分接触和高效的可连续操作特性在许多领域得到了广泛应用 .在过去的 4 0多年里 ,人们采用许多测量方法(光导纤维、多普勒测速仪、电导法、压力传感技术 )对鼓泡床中的各种流动行为进行了大量研究 ,由于床层内流动的复杂性以及各测量手段间的差别 ,得出的结论不尽相同[1] ,而且工业反应多数在高温、高压、非透明体系下进行 ,这限制了许多测量技术的应用 .压力传感技术以其适用范围广、所需仪器便宜、耐用、测量结果准确的特点在鼓泡床流体力学参数测量中得到了广泛应用床层塌落法是压力传感技术在鼓泡床流体力学参数测量中的一个重要应用 .Sriram和Mann[2 ] 较早地将其应用于测量鼓泡床中的气含率 ;Fan等[3] 也曾利用此方法测量鼓泡床内的固含率 .前人大都采用压力传感技术测量床层内的平均相含率 ,而采用此方法测量大小气泡分数和气泡上升速度的报道很少 .本文根据前人在此方面的研究成果并结合本实验的特点进行了这方面的研究1　实验装置本实验结合工业对二甲苯氧化反应器的特点设计并建立了其流体力学冷模实验装置 ,如图 1所示 .鼓泡床高 6 6m ,内径 0 3m .在鼓泡床一侧自...     

Behaviour of a large bubble flowing through a sudden constriction between a cylindrical pipe and a rectangular cross section channel

The behaviour of a single large bubble flowing through a sudden constriction between a cylindrical pipe and a channel of rectangular cross section is studied experimentally. Two types of constrictions are considered: an abrupt one and a smooth one. Image analysis displays the deformation of the large bubble generated in the upstream vertical pipe and flowing through each kind of constriction. Image processing allows an estimate to be made of the velocity of Dumitrescu bubbles upstream of the constriction and the velocity of a 2D cap bubble flowing downstream of the constriction in a rectangular-cross-section channel. When the large bubble flows through a constriction, its behaviour can be considered in two steps: a first step corresponding to the disengagement of the large bubble and a second step corresponding to its transient behaviour after detachment. In terms of disengagement, an abrupt constriction induces systematic break-up of the large bubble whereas, with a smooth constriction, the large bubble undergoes strong deformations but does not break up. After detachment, large bubbles relax in a similar way and their velocities tend towards the terminal velocity of the 2D cap bubble.     

Bubble breakup with permanent obstruction in an asymmetric microfluidic T‐junction

Bubble breakup with permanent obstruction in an asymmetric microfluidic T‐junction is investigated experimentally. The breakup process of bubbles can be divided into three stages: squeezing, transition, and pinch‐off stages. In the squeezing stage, the thinning of the bubble neck is mainly controlled by the velocity of the fluid flowing into the T‐junction, and the increase of the liquid viscosity can promote this process. In the transition stage, the minimum width of bubble neck decreases linearly with time. In the pinch‐off stage, the effect of the velocity of the fluid flowing into the T‐junction on the thinning of the bubble neck becomes weaker, and the increase of the liquid viscosity would delay this process. The evolution of the minimum width of the bubble neck with the remaining time before the breakup can be scaled by a power–law relationship. The bubble length has little influence on the whole breakup process of bubbles. © 2014 American Institute of Chemical Engineers AIChE J, 61: 1081–1091, 2015     

Experimental measurement of bubble breakup in a jet bubbling reactor

The bubble breakups in a jet bubbling reactor are captured using a high-speed camera and the velocity field is measured by particle image velocimetry. Two typical breakup patterns, jet breakup and jet-vortex breakup are observed. The breakup time interval of the jet-vortex breakup is two orders of magnitude higher than the jet breakup. The probability of the jet-vortex breakup and the jet breakup accounting in the total breakup events increases and decreases with the jet velocity and the mother bubble size, respectively. The bubble breakup region increases with the jet velocity. The bubble breakup frequency increases with the turbulent dissipation rate and the mother bubble size. The average number of daughter bubbles increases with the Weber number. An L-shaped daughter bubble size distribution is observed. Empirical correlations are established for the bubble breakup frequency, the average number of daughter bubbles and daughter bubble size distribution, and fitted well with the experimental results.