应用电导探针法测定气泡参数

采用照相法对研制的双电导探针测定气泡参数的测量系统■进行标定,并将其用于测定槽径为(?)0.287m 的搅拌槽内的气泡运动速度、气泡大小分布。     

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。     

两相流中气泡和液滴的直径及其分布的自动测量

<正>气泡、液滴大小及概率密度分布对研究气液及液液两相流设备中的能量传递、反应过程以及设备和工艺的最优化设计等,具有十分重要的意义.以往,测量液滴、气泡大小分布主要采用照相法、化学法、电阻探针法等,这些方法应用范围窄,或者费时长、精度低.     

搅拌槽中气泡大小分布规律的研究

运用改进后的光电毛细管探头技术测量了搅拌槽中较宽操作条件范围内的气泡大小分布,由湍流理论分析了叶轮区和循环区影响气泡大小的主要因素,得到了气泡大小空间分布的初步规律及不同区域内的气泡平均直径与操作条件之间的定量关系.     

微分散法连续制备微气泡的研究进展

微气泡的尺寸介于1~1000 μm之间。相比于传统大气泡,微气泡具有体积小、比表面积大、上浮速度慢和传质效率高等优点,被广泛应用于石油、化工、食品、化妆品、医学和废水处理等领域。相比于传统的微气泡制备方法,气液微分散法制备微气泡生产效率高、可控性好、灵活性高和易于放大,受到了学者们的广泛关注。鉴于微气泡的广泛应用,快速准确的对气泡的大小和尺寸分布的表征也至关重要。本工作对常用的微气泡尺寸表征方法进行了归纳总结,比较了不同的微气泡制备方法的优缺点,并重点阐述了微通道法和膜分散法制备微气泡的研究现状。在此基础上对微分散法制备微气泡的未来研究方向进行展望。     

喷嘴释放单气泡的声发射特性

利用声发射技术在单气泡发生实验装置中研究了气液两相流中单气泡的动力学特性,使用自行开发的采集处理程序进行气泡声信号的参数提取,采用统计分析、小波变换和快速傅里叶变换对声信号进行时域和频域范围的分析。分析结果表明,声发射技术可以检测到管内气泡的声信号,具有较高的信噪比,且声信号随着喷嘴尺寸的增大而增大,随着液相表面张力的减小而减小。比较不同喷嘴直径下气泡的频率谱,发现喷嘴释放气泡发出的声信号频率为150～200 kHz,且随着喷嘴直径的增大,峰值频率相应增大,提出了声信号峰值频率与气泡尺寸之间的关联式。同时得到了气泡上升过程中的连续形态变化,分析了气泡产生声音的机理。研究表明,声发射技术是一种灵敏度高、测量手段方便的方法,可用于气液两相流气泡运动特性的检测。     

微通道内气-液两相传质过程行为及其应用

微通道内气-液两相体系中Taylor流和泡状流具有气泡尺寸均一、停留时间分布窄、可调控性强和比表面积高等优点,具有广泛的应用前景。从Taylor气泡和泡状气泡的传质过程出发,系统综述了微尺度下气泡的溶解规律、传质过程机理和传质/溶解模型等方面的研究进展,并介绍上述流型在反应或过程强化、基础物性及动力学数据测量和微纳材料合成方面的应用。最后总结并展望了技术领域的研究难点与研究方向。     

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。     

三相循环流化床中气泡上升速度的实验研究

开发了一种新型的光纤探头多相流气泡测试系统,可用于气－液两相和气－液－固三相体系中气泡参数的测定。应用此系统研究了三相循环流环化床中不同径同位置气泡的上升速度分布,气泡上升速度均值的径向布以及操作条件对这现任中分布的影响。     

高速剪切流剪切形成微气泡的研究

气浮工艺中气泡的大小是衡量气炮制造技术的关键.研究了利用陶瓷微孔膜管在高速剪切流剪切作用下形成微气泡的条件,流体物性对气泡粒径分布的影响.试验采用静态显微摄像技术和图像分析系统对气泡粒径分布进行了表征.结果表明,高速剪切流剪切形成的微气泡直径在15～50um之间,膜管孔径大小及表面性能,剪切流流速,液体表面张力,粘度是影响气泡粒径分布的主要因素.     

A numerical study of mass transfer of ozone dissolution in bubble plumes with an Euler-Lagrange method

In this paper we study the mass transfer process of ozone dissolution in a bubble plume inside a rectangular water tank, as a model problem for a water purification system. The effect of bubble diameter and plume structure on mass transfer efficiency of ozone in bubble plumes is investigated numerically. In order to capture the detailed plume structure, the interaction between liquid and bubbles is treated by a two-way coupling Euler-Lagrange method. The motion of the continuous phase (a mixture of liquid and gas bubbles) is solved using a finite difference method in an Eulerian framework. The motion of the dispersed phase (bubbles) is tracked individually in a Lagrangian approach. The ozone transfer process from bubbles to liquid is computed by modelling the mass transfer rate of individual bubbles. Our numerical results show a nonlinear dependence of the ozone dissolution efficiency on the initial bubble size. The dissolution efficiency varies rapidly when the initial bubble size reaches certain value while the change of efficiency is much slower at other bubble sizes. Therefore, for a given tank size it is not necessary to generate bubbles much smaller than the optimal size. This result is of importance for engineering since it is difficult to generate small bubbles in practice. Our results also show that the instantaneous dissolution rate of ozone could be increased by increasing the initial volumetric fraction of ozone inside bubbles even up to 20% while maintaining the dissolution efficiency.     

团聚液雾化气泡粒径分布特性的可视化研究

泡沫团聚法是有效脱除细颗粒物PM_2.5的方法。本文对团聚液的雾化粒径进行了研究,筛选出适于团聚PM_2.5的气泡粒径的溶液及喷雾条件。文中首先对气泡粒径与团聚颗粒物的能力进行估算,进而通过CCD拍摄精细雾化喷嘴喷出的团聚液泡沫的流动过程,利用MATLAB处理图片,得出雾化气泡粒径和密度大小。实验结果表明,发泡剂会使团聚液的雾化液滴形成气泡,增大雾化颗粒直径;PAM团聚液形成的气泡粒径偏小,且雾化颗粒密度大,粒径主要分布在小于200μm范围;XTG团聚液气泡粒径偏大,CMC团聚液气泡粒径介于两者之间;0.2% CMC团聚液气泡粒径均匀,颗粒数量大;在距喷口轴向20cm处,气泡破碎和聚合趋于稳定;喷口直径0.5mm时,气泡雾化粒径大多分布在100~300μm粒径范围内,符合团聚脱除PM_2.5的气泡条件;随着温度的升高,直径在0~300μm内的气泡颗粒数量增大明显。     

Interaction between partitioning porous plate and rising bubbles in a trayed bubble column

In a trayed bubble column, the structure of the partitioning plate plays an important role on the bubble behavior. This study examined the effect of the opening ratio and pore size of the plate on the bubble break-up frequency and bubble size distribution. The sieve tray was used as the partitioning plate. The opening ratio was closely related to gas cap development. The stagnation of bubble flow and a gas cap were observed with an opening ratio less than 48.5%. The gas cap increased with decreasing opening ratio and increasing superficial gas velocity. The main effect of the sieve tray could be categorized into the additional drag force and bubble break-up depending on the sieve pore size. When the sieve pore size was smaller than the Sauter diameter of the bubble swarm, the movement of rising bubbles was interrupted by the drag force applied by the surrounding mesh lines. On the other hand, when the sieve pore size was larger than the Sauter diameter, the bubbles were affected by the additional bubble break-up. After the bubbles penetrated the sieve tray, the bubble size distribution shifted to a smaller one and the Sauter diameter decreased.     

单孔及微孔曝气低气速鼓泡床内气泡行为比较

引言鼓泡床反应器被广泛应用于吸收、液相氧化、好氧生化等气液反应过程,气体在液相中的分散情况对鼓泡床的反应和传质特性都有很大影响.为了提高气液传质效率,增加生产强度,工业反应器很多都是在高气速下操作(Ug>0·05m·s-1),很多研究都集中在高气速湍动鼓泡区[1~3].但对有机     

FORMATION AND FLOW OF GAS BUBBLES IN A PRESSURIZED BUBBLE COLUMN WITH A SINGLE ORIFICE OR NOZZLE GAS DISTRIBUTOR

The characteristics of gas bubbles in a 5 cm diameter bubble column equipped with a single orifice of 1,3 or 5 mm diameter were investigated under system pressure of 0.1-15 MPa. The formation of gas bubbles was strongly affected by the system pressure. Under high pressures a dispersed gas jet was formed at gas velocities where spherical gas bubbles would have been formed at atmospheric pressure. The critical gas velocity between the bubbling regime and the jetting regime was correlated with the liquid phase Weber number and the gas phase Reynolds number based on the gas velocity at the orifice. Bubble size and gas holdup in the main part of the bubble column were also affected by the bubble formation pattern at the distributor     

Hydrodynamic study in a slurry-bubble-column reactor

Local gas holdup, bubble diameter and bubble rise velocity in the nitrogen/Drakeol-10 oil system were measured at both laboratory (ambient temperature and pressure) and industrially relevant (high temperature and pressure) conditions using a dual conductivity probe in a slurry-bubble-column reactor. It was found that a constant superficial velocity, the Sauter mean bubble diameter decreases with increasing pressure and temperature. The bubble rise velocity significantly decreases as the pressure increases. Large bubbles rise faster than smaller bubbles. Akita and Yoshida's correlation [1] was utilized to compute the bubble size. Predicted values agree with the experimental data at high temperature.     

EFFECT OF DISTRIBUTOR ON BUBBLE SIZE IN A CYLINDRICAL FLUIDIZED BED AT AN ELEVATED TEMPERATURE†

The effects of temperature and distributor on bubble diameter were investigated using a cylindrical fluidized bed of 147 mm in diameter. Three perforated distributors having different holes in diameter and the same ratio of holes to bed area were used. Eruption diameters of bubbles were measured using a high speed video-camera system under the following conditions: bed temperature = 300 and 600 K, bed particles = spherical glass beads of 272 μm in average size, excess gas velocity = 1-4 cm/s, and static bed height equals; 10-42 cm. The bubble diameter at 600 K was larger than that at 300 K. The difference became smaller with increasing the static bed height and with increasing the excess gas velocity. The distributor with larger holes gave larger bubbles. The effect of hole diameter of the distributor on the bubble diameter became insignificant with increasing the static bed height and with increasing the excess gas velocity.     

Bubbling process in stirred tank reactors I: Agitator effect on bubble size, formation and rising

The study of the hydrodynamics generated by impellers and its effect on the generation of bubbles and on their rising and dispersion is of key importance to improve the knowledge about the contact between phases and the mass transfer rates, particularly in cases where it is the limiting step. CFD simulations and high-speed video techniques are used to study the hydrodynamics developed by five different impellers, each located at three different positions above the dispersion device. Furthermore, two dispersion devices with one and two holes, respectively, are also used. The effect of the impellers on the characteristics of the bubbles and of the dispersions generated has been analysed. Bubbles generated under stirring are smaller than those generated in stagnant fluids. It is also shown that the initial bubble size at the orifice determines the contribution of the impeller and the perforated plate to the Sauter mean diameter. Although bubble formation is chaotic, the formation period is predictable based on three variables: the location of the impeller, its rotational speed and the gas flow rate. Bubble mean diameter was correlated to classical equations based on Kolmogorov's theory. Only when impellers are capable of breaking the bubbles, Kolmogorov's theory is completely verified.