Bubble Size (bubble + size)

Distribution by Scientific Domains
Chemistry72%

Terms modified by Bubble Size

  • bubble size distribution
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    Selected Abstracts

    Air Inclusion Into a Model Cake Batter Using a Pressure Whisk: Development of Gas Hold-up and Bubble Size Distribution

    JOURNAL OF FOOD SCIENCE, Issue 8 2001
    A.H. Massey
    ABSTRACT: This paper investigates the development of gas hold-up (that is, gas volume fraction) and bubble size distribution in a model cake batter, which is aerated in a pressure whisk. With increasing aeration time, the hold-up was found to pass through a maximum before approaching a uniform steady state value. A mathematical model that describes this profile has been developed. Bubble size distribution was found to be adequately described by a log normal distribution function with mean size varying between 20 and 50 ,m. Higher pressures were found to increase hold-up and mean bubble size, whereas higher whisk speeds reduced the time required to achieve a given hold-up and the final mean bubble size. [source]

    The influence of the particle size distribution on fluidized bed hydrodynamics using high-throughput experimentation

    AICHE JOURNAL, Issue 8 2009
    Renske Beetstra
    Abstract The goal of the described project is to design mixtures of particles with optimal fluidization properties. Using high-throughput experimentation, a novel approach to study hydrodynamics in fluidized beds, the relevant properties can be obtained in a limited period of time. This approach is demonstrated by assessing the influence of particle size distribution on fluidized bed hydrodynamics of Geldart A powders. By manipulating the width of the particle size distribution of alumina powder, the bubble diameter is reduced up to 40%. The addition of fines to a given particle size distribution also decreases the bubble diameter up to 40%, whereas the addition of coarse particles hardly influences the bubble size. At low gas velocities, the bubble size was found to increase with fines addition or increasing standard deviation. © 2009 American Institute of Chemical Engineers AIChE J, 2009 [source]

    Passage of a bubble through a liquid,liquid interface

    AICHE JOURNAL, Issue 3 2008
    N. Dietrich
    Abstract The aim of this study is to investigate the bubble passage at a liquid,liquid interface using a high-speed video camera (950 images per second) and a Particle Image Velocimetry (PIV) system. Experiments were conducted in a square Plexiglas column of 0.1 m. Bubbles were generated through a submerged orifice (D = 1 × 10,3 m). The Newtonian Emkarox (HV45) solution was employed for the heavy phase whereas two different organic liquids of different viscosity (Silicone oil 10 mPa s and 100 mPa s) were used as light phase. Experimental results show the effect of the bubble size and the viscosity of the light phase on the retention time, the length of the column of fluid entrained behind the bubble, the bubble velocity as well as the velocity fields at the liquid,liquid interface. © 2008 American Institute of Chemical Engineers AIChE J, 2008 [source]

    A CFD,PBM coupled model for gas,liquid flows

    AICHE JOURNAL, Issue 1 2006
    Tiefeng Wang
    Abstract A computational fluid dynamics,population balance model (CFD-PBM) coupled model was developed that combines the advantages of CFD to calculate the entire flow field and of the PBM to calculate the local bubble size distribution. Bubble coalescence and breakup were taken into account to determine the evolution of the bubble size. Different bubble breakup and coalescence models were compared. An algorithm was proposed for computing the parameters based on the bubble size distribution, including the drag force, transverse lift force, wall lubrication force, turbulent dispersion force, and bubble-induced turbulence. With the bubble breakup and coalescence models and the interphase force formulations in this work, the CFD-PBM coupled model can give a unified description for both the homogeneous and the heterogeneous regimes. Good agreement was obtained with the experimental results for the gas holdup, liquid velocity, and bubble size distribution. © 2005 American Institute of Chemical Engineers AIChE J, 2006 [source]

    Surface roughness effects on thermo-hydrodynamic lubrication of journal bearings lubricated with bubbly oil

    LUBRICATION SCIENCE, Issue 1 2006
    A. M. A. El-Butch
    In this paper, the combined effect of surface roughness and bubbles content on the hydrodynamic performance of journal bearings is studied. In the analysis, it is assumed that the bearing and shaft surfaces are covered with homogeneous isotropic roughness, the air bubbles are evenly distributed through the lubricant and the bubble size is very small. The modified Reynolds equation governing the pressure generation in the bearing gap for compressible fluid is solved simultaneously with the energy equation. Temperature and pressure distributions, coefficient of friction, bearing load capacity and attitude angle as affected by surface roughness, bubble content and some bearing parameters are presented. Results showed that the bearing load carrying capacity is higher at higher values of average roughness and higher bubble content as a direct consequence of the higher pressure values attained, and the average roughness and the bubbles content had no significant effect on the attitude angle. Copyright © 2006 John Wiley & Sons, Ltd. [source]

    Impact of tangled magnetic fields on fossil radio bubbles

    MONTHLY NOTICES OF THE ROYAL ASTRONOMICAL SOCIETY, Issue 2 2007
    M. Ruszkowski
    ABSTRACT There is growing consensus that feedback from active galactic nuclei (AGN) is the main mechanism responsible for stopping cooling flows in clusters of galaxies. AGN are known to inflate buoyant bubbles that supply mechanical power to the intracluster gas [intracluster medium (ICM)]. High Reynolds number hydrodynamical simulations show that such bubbles get entirely disrupted within 100 Myr, as they rise in cluster atmospheres, which is contrary to observations. This artificial mixing has consequences for models trying to quantify the amount of heating and star formation in cool core clusters of galaxies. It has been suggested that magnetic fields can stabilize bubbles against disruption. We perform magnetohydrodynamical simulations of fossil bubbles in the presence of tangled magnetic fields using the high-order pencil code. We focus on the physically motivated case where thermal pressure dominates over magnetic pressure and consider randomly oriented fields with and without maximum helicity and a case where large-scale external fields drape the bubble. We find that helicity has some stabilizing effect. However, unless the coherence length of magnetic fields exceeds the bubble size, the bubbles are quickly shredded. As observations of Hydra A suggest that length-scale of magnetic fields may be smaller than typical bubble size, this may suggest that other mechanisms, such as viscosity, may be responsible for stabilizing the bubbles. However, since Faraday rotation observations of radio lobes do not constrain large-scale ICM fields well if they are aligned with the bubble surface, the draping case may be a viable alternative solution to the problem. A generic feature found in our simulations is the formation of magnetic wakes where fields are ordered and amplified. We suggest that this effect could prevent evaporation by thermal conduction of cold H, filaments observed in the Perseus cluster. [source]

    Bubble shape, gas flow and gas,liquid mass transfer in pulp fibre suspensions

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 3 2010
    L. K. Ishkintana
    Abstract Gas,liquid mass transfer in pulp fibre suspensions in a batch-operated bubble column is explained by observations of bubble size and shape made in a 2D column. Two pulp fibre suspensions (hardwood and softwood kraft) were studied over a range of suspension mass concentrations and gas flow rates. For a given gas flow rate, bubble size was found to increase as suspension concentration increased, moving from smaller spherical/elliptical bubbles to larger spherical-capped/dimpled-elliptical bubbles. At relatively low mass concentrations (Cm,=,2,3% for the softwood and Cm,,,7% for the hardwood pulp) distinct bubbles were no longer observed in the suspension. Instead, a network of channels formed through which gas flowed. In the bubble column, the volumetric gas,liquid mass transfer rate, kLa, decreased with increasing suspension concentration. From the 2D studies, this occurred as bubble size and rise velocity increased, which would decrease overall bubble surface area and gas holdup in the column. A minimum in kLa occurred between Cm,=,2% and 4% which depended on pulp type and was reached near the mass concentration where the flow channels first formed. le transfert de masse gaz-liquide dans des suspensions de fibres de pulpe, dans une colonne à bulles de traitement en lot, est expliqué par des observations faites dans une colonne 2D de la taille et de la forme des bulles. Deux suspensions de fibres de pulpe (pulpes kraft de bois dur et de bois tendre) ont été étudiées sur un intervalle de concentrations en masse des suspensions et sur un intervalle de débits de gaz. Pour un débit de gaz donné, on a observé que la taille des bulles augmentait avec l'augmentation de la concentration de la suspension, passant de petites bulles sphériques/elliptiques à des bulles plus grosses de forme quasi-sphérique avec capuchon à elliptique avec dépression. À des concentrations en masse relativement basses (Cm,=,2,3% pour le bois tendre et Cm,=,,7% pour la pulpe de bois dur), des bulles distinctes n'étaient plus observées dans la suspension. Au lieu de cela, un réseau de canaux se formait, au travers duquel le gaz s'écoulait. Dans la colonne à bulles, le taux de transfert de masse volumétrique gaz-liquide, kLa, diminuait avec l'augmentation de la concentration de la suspension. À partir des études 2D, cela se produisait lorsque la taille des bulles et la vélocité ascendante augmentaient, ce qui devrait faire diminuer la surface d'ensemble des bulles et la retenue de gaz dans la colonne. Un minimum de kLa a été observé avec Cm,=,2% et 4% (selon le type de pulpe) et était atteint à proximité de la concentration en masse pour laquelle les canaux d'écoulement commençaient à se former. [source]

    Local Bubble Dynamics and Macroscopic Flow Structure in Bubble Columns with Different Scales

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 6 2003
    Wei Chen
    Abstract Local bubble behaviours were investigated in three bubble columns with different diameters of 200, 400 and 800 mm. By means of a novel single-tip optical fibre probe employing laser Doppler technique, the local gas holdup, bubble frequency, bubble size and velocity were measured simultaneously at different locations of the columns. Measurements were performed in air-water system at superficial gas velocities up to 90 mm/s. The averaged profiles and instantaneous measurements were analyzed and compared for different columns. The presence of a coherent gross circulation structure spanning the entire column diameter in the larger column rather than a pair of symmetrical circulation cells observed in the smaller columns has been confirmed. Les comportements locaux des bulles ont été étudiés dans trois colonnes à bulles de diamètres différents, soient 200, 400 et 800 mm. Au moyen d'une nouvelle sonde à fibre optique à embout unique employant la technique laser Doppler, des mesures locales de la rétention de gaz, de la fréquence des bulles, de la taille des bulles et de la vitesse ont été effectuées simultanément à différents endroits dans les colonnes. Ces mesures ont été effectuées pour un système air-eau à des vitesses de gaz superficielles atteignant 90 mm/s. Les profils moyennés et les mesures instantanées ont été analysés puis comparés pour différentes colonnes. La présence d'une structure de circulation unique cohérente occupant tout le diamètre de la colonne dans la colonne la plus large plutôt qu'une paire de cellules de circulation symétriques observées dans les colonnes plus petites est confirmée. [source]

    The Effect of Bed Temperature on Mass Transfer between the Bubble and Emulsion Phases in a Fluidized Bed

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 5 2003
    Wenyuan Wu
    Abstract The rate of interphase mass transfer between the bubble and emulsion phases of a bubbling fluidized bed is of primary importance in all models for fluidized bed reactors. Many experimental studies have been reported, however, all these investigations have been carried out in fluidized beds operated at room temperature. In this work, the effect of the bed temperature on the interphase mass transfer is reported. Single bubbles containing argon , used as a tracer , were injected into an incipiently fluidized bed maintained at the required temperature. The change in argon concentration in the bubble was measured using a suction probe connected to a mass spectrometer. The effects of bed particle type and size, bubble size, and bed temperature on the mass transfer coefficient were examined experimentally. The interphase mass transfer coefficient was found to decrease with the increase in bed temperature and bubble size, and increase slightly with increase in particle size. Experimental data obtained in this study were compared with some frequently used correlations for estimation of the mass transfer coefficient. Le taux de transfert de matière interphasique entre les phases à bulles et à émulsion d'un lit fluidisé bullant est de première importance dans tous les modèles de réacteurs à lits fluidisés. Beaucoup d'études expérimentales ont été présentées; toutefois, toutes ces recherches ont été menées dans des lits fluidisés fonctionnant à la température ambiante. Dans ce travail, on décrit l'effet de la température du lit sur le taux de transfert de matière. Des bulles simples contenant de l'argon – utilisé comme traceur – ont été injectées dans un lit fluidisé naissant maintenu à la température requise. Le changement de concentration d'argon dans la bulle est mesuré à l'aide d'une sonde de succion reliée à un spectromètre de masse. Les effets du type et de la taille des particules de lit, de la taille des bulles et de la température de lit sur le coefficient de transfert de matière sont examinés de façon expérimentale. On a trouvé que le coefficient de transfert de matière interphasique diminuait avec l'augmentation de la température du lit et de la taille des bulles, et augmentait légèrement avec l'augmentation de la taille des particules. Les données expérimentales obtenues dans cette étude sont comparées avec quelques corrélations fréquemment utilisées pour l'estimation du coefficient de transfert de matière. [source]

    Important Factors in Bubble Coalescence Modeling in Stirred Tank Reactors

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 3-4 2003
    Rahman Sudiyo
    Abstract Bubble coalescence has been studied in a 2.6 L stirred tank. Instantaneous velocity fields were measured using PIV and corresponding turbulent kinetic energy, dissipation rate, various length and timescales were estimated. All of these data, combined with data of local gas hold-up, bubble size and coalescence rate obtained with shadowgraph were used to assess bubble coalescence at different positions. Results show that bubble coalescence takes place mostly near the tank wall, especially on the leeward side of baffles. The most important factors affecting coalescence are gas hold-up, fluctuation of liquid velocity, different rise velocities of bubbles, and trapping of bubbles in stationary and turbulent eddies. On a étudié la coalescence des bulles dans un réservoir agité de 2,6 L. Les champs de vitesse instantanée ont été mesurés par vélocimétrie à imagerie de particules (PIV), et l'énergie cinétique turbulente correspondante, la vitesse de dissipation et diverses échelles de longueur et de temps ont été estimés. Toutes ces données, combinées à des données de rétention de gaz locale, de taille des bulles et de vitesse de coalescence obtenues avec le projecteur de profils, ont permis d'évaluer la coalescence des bulles à différentes positions. Les résultats montrent que la coalescence des bulles se produit principalement près de la paroi du réservoir, spécialement sur la face aval des chicanes. Les principaux facteurs qui influent la coalescence sont la rétention de gaz, la fluctuation de la vitesse de liquide, les différentes vitesses d'ascension des bulles et le piégeage des bulles dans des tourbillons stationnaires et turbulents. [source]

    Combined PIV/PTV-Measurements for the Analysis of Bubble Interactions and Coalescence in a Turbulent Flow

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 3-4 2003
    Dirk Bröder
    Abstract In order to allow more reliable modeling of coalescence processes in turbulent bubbly flows, detailed experiments in a double loop reactor were performed. Narrow and essentially monomodal bubble size distributions in the range of 2 to 4 mm were created. For simultaneous measurements of bubble size, bubble velocity and liquid velocity a combined system of PIV and PTV was developed and applied. It was possible to determine bubble size distributions and mean, as well as fluctuating velocities for both phases. The spatial changes of the bubble size distribution, due to the influence of bubble coalescence, was analyzed and coalescence rates were calculated. Afin d'améliorer la fiabilité de la modélisation des procédés de coalescence dans les écoulements bouillonnants turbulents, des expériences poussées ont été menées dans un réacteur à double boucle. Des distributions de taille des bulles étroites, essentiellement monodisperses, dans la gamme de 2 à 4 mm, ont été créées. Pour les mesures simultanées de la taille des bulles, de la vitesse des bulles et de la vitesse du liquide, on a mis au point et appliqué un système combiné de PIV et PTV. Il a été possible de déterminer les distributions de taille des bulles et la moyenne mais également les vitesses fluctuantes pour les deux phases. Les changements spatiaux de la distribution de la taille des bulles dus à l'influence de la coalescence des bulles ont été analysés et les vitesses de coalescence ont été calculées. [source]

    Effect of Gas Density on the Hydrodynamics of Bubble Columns and Three-Phase Fluidized Beds

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 3-4 2003
    Arturo Macchi
    Abstract Experiments were performed at ambient temperature and pressure in a 127 mm inner diameter column with a 55% wt. aqueous glycerol solution, 6-mm spherical borosilicate beads and four gases , helium, air, carbon dioxide and sulphur hexafluoride , giving a 35-fold gas density range. The dispersed bubble flow regime was sustained to higher gas velocities and gas holdups for denser gases. This finding appears to be due to the reduction of the maximum stable bubble size (i.e. enhanced bubble break-up), rather than to formation of smaller bubbles at the distributor with increasing gas density. The effect of gas density was significant both with and without the particles present, with gas holdup increasing, bed voidage increasing and liquid holdup decreasing with increasing gas density. The holdup correlations of Han et al. (1990) have been modified to incorporate the effect of gas density. On a mené des expériences à la température et à la pression ambiante dans une colonne de 127 mm de diamètre intérieur avec une solution de glycérol aqueux de 55 % en poids, des billes de verre de borosilicate sphériques de 6 mm et quatre gaz , hélium, air, gaz carbonique et hexafluorure de soufre , donnant une gamme de densité gazeuse multipliée par 35. Le régime d'écoulement bouillonnant dispersé est maintenu jusqu'à des vitesses et des rétentions de gaz supérieures pour les gaz plus denses. Ce résultat semble être dû à la réduction de la taille de bulle stable maximum (c.-à-d. une rupture de bulles améliorée), plutôt qu'à la formation de bulles plus petites au distributeur avec l'augmentation de la densité gazeuse. L'effet de la densité gazeuse est significatif avec ou sans la présence des particules, avec l'augmentation de la rétention de gaz, l'augmentation du vide du lit et la diminution de la rétention de liquide avec l'augmentation de la densité gazeuse. Les corrélations de rétention de Han et al. (1990) sont modifiées de sorte à introduire l'effet de la densité gazeuse. [source]

    Bubble coalescence and its effect on dynamic foam stability

    THE CANADIAN JOURNAL OF CHEMICAL ENGINEERING, Issue 2 2002
    Yoon Seong Cho
    Abstract The size of bubbles generated using a single-hole sparger, a multi-hole sparger and a flotation cell were measured. While the size of bubbles generated from the single-hole sparger does not depend on frother concentration, the bubble size strongly depends on frother concentration when the multi-hole sparges, or flotation cell, are utilized. The bubbles size ceases to depend on frother at the concentrations exceeding the value characteristic for each frother and referred to as the critical coalescence (CCC). All the bubble size vs. frother concentration curves converge on a single curve. Aqueous solutions of the frothers that are characterized by low CCC values from foams quite stable under dynamic conditions. Since bubble coalescence can be inhibited by frother concentrations exceeding the CCC, sparing systems can be studied and compared only at frother concentrations that exceed CCC. On a mesuré la taille des bulles produites par un aérateur à orifice unique, un aérateur à orifices multiples et une cellule de flottation. Alors que la taille des bulles produites avec l'aérateur à orifice unique n'est pas liée à la concentration d'agent moussant, la taille des bulles dépend fortement de la concentration d'agent moussant dans le cas des aérateurs à orifices multiples ou de la cellule de flottation. La taille des bulles cesse d'êde la valeur caractéristique de chaque agent moussant (concentration de coalescence critique ou CCC). Toutes les courbes de taille des bulles par rapport à la concentration d'agent moussant se superposent. Les solutions aqueuses des agents moussants qui sont caractérisés par de faibles valeurs de CCC forment des mousses plutôt stables dans des conditions dynamiques. Considérant que la coalescence es bulles peut être inhibée par des concentrations d'agent moussant excédant la CCC, les systèmes de dispersion peuvent être étudiés et comparés seulemetn à des concentrations d'agent moussant qui excèdent la CCC. [source]

    Sensitivity Study on Modeling an Internal Airlift Loop Reactor Using a Steady 2D Two-Fluid Model

    CHEMICAL ENGINEERING & TECHNOLOGY (CET), Issue 12 2008
    Q. Huang
    Abstract The sensitivity study of bubbly flow in an internal airlift loop reactor is presented using a steady Reynolds averaging two-fluid model. Comparative evaluation of different drag formulations, drag coefficient correlations, turbulence effect on the drag coefficient, outlet slip velocity, and bubble size is performed and the respective influence to the simulation results is highlighted. It is found that a complicated drag formulation may not result in reliable predictions. All the drag coefficient correlations underpredict the gas holdup if the influence of turbulence on the drag coefficient is not well incorporated. Fortunately, the global hydrodynamics is not sensitive to the outflow slip velocity for a wide range, so a steady two-fluid model can be used to simulate the bubbly flow when the flow field is fully developed. The correct estimation of bubble size with properly selected correlations play an important role in successful simulation of gas-liquid bubbly flow in airlift loop reactors. [source]

    Comparison of decoupling methods for analyzing pressure fluctuations in gas-fluidized beds

    AICHE JOURNAL, Issue 4 2010
    Yongmin Zhang
    Abstract Two methods of decoupling pressure fluctuations in fluidized beds by using the incoherent part (IOP) of absolute pressure (AP) and differential pressure (DP) fluctuations are evaluated in this study. Analysis is conducted first to demonstrate their similarities, differences, and drawbacks. Then, amplitudes, power spectral densities, mean frequencies, coherence functions, and filtering indices of the IOP of AP and DP fluctuations are calculated and compared based on experimental data from a two-dimensional fluidized column of FCC particles. Derived bubble sizes are also compared with the sizes of bubbles viewed in the two-dimensional bed. The results demonstrate the similarity of these two methods in filtering out global compression wave components from absolute pressure fluctuations, especially those generated from oscillations of fluidized particles and gas flow rate fluctuations. However, both methods are imperfect. Neither can filter out all the compression wave components and retain all the useful bubble-related wave components. Their amplitudes can be used to characterize global bubble property and quality of gas,solids contacting in bed, but they do not give accurate measurement of bubble sizes. © 2009 American Institute of Chemical Engineers AIChE J, 2010 [source]

    Applications of Defocusing DPIV to Bubbly Flow Measurement

    PARTICLE & PARTICLE SYSTEMS CHARACTERIZATION, Issue 3 2003
    David Jeon
    Abstract Defocusing digital particle image velocimetry (DDPIV) was used to investigate a bubbly flow in the wake of a hydrofoil. DDPIV is a three component volumetric velocimetry technique that operates at full video rate. Complex, three-dimensional, and time-dependent flows can be measured. To measure the bubble sizes, an extension to DDPIV was made to infer bubble sizes from their intensities. Both bubble size distributions and bubble velocity fields were simultaneously measured. Results indicate that DDPIV can reliably measure bubble sizes in the range of 100,microns, as well as resolving their aggregate motion. [source]

    Phases Dispersion and Oxygen Transfer in a Simulated Fermentation Broth Containing Castor Oil and Proteins

    BIOTECHNOLOGY PROGRESS, Issue 5 2004
    Nancy Pulido-Mayoral
    The sizes of air bubbles and castor oil drops were studied by image analysis as a function of the concentration of soluble protein (bovine serum albumin [BSA] and lipase, as model proteins) in a three-phase system using a simulated fermentation medium (aqueous salt solution, castor oil, and air). Small amounts of proteins (<0.02 g/L) caused an important decrease in oil drops and bubbles sizes, together with a pronounced decrease in surface tension. The extent and profiles of this decrease seem to be determined by the conformation of the protein at the interface. The kLa value increased considerably for increasing concentration (up to 0.02 g/L) of the two proteins but was very different (2-fold higher for the lipase) at the highest concentrations tested (0.5 g/L), a phenomenon that can be caused by the extent to which bubbles are trapped within oil drops. [source]