用电导探针测定气-液多层桨搅拌槽内气泡尺寸分布

在直径0.48 m的椭圆底三层组合桨搅拌槽中,使用双电导探针测定常温24℃及热态81℃通气条件下,空气-去离子水体系的局部气泡尺寸分布,分别利用标定法及数学重构法进行数据处理,得出适宜方法为数值解析的重构法.采用以半椭圆管盘式涡轮(HEDT)为底桨,上两层分别为四叶轴流桨下压(WHD)及上提(WHu)操作的HEDT+2...     

搅拌槽内局部气含率及其分布规律的研究

搅拌槽内局部气含率及其分布规律的研究高正明，王英琛，施力田，傅举孚（北京化工大学化学工程系，北京１０００２９）关键词：局部气含率，气－液搅拌槽，搅拌１前言气－液搅拌槽反应器在石油化工、生物化工等领域内都得到了极为广泛的应用。但由于受到测试手段的限制，...     

搅拌槽内气——液体系的分散,传质和传热

综述了搅拌槽内气－液体系分散、传质和传热特性，比较了搅拌器类型、通气方式和多级搅拌器对混合性能的影响。对文献中观点的分歧进行了探讨，由此得到两个传质系数关联式，并揭示出给热系数随操作条件变化的机理。     

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.     

槽内溶液的空气搅拌

本文研究了槽内溶液的空气搅拌、搅拌装置的设计方法。根据由实验得出的搅拌强度分布型式,分析了搅拌强度与风量、吹出孔孔径等因素的关系,认为设计时应按照电镀零件在槽内的排列,设置空气吹出孔;孔数一般为12～22只/米,孔径3～6mm;再按每只孔8～14L/min的风量计算总风量,并按空气吹管在溶液内的深度计算所需的空气动力。此种计算法与按溶液体积及按溶液的液面积计算风量的方法相比,更符合实际需要;计算所得的风量能保证搅拌效果,而且不会造成动力浪费和其他不良影响。     

挡板进气多级搅拌槽内的气—液分散特性

研究了挡板进气多级搅拌槽内的气－液分散流型、临界分散转速、搅拌功率、气含率和气泡停留时间。试验证明，这种结构的搅拌槽，比标准通气式搅拌槽具有更优良的气－液分散特性，并回归得到了搅拌功率、气含率和气泡停留时间的关联式。     

搅拌槽内温度场分布的实验研究

在对称装有四组垂直加热列管、直径为500mm的搅拌槽中使用CBY桨进行搅拌,以甘油为工作物料,让液晶粒子均匀分散在某中,然后采用LC测温技术测量搅拌槽内温度场的分布。分别研究了搅拌槽中轴向、径向的温度分布随时间的变化以及同一轴截面的温度分布随搅拌转速不同而变化的情况。     

3D Single Bubble Breakup Tracking in a Stirred Tank

A detailed understanding of turbulent fluid particle breakup mechanisms is essential for the accurate modeling of gas/liquid and liquid/liquid dispersions. The design of a fully automated setup for the three‐dimensional serial examination of the single bubble breakup process in a stirred tank, ensuring high repetition rates necessary for the additionally automated statistical analysis, is described. The implementation of a three‐dimensional automatic bubble breakup tracking tool is illustrated. At last, exemplary bubble breakup trajectories that show the benefits and limitations of the developed system and method are discussed.     

Gas-liquid flow and bubble size distribution in stirred tanks

This work is aimed at investigating the turbulent two-phase flow and the bubble size distribution (BSD) in aerated stirred tanks by experiments and computational fluid dynamics (CFD) modelling. The experimental data were collected using a two-phase particle image velocimetry technique and a digital image processing method based on a threshold criterion. With the former technique, the liquid and the gas phase ensemble-averaged mean and r.m.s. velocities are measured simultaneously, while with the latter the dimensions of the bubbles dispersed inside the liquid are evaluated. On the modelling side, a CFD approach, based on the solution of Reynolds average Navier-Stokes equations in an Eulerian framework for both phases, is adopted. As for the bubble dimensions modelling, besides the mono-dispersed assumption, a population balance method, named MUSIG, with bubble break-up and coalescence models is considered. The BSD and the axial and radial velocity of the gas and the liquid phase are presented and discussed. The outcomes of the computational work are evaluated on the basis of the experimental results.     

Revisiting Basics of kLa Dependency on Aeration in Bubble Columns: a Is Surprisingly Stable

A comprehensive experimental characterization of a small-scale bubble column bioreactor (60 mL) is presented. Bubble size distribution (BSD), gas holdup, and k_La were determined for different types of liquids, relevant fermentation conditions and superficial gas velocities u_G. The specific interfacial area a and liquid mass transfer coefficient k_L have been identified independent of each other to unravel their individual impact on k_La. Results show that increasing u_G leads to larger bubbles and higher gas holdup. As both parameters influence a in opposite ways, no increase of a with u_G is found. Furthermore, k_L increases with increasing bubble size outlining that improved oxygen transfer is not the result of higher a but of risen k_L instead. The results build the foundation for further simulative investigations.     

Experimental Determination and Modeling of Bubble Size Distributions in Bubble Columns

Using a five point conductivity technique local values of bubble size,bubble velocity and gas fractionhave been experimentally determined in a 288 mmID and 4.3 m high bubble column as a function of axial andradial position for the air/water and CO_2/N_2/aqueous MDEA systems.The experimental results are comparedwith predictions from a fundamental two-fluid model.The implementation of a non-steady lateral drag term inthe two-fluid model has been shown.In addition to improving the physical realism of the model,it is found togive slight improvements in the predictions of the distributions of local bubble size.Predictions of bubble size arefound in reasonable agreement with experimental values in the heterogeous flow regime,whereas they are stil1found to be unreliable at low gas velocities.Local void predictions are found in reasonable agreement with experi-mental values,but deviations occur in the homogeneous flow regime towards the wall.This is attributed to defi-ciencies in the simplified bubble size mode     

Bubble Size Distribution in Oil‐Based Bubble Columns

A practical population balance model was used to evaluate the bubble size distribution in a bubble column. In addition, the bubble size distribution in the bubble column was measured at different gas velocities by photography and analysis of the pictures. Four types of liquid, i.e., water and three petroleum‐based liquids, were used in the experiments. The gas phase was air. It was found that the existing models in the literature are not able to satisfactorily predict the experimentally measured bubble size distribution. The model can be corrected by applying a correction factor to the energy dissipation rate. The corrected model fits the experimental bubble size distribution considerably better than the existing models. The variation of this correction factor is reported for different systems at different gas velocities.     

外换热器为复杂流向的搅拌容器中液体不稳定传热计算

本文论述了带复杂流向外换热器的搅拌容器中液体不稳定传热计算方法,对几种常见的这类情况进行了算式推导,并举例说明。     

Bubble characteristics in shallow bubble column reactors

The bubble characteristics have been investigated in an air–water bubble column with shallow bed heights. The effect of bed height, location and the presence of solids on the bubble size, bubble rise velocity and overall and sectional gas holdup are studied over a range of superficial gas velocities. Optimal shallow bed operation relies on the combined entrance and exit effects at the distributor and the liquid bed surface. The gas holdup is found to decrease with an increase in H/D ratio but the effect is diminishing at high H/D ratios. A H/D ratio of 2–4 is found to be suitable for shallow bed operation. The presence of solids causes the formation of larger bubbles at the distributor and the effect is diminishing as the gas velocity is increased.