Bibliografie tematiche / Bubble column

Letteratura scientifica selezionata sul tema "Bubble column"

Autore: Grafiati
Pubblicato: 4 giugno 2021
Ultima modifica: 19 aprile 2023

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Articoli di riviste sul tema "Bubble column"

1

Reeder, D. Benjamin, John E. Joseph, Thomas A. Rago, Jeremy M. Bullard, David Honegger e Merrick C. Haller. "Acoustic spectrometry of bubbles in an estuarine front: Sound speed dispersion, void fraction, and bubble density". Journal of the Acoustical Society of America 151, n. 4 (aprile 2022): 2429–43. http://dx.doi.org/10.1121/10.0009923.

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Abstract (sommario):
Estuaries constitute a unique waveguide for acoustic propagation. The spatiotemporally varying three-dimensional front between the seawater and the outflowing freshwater during both flood and ebb constitutes an interfacial sound speed gradient capable of supporting significant vertical and horizontal acoustic refraction. The collision of these two water masses often produces breaking waves, injecting air bubbles into the water column; the negative vertical velocities of the denser saltwater often subduct bubbles to the bottom of these shallow waveguides, filling the water column with a bubbly mixture possessing a significantly lower effective sound speed. A field experiment was carried out in the mouth of Mobile Bay, Alabama in June 2021 to characterize estuarine bubble clouds in terms of their depth-dependent plume structure, frequency-dependent sound speed and attenuation, bubble size distribution, bubble number density, and void fraction. Results demonstrate that sound speed in the bubbly liquid consistently falls below the intrinsic sound speed of bubble-free water; specifically, the bubbly liquid 1.3 m below the surface in a front in this environment possesses effective sound speeds, void fractions, and bubble number densities of approximately 750 m/s, 0.001%, and 2 × 106 bubbles/m3, respectively.
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2

MUDDE, ROBERT F., e TAKAYUKI SAITO. "Hydrodynamical similarities between bubble column and bubbly pipe flow". Journal of Fluid Mechanics 437 (22 giugno 2001): 203–28. http://dx.doi.org/10.1017/s0022112001004335.

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The hydrodynamical similarities between the bubbly flow in a bubble column and in a pipe with vertical upward liquid flow are investigated. The system concerns air/water bubbly flow in a vertical cylinder of 14.9 cm inner diameter. Measurements of the radial distribution of the liquid velocity, gas fraction and the bubble velocity and size are performed using laser Doppler anemometry for the liquid velocity and a four-point optical fibre probe for the gas fraction, bubble velocity and size. The averaged gas fraction was 5.2% for the bubble column (with a superficial liquid velocity of zero) and 5.5% for the bubbly pipe flow at a superficial liquid velocity of 0.175 m s−1. From a hydrodynamical point of view, the two modes of operation are very similar. It is found that in many respects the bubbly pipe flow is the superposition of the flow in the bubble column mode and single-phase flow at the same superficial liquid velocity.The radial gas fraction profiles are the same and the velocity profiles differ only by a constant offset: the superficial liquid velocity. This means that the well-known large-scale liquid circulation (in a time-averaged sense) of the bubble column is also present in the bubbly pipe flow. For the turbulence intensities it is found that the bubbly pipe flow is like the superposition of the bubble column and the single-phase flow at the superficial liquid velocity of the pipe flow, the former being at least an order of magnitude higher than the latter. The large vortical structures that have been found in the bubble columns are also present in the bubbly pipe flow case, partly explaining the much higher ‘turbulence’ levels observed.
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3

Ariny Demong, Andrew Ragai Rigit e Khairuddin Sanaullah. "Effect of Swirl Gas Injection on Bubble Characteristics in a Bubble Column". Journal of Advanced Research in Fluid Mechanics and Thermal Sciences 102, n. 2 (27 febbraio 2023): 155–65. http://dx.doi.org/10.37934/arfmts.102.2.155165.

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Abstract (sommario):
Swirling gas injection is a well-known technique to improve mass transfer in bubble columns. It can be used to create small bubbles with a high surface area-to-volume ratio, which is beneficial for mass transfer. Swirl gas injection can also be used to create a more uniform bubble size distribution and improve the mixing of gas and liquid in the column. This study aims to determine the impact of swirl gas injection on bubble properties, including bubble shape, size, and velocity. A bubble detection approach has been developed for quick and precise determination of bubble size distributions in gas-liquid systems. Advanced digital image processing, including edge detection and bubble edge recognition, is used in this method. The experiment is conducted in a bubble column at a height of 57 cm and 61 cm. The column had a ring sparger and was made of Plexiglas. Tap water was used as the liquid, while air from an air compressor was utilized as the gas phase. The shape, size, population, and velocity of the bubble are measured using a high-speed digital camera. According to this study, the average bubble size reduced as the impeller speed increased, while the population of bubbles increased when the sparger rotation speed increased from 30 to 150 rpm.
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4

Tian, Ye, Hua Qian e Qiu Hong Ke. "A Bubble Detection Algorithm Based on Wavelet Transform and Canny Operator for Deinked Pulp Flotation Column". Applied Mechanics and Materials 278-280 (gennaio 2013): 1162–66. http://dx.doi.org/10.4028/www.scientific.net/amm.278-280.1162.

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Deinked pulp flotation column has been applied in wastepaper recycling. Bubble size in deinked pulp flotation column is very important during the flotation process. In this paper, bubble images of deinked pulp flotation column are first caught by digital camera, and then the bubbles are detected by using a bubble detection algorithm based on wavelet transform and canny operators. The results show the algorithms are very practical and effective on bubble detection in deinked pulp flotation column.
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5

Bastani, Dariush, Ali Baghaei e Amir Sarrafi. "“Bubble Bunch” phenomenon in operation of a bubble column". Open Chemistry 7, n. 4 (1 dicembre 2009): 803–8. http://dx.doi.org/10.2478/s11532-009-0081-4.

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AbstractWhile studying the operation of a rectangular bubble column in laboratory scale, it was observed that under certain circumstances tiny bubbles attach to larger bubbles without causing them to coalesce. In other words, bubbles with large diameters (d > 5 mm) swept tiny bubbles (d
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6

Mosdorf, Romuald, Tomasz Wyszkowski e Kamil Dąbrowski. "Multifractal properties of large bubble paths in a single bubble column". Archives of Thermodynamics 32, n. 1 (1 aprile 2011): 3–20. http://dx.doi.org/10.2478/v10173-011-0001-9.

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Multifractal properties of large bubble paths in a single bubble columnIn the paper the paths of bubbles emitted from the brass nozzle with inner diameter equal to 1.6 mm have been analyzed. The mean frequency of bubble departure was in the range from 2 to 65.1 Hz. Bubble paths have been recorded using a high speed camera. The image analysis technique has been used to obtain the bubble paths for different mean frequencies of bubble departures. The multifractal analysis (WTMM - wavelet transform modulus maxima methodology) has been used to investigate the properties of bubble paths. It has been shown that bubble paths are the multifractals and the influence of previously departing bubbles on bubble trajectory is significant for bubble departure frequencyfb> 30 Hz.
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Battistella, Alessandro, Sander Aelen, Ivo Roghair e Martin van Sint Annaland. "Euler–Lagrange Modeling of Bubbles Formation in Supersaturated Water". ChemEngineering 2, n. 3 (24 agosto 2018): 39. http://dx.doi.org/10.3390/chemengineering2030039.

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Phase transition, and more specifically bubble formation, plays an important role in many industrial applications, where bubbles are formed as a consequence of reaction such as in electrolytic processes or fermentation. Predictive tools, such as numerical models, are thus required to study, design or optimize these processes. This paper aims at providing a meso-scale modelling description of gas–liquid bubbly flows including heterogeneous bubble nucleation using a Discrete Bubble Model (DBM), which tracks each bubble individually and which has been extended to include phase transition. The model is able to initialize gas pockets (as spherical bubbles) representing randomly generated conical nucleation sites, which can host, grow and detach a bubble. To demonstrate its capabilities, the model was used to study the formation of bubbles on a surface as a result of supersaturation. A higher supersaturation results in a faster rate of nucleation, which means more bubbles in the column. A clear depletion effect could be observed during the initial growth of the bubbles, due to insufficient mixing.
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Weber, Andreas, e Hans-Jörg Bart. "Flow Simulation in a 2D Bubble Column with the Euler-lagrange and Euler-euler Method". Open Chemical Engineering Journal 12, n. 1 (25 gennaio 2018): 1–13. http://dx.doi.org/10.2174/1874123101812010001.

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Object: Bubbly flows, as present in bubble column reactors, can be simulated using a variety of simulation techniques. It is presented, how Computational Fluid Dynamics (CFD) methods are used to simulate a pseudo 2D bubble column using Euler-Lagrange (EL) and Euler-Euler (EE) techniques. Method: The presented EL method uses the open access software OpenFOAM to solve bubble dynamics with bubble interactions computed via Monte Carlo methods. The estimated bubble size distribution and the predicted hold-up are compared with experimental data and other simulative EE work with a reasonable consensus for both. Benchmarks with state of the art EE simulations shows that the EL approach shows good performance if the bubble number stays at a certain level, as the EL approach scales linearly with the number of bubbles simulated. Therefore, different computational meshes have been used to account for influence of the resolution quality. Conclusion: The EL approach indicated faster solution for all realistic cases, only deliberate decrease of coalescence rates could push CPU time to the limits. Critical bubble number - when EE becomes superior to the EL approach - was estimated to be 40.000 in this particular case.
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Ning, Chen, e Fang Bing Wang. "Numerical Simulation of Hydrodynamics in Slurry Bubble Column Reactor". Applied Mechanics and Materials 303-306 (febbraio 2013): 2679–82. http://dx.doi.org/10.4028/www.scientific.net/amm.303-306.2679.

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Gas dispersion and solid suspension in industrial size slurry bubble column reactors for producing sodium dichromate are simulated numerically by using of computational fluid dynamics (CFD). The Eulerian multi-fluid model and standard k-ε turbulence model are used to describe the flow behavior in bubble columns. The simulated results show that gas is easy to flow toward the centre of the bubble column and in relatively high local gas holdup there. Installing gas-re-distributors in the bubble column is favorable for gas dispersion. Solid suspension in the bubble columns under the operating condition we investigated is relatively uniform.
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Zhang, Xinyu, e Goodarz Ahmadi. "Numerical Simulations of Liquid-Gas-Solid Three-Phase Flows in Microgravity". Journal of Computational Multiphase Flows 4, n. 1 (marzo 2012): 41–63. http://dx.doi.org/10.1260/1757-482x.4.1.41.

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Three-phase liquid-gas-solid flows under microgravity condition are studied. An Eulerian-Lagrangian computational model was developed and used in the simulations. In this approach, the liquid flow was modeled by a volume-averaged system of governing equations, whereas motions of particles and bubbles were evaluated using the Lagrangian trajectory analysis procedure. It was assumed that the bubbles remained spherical, and their shape variations were neglected. The bubble-liquid, particle-liquid and bubbl-particle two-way interactions were accounted for in the analysis. The discrete phase equations used included drag, lift, buoyancy, and virtual mass forces. Particle-particle interactions and bubble-bubble interactions were accounted for by the hard sphere model. Bubble coalescence was also included in the model. The transient flow characteristics of the three-phase flow were studied; and the effects of gravity, inlet bubble size and g-jitter acceleration on variation of flow characteristics were discussed. The low gravity simulations showed that most bubbles are aggregated in the inlet region. Also, under microgravity condition, bubble transient time is much longer than that in normal gravity. As a result, the Sauter mean bubble diameter, which is proportional to the transient time of the bubble, becomes rather large, reaching to more than 9 mm. The bubble plume in microgravity exhibits a plug type flow behavior. After the bubble plume reaches the free surface, particle volume fraction increases along the height of the column. The particles are mainly located outside the bubble plume, with very few particles being retained in the plume. In contrast to the normal gravity condition, the three phases in the column are poorly mixed under microgravity conditions. The velocities of the three phases were also found to be of the same order. Bubble size significantly affects the characteristics of the three-phase flows under microgravity conditions. For the same inlet bubble number density, the flow with larger bubbles evolves faster. The simulation results showed that the effect of g-jitter acceleration on the gas-liquid-particle three phase flows is small.
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Più fonti

Tesi sul tema "Bubble column"

1

Urseanu, Maria Ioana. "Scaling up bubble column reactors". [S.l. : Amsterdam : s.n.] ; Universiteit van Amsterdam [Host], 2000. http://dare.uva.nl/document/83970.

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2

McMahon, Andrew Martin. "Modelling the flow behaviour of gas bubbles in a bubble column". Master's thesis, University of Cape Town, 2009. http://hdl.handle.net/11427/5441.

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Abstract (sommario):
Includes abstract.
Includes bibliographical references (leaves 96-99).
The bubble column reactor is commonly used in industry, although the fluid dynamics inside are not well understood. The challenges associated with solving multi phase flow problems arise from the complexity of the governing equations which have to be solved, which are typically mass, momentum and energy balances. These time-dependent problems need to include effects of turbulence and are computationally expensive when simulating the hydrodynamics of large bubble columns. In an attempt to reduce the computational expense in solving bubble column reactor models, a "cell" model is proposed which predicts the velocity flow field in the vicinity of a single spherical bubble. It is intended that this model would form the fundamental building block in a macroscale model framework that does predict the flow of multiple bubbles in the whole column. The non-linear Navier-Stokes (NVS) equations are used to model fluid flow around the bubble. This study focusses on the Reynolds number range where the linear Stokes equations can be used to accurately predict the flow around the bubble. The Stokes equations are mathematically easier to solve than the NVS equations and are thus less computationally expensive. The validity of the NVS model was tested against experimental data for the flow of water around a solid sphere and was found to be in close agreement for the Reynolds number range 25 to 80. The simulation results from the Stokes flow model were compared with those from the NVS flow model and were similar at Reynolds numbers below 1. The application is then in the partitioning of the bubble column into regions governed by either Stokes or NVS equations.
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3

Shi, Weibin. "Dynamic modelling and simulation of turbulent bubbly flow in bubble column reactors". Thesis, University of Nottingham, 2018. http://eprints.nottingham.ac.uk/53960/.

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Abstract (sommario):
Considerable progress in understand and predicting turbulent bubbly flow in bubble column reactors has been advanced over the last two decades or so using a combination of model development, computational techniques and well-designed experiments. However, there remain many modelling uncertainties mainly associated with inadequate physical prescriptions rather than numerical schemes. The present project addresses some of these questions, in particular in relation to the interactions between the deformable rising bubbles and the turbulent eddies, with the later which from liquid shear flow or in the wakes of bubbles. Recent literature on existing models and experimental studies of bubble column reactors is reviewed in Chapter 1. It appears that the correlations and phenomenal models developed from early-stage experimental studies have been implemented into CFD modelling, and in return, accelerates the developments of theoretical understandings of the flow characteristics in the bubble columns. The research efforts made from both CFD modelling and experimental studies to understand the complicated mechanisms of gas-liquid interactions have been summarised in this chapter. In chapter 2, the inlet conditions, as one of the important issues in the CFD simulations of bubble columns, have been addressed. A kinetic inlet model is proposed, which considers the effects of number and size of holes on the gas spargers, the volume flow rate, and the gas-phase velocity profile. The proposed model achieves similar accuracy as modelling the real sparger holes while the computational costs have been significantly reduced. Chapter 3 applies a CFD-PBM method to investigate the influence of various shapes of bubbles on the bubble breakage rate and bubble size distribution. Bubbles are classified into spherical, ellipsoidal and spherical-capped shapes, and explicitly calculated in the breakage kernel. The correlation of aspect ratio of ellipsoidal bubbles is developed base on dimensionless numbers, summarising the effect of buoyancy, surface tension, and viscosity. The surface energy and pressure head have been adopted as two competing breakage mechanisms with the energy density constraint has been used as the breakage criterion. The simulation results demonstrate improvements in the estimations of gas holdup, liquid velocity, and bubble size distribution, as well as strong enhancements in mass transfer prediction. The effects of the turbulent kinetic energy spectrum for the turbulent bubbly flow on the bubble breakage are considered in Chapter 4. The κ-3 power law scaling behaviour of bubble induced turbulence is considered together with the Kolmogorov -5/3 law to characterise the turbulent eddies that interact with the subsequent bubbles. A characteristic length scale Λ is used to approximately separate the shear turbulence and bubble induced turbulence. The implementation of the modified breakage model into CFD modelling shows a great improvement in the prediction of bubble breakage rate, which believes to be competitive to the results obtained from Chen et al. (2004) that has artificially increase of breakage rate by 10 times. In Chapter 5, the approaching velocities of collision bubbles that are under the influence of shear turbulence and bubble induced turbulence are clearly distinguished. The turbulence dissipation rate that strongly affects the estimation of collision time has been calculated by taking into account the turbulence generation and dissipation in the wakes of bubbles, especially considering the anisotropic feature of bubble induced turbulence in the Reynolds stress turbulence model by using extra source terms. The modified coalescence model properly addresses the coalescence rate for different sizes of binary bubble coalescence. Chapter 6 presents the experimental study of the spatial velocity fluctuations and the turbulence energy spectrum in the wakes of bubbles by using PIV and highspeed imaging techniques. The experimental results clearly demonstrate the existence of the κ-3 power law scaling region due to bubble induced turbulence. The theoretical analysis successfully shows that the scaling exponent of -3 to be robust from three different aspect. In sum, some important issues of the gas-liquid interactions in turbulent bubbly flows have been addressed in this project. The implication is that the liquid phase turbulence is strongly affected by the size and shape of rising bubbles. Meanwhile, it can be found from the turbulence energy spectrum that the behaviours of turbulent eddies in the wakes of bubbles are very different from those in shear flow, thereby strongly influencing the kernels of bubble coalescence and breakage and hence the model predicted bubble size distributions.
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4

Gandhi, Bimal C. "Hydrodynamic studies in a slurry bubble column". Thesis, National Library of Canada = Bibliothèque nationale du Canada, 1997. http://www.collectionscanada.ca/obj/s4/f2/dsk2/ftp04/mq28573.pdf.

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5

Sharp, David Anthony. "Simulation of a two-dimensional bubble column". Thesis, National Library of Canada = Bibliothèque nationale du Canada, 2000. http://www.collectionscanada.ca/obj/s4/f2/dsk1/tape3/PQDD_0009/MQ60174.pdf.

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6

Shen, Gang 1953. "Bubble swarm velocities in a flotation column". Thesis, McGill University, 1994. http://digitool.Library.McGill.CA:80/R/?func=dbin-jump-full&object_id=28529.

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Abstract (sommario):
A new fast response conductivity meter was developed and tested. The "five time constant" of the meter is 0.08 s which meets the requirement for measurements under the dynamic conditions relevant to this work.
In a laboratory column, a bubble interface was created by introducing a step change of gas flow, and the rising velocity of this interface, $u sb{in},$ was measured using a conductivity method with the new conductivity meter. A measurement of the three-dimensional bubble swarm velocity in the column was obtained by interpolation from the $u sb{in}$ measured as a function of $J sb{g2} vert J sb{g} sb1 ,$ where $J sb{g} sb1$ and $J sb{g} sb2$ are the superficial gas velocities before and after a step change of gas flowrate, respectively. This velocity was referred to as the hindered velocity, $u sb{h}.$ The buoyancy velocity, $u sb0 ,$ was readily determined by switching off the gas, i.e. $u sb0 = u sb{in}$ at $J sb{g} sb2 = 0.$
The average gas velocity, $u sb{g},$ was corrected to the local average gas velocity, $u sb{g,loc},$ to obtain the average gas velocity under the local pressure conditions at a given vertical position in the column. The experimental results showed that $u sb{h}$ was significantly less than $u sb{g,loc}$ (and $u sb{g}).$ This is because the $u sb{h}$ is the three-dimensional bubble swarm velocity and $u sb{g,loc}$ is the one-dimensional bubble swarm velocity. Unlike $u sb{g,loc},$ the $u sb{h}$ was constant along the column, which was supported by theoretical momentum analysis. The $u sb{h}$ is proposed as the key characteristic swarm velocity of the system.
For the air-water only system in the two-dimensional domain, using parabolic models for gas holdup and liquid circulation velocity profiles over the cross section of the column, the $u sb{h}$ could be fitted to the experimental data. For the air-water-frother system, the $u sb{h}$ could not be fitted to the experimental data which is attributed to the air bubbles adopting a circulatory flow pattern.
In the air-water only system under batch operation, Nicklin's derivation (1962), i.e. $u sb{g} = u sb0 + J sb{g},$ was supported only under restrictive conditions, namely $u sb{g}$ and $J sb{g}$ must be measured at atmospheric pressure. Considering the local values, the experiments showed that $u sb{g,loc}$ was not equal to $u sb0 + J sb{g,loc}.$ In the presence of frothers under batch or countercurrent operation, the experiments showed that Nicklin's derivation was not applicable even if atmospheric values of $u sb{g}$ and $J sb{g}$ were used.
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KHAN, KHURRAM IMRAN. "Fluid dynamic modelling of bubble column reactors". Doctoral thesis, Politecnico di Torino, 2014. http://hdl.handle.net/11583/2528494.

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Numerical simulations of rectangular shape bubble column reactors (BCR) are validated starting from preliminary simulations aimed at identifying proper simulation parameters for a given system and resulting up to the numerical simulation with mass transfer and chemical reactions. The transient, three dimensional simulations are carried out using FLUENT software and the results obtained for a system with low gas flow rate (48 L/h) indicated that we need enough fine mesh grid and appropriate closure of interfacial forces to predict reliably plume oscillation period, liquid axial velocity and gas holdup profiles. In case of high flow rate (260 L/h), we compared the results for the effect of different interfacial closure forces and change in inlet boundary condition for gas volume fraction. There is no change in hydrodynamic results when there is change in gas volume fraction at inlet boundary condition. The effect of virtual mass interfacial force on the simulation results is also negligible. However, the major effects of applying lift force on results of plume oscillation period, liquid axial velocity and gas holdup is predicted. For comparable simulation results to experimental data, it is suggested that requirement of enough fine grids and appropriate correlations for interfacial forces, especially the combination of drag and lift forces is necessary. To study the bubble size distribution in BCR the numerical simulations are carried out with QMOM population balance technique for air-water fluid system. After finalization of the generic moment boundary conditions with simulations with PBM using QMOM without breakage and coalescence phenomena, then we simulated the system with breakage and coalescence and eventually, the simulation results are compared with experimental and simulation data taken from the scientific literature. For better hydrodynamics results of BCR as compared to experimental results, the interfacial lift force with combination of drag force is predicted for QMOM. The discretization scheme for gas volume fraction and moments of first order upwind provided the expected results of bubble size distribution. The simulation result of QMOM with breakage and coalescence models were also in good agreement with hydrodynamics experimental results and simulation results of class methods and DQMOM for bubble size distribution results. The modelling of chemical absorption of pure CO2 gas in caustic solution is carried out in a rectangular BCR with identical simulation parameters settings of previous work. For applicability of available kinetic and physical data we developed concentration differential equations to estimate the species molar concentration with respect to time in MATLAB code. The obtained profiles of evaluation of concentration and pH were in similar fashion as compared to available CFD simulated concentration and pH profiles at a point in the bubble column with respect to time. CFD simulation taking into account the mass transfer and chemical reaction, the E-E approach is used with assumption of uniform bubble size for modelling of chemisorption of the CO2 gas bubbles into NaOH aqueous solution. The adopted models successfully predicted the hydrodynamics results and are in good agreement with experimental and simulation results, however, reaction processes results are not as per expectation and further improvement in adopted simulation methods is required for better results.
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8

Rajapakse, Sumanasiri D. N. "An experimental study on the effect of viscosity on micro-bubble size distribution and rise velocity in a bubble column". Thesis, Edith Cowan University, Research Online, Perth, Western Australia, 2022. https://ro.ecu.edu.au/theses/2527.

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Abstract (sommario):
Dissolved air flotation (DAF) is a proven solid-liquid separation technology that is being used in water and wastewater treatment as an alternative process to conventional sedimentation operation. Due to its smaller footprint and ability to cater for higher liquid loading rates, it is ideal in many urban water treatment plants where space is limited and is usually designed for larger capacities. DAF systems generate microscale air bubbles to lift suspended particles in influent solution to the top of a rectangular tank and remove them by scrapers. Due to the recent focus on different applications of micro and nanoscale air bubbles across many industrial operations, researchers and engineers are trying to explore the application of DAF in other industries such as mineral ore processing, chemical industries, and sludge thickening operation in wastewater treatment plants (WWTPs). However, these applications have yielded low treatment efficiencies and less predictable performances, which demands more studies on the use of DAF in the high solid concentration of solid-liquid separation applications. While higher solid concentrations alter several physicochemical parameters in influent, an increase in slurry solution viscosity is a major concern. As a result, this thesis sought to identify the effect of viscosity on the microbubble (MB) size distribution and rise velocities which are identified as among the main factors affecting DAF performance. A laboratory-scale micro bubble generation system attached with a bubble column was designed and built to investigate the effect of viscosity on system dynamics. Shadow imaging technology and particle image velocimetry were utilised to measure bubble size distribution and bubble rise velocities respectively for different viscosities. Solutions were prepared by mixing commercially available Xanthan Gum powder in different concentrations. The results of these experiments identified interesting variations of bubble sizes and rise velocities concerning viscosity (ranging from 1 mPas to 67.6 mPas). An increase in viscosity reduced bubble sizes and narrowed size distribution (from 60 - 200 μm to 30 – 70 μm) while reducing mean bubble rise velocities from 57 mm/s to 9 mm/s. The results of these experimental studies were critically analysed, and it was identified that reduction of bubble coalescence in high viscous solutions resulted in smaller bubble sizes, while increased drag forces slow down the rise velocity of bubbles. Moreover, this study provides essential baseline information for future studies when trying to improve DAF efficiency in high solid content applications during solidliquid separation operations.
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9

Rahimi, Rahbar. "Heat transfer in bubble columns". Thesis, University of Bath, 1988. https://ethos.bl.uk/OrderDetails.do?uin=uk.bl.ethos.380868.

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10

Syed, Alizeb Hussain. "Modeling of two & three phases bubble column". Thèse, Université de Sherbrooke, 2017. http://hdl.handle.net/11143/11431.

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Abstract (sommario):
Abstract : The industrial partner of this project uses a slurry bubble reactor for the production of biogenic methanol. In the latter syngas is dispersed into the slurry continuous phase containing both liquid and solid phases. The rising bubbles containing a wide spectrum of the bubbles sizes, interact with the continuous phase due to the interface momentum transfer. The latter includes the drag, lift, wall lubrication and turbulent dispersion terms that require average bubble size, which needs to be calculated. One way to predict this average bubble size is by using population balance model (PBM), which can be coupled with the Eulerian framework. PBM also needs closure kernels for the bubble coalescence and bubble breakup. In this study, the influence of bubble coalescence and bubble breakup kernels have been studied in two- and three-phase system using eulerian approach, which solves momentum equation for each phase. The influence of the mesh sizes, number of bubble classes, numerical schemes, wall lubrication force and turbulent dispersion force are also included. In the two-phase system, results show that the Luo coalescence model needs to be tuned when used in combination with the Luo breakup kernel. The combination of the Luo coalescence and the Lehr breakup kernels (Luo-Lehr) show promising time-averaged radial profiles of gas holdup and axial liquid velocity as compared to empirical values. In the three-phase system, the combination of the Luo coalescence and the Lehr breakup kernels (Luo-Lehr) and the Luo coalescence and the Luo breakup kernels (Luo-Luo) predict convincing time-averaged radial profile of axial solid velocity as compared to experiments. However, at an elevated superficial gas velocity, a non-realistic behavior was predicted when compared to empirical observations. The sensitivity analysis results show that the 3 mm mesh size depicts a trend similar to the empirical values of the radial profiles of the gas holdup, axial liquid velocity, and solid axial velocity. The number of bubble classes influence the predicted bubble size distribution in the three-phase system while the numerical discretizing schemes have no influence on the results. The bench simulation results show that the inclusion of the turbulent dispersion term using a single porous tubular sparger influences the hydrodynamic behavior of the bubble column.
Le partenaire industriel de ce projet utilise un réacteur à suspension à trois phases pour la production de méthanol biogénique. Dans celui-ci, le gaz de synthèse est diffusé par barbotement dans la phase à suspension qui contient à la fois les phases liquide et solide. Les bulles en ascension présentent un large spectre de tailles et interagissent avec la phase à suspension en échangeant de la quantité de mouvement via leurs surfaces. Cet échange comprend les forces de trainé, de portance, de lubrification en proche parois et de dispersion par turbulence; lesquelles requièrent notamment le calcul de la taille moyenne des bulles. Une façon de prédire numériquement cette taille moyenne est de recourir à un modèle de bilan de population (PBM, de l’anglais Population Balance Model), qui peut être couplé avec un model multiphasique eulérien. Un tel PBM a requière des modèles de fermetures pour la coalescence et la rupture des bulles. Dans la présente étude, l'influence des modèles noyaux de coalescence et de rupture des bulles a été étudiée pour des systèmes à deux et à trois phases en utilisant l’approche eulérienne. L'influence de la taille du maillage, du nombre de classes de bulles, du schéma numérique, de la force de lubrification en proche parois et de la force de dispersion par turbulence sont également incluses. Dans un système bi-phasique, les résultats montrent que le modèle de coalescence Luo doit être ajusté lorsqu'il est utilisé en combinaison avec le noyau de rupture Luo. La combinaison des noyaux de coalescence Luo et de rupture Lehr (Luo-Lehr) montrent des profils radiaux moyennés dans le temps qui sont valides pour la concentration de gaz et la vitesse axiale du liquide par rapport aux mesures expérimentales. Dans le système triphasé, la combinaison des modèles noyaux de coalescence de Luo et de rupture de Lehr (Luo-Lehr) et de la coalescence de Luo et de rupture de Luo (Luo-Luo) prédisent des profils radiaux moyennés dans le temps qui sont valides pour la vitesse axiale moyenné dans le temps par rapport aux expériences. Cependant, à une vitesse de gaz superficielle élevée, ces profils prédisent un comportement non réaliste par rapport aux observations empiriques. Les résultats de l'analyse de sensibilité du maillage montrent qu’avec des cellules de 3 mm, le model prédit une tendance similaire aux valeurs empiriques pour les profils radiaux de concentration du gaz, de vitesse axiale du liquide et de vitesse axiale solide. Le nombre de classes de bulles influe sur les distributions prédites de taille de bulle dans le système triphasé alors que les schémas de discrétisation numériques n'ont aucune influence sur les résultats. Les résultats des simulations d’un banc d’essai avec diffuseur à bulles poreux montrent que tenir compte du terme de dispersion influence le comportement hydrodynamique de la colonne à bulles.
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Libri sul tema "Bubble column"

1

Deckwer, Wolf-Dieter. Bubble column reactors. Chichester: Wiley, 1992.

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2

Wadley, R. J. Studies of a bubble column reactor system for finechemicalsproduction. Manchester: UMIST, 1994.

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3

Sam, Abbas. Single bubble behaviour study in a flotation column: Abbas Sam. Montréal, Qué: McGill University, 1995.

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4

Lu, Xiao-Xiong. A study of the characteristics of a novel cocurrent downflow bubble column contactor for use as athree-phase reactor. Birmingham: University of Birmingham, 1988.

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5

Sulidis, Andrew Thomas. Application of the occurrent downflow bubble column contactor (CDC) for use as a photocatalytic reactor and associated mass transfer studies. Birmingham: University of Birmingham, 1995.

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6

Olajuyigbe, Johnson Temitope. Behaviour of bubble columns with two and three phases. Birmingham: Aston University. Department of Chemical Engineering, 1986.

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7

Letzel, Martijn. Hydrodynamics and mass transfer in bubble columns at elevated pressures. Delft: Delft University, 1998.

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8

E, El-Shall Hassan, Gruber Glenn A, University of Florida e Florida Institute of Phosphate Research., a cura di. Bubble generation, design, modeling, and optimization of novel flotation columns for phosphate beneficiation: Final report. Bartow, Fla: Florida Institute of Phosphate Research, 2001.

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9

Deckwer, Wolf-Dieter. Bubble Column Reactions. Wiley, 1991.

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10

MANDAL, AJAY. GAS-LIQUID TWO-PHASE FLOW IN AN EJECTOR INDUCED DOWNFLOW BUBBLE COLUMN. LAP Lambert Academic Publishing, 2010.

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Capitoli di libri sul tema "Bubble column"

1

Jakobsen, Hugo A. "Bubble Column Reactors". In Chemical Reactor Modeling, 883–935. Cham: Springer International Publishing, 2014. http://dx.doi.org/10.1007/978-3-319-05092-8_8.

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2

Lübbert, Andreas. "Bubble Column Bioreactors". In Bioreaction Engineering, 247–73. Berlin, Heidelberg: Springer Berlin Heidelberg, 2000. http://dx.doi.org/10.1007/978-3-642-59735-0_9.

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3

Gamwo, Isaac K., Dimitri Gidaspow e Jonghwun Jung. "Slurry Bubble Column Reactor Optimization". In ACS Symposium Series, 225–52. Washington, DC: American Chemical Society, 2007. http://dx.doi.org/10.1021/bk-2007-0959.ch017.

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4

Yoon, S. W., K. J. Park, L. A. Crum, M. Nicholas, R. A. Roy, A. Prosperetti e N. Q. Lu. "Collective Oscillations in a Bubble Column". In Natural Physical Sources of Underwater Sound, 371–78. Dordrecht: Springer Netherlands, 1993. http://dx.doi.org/10.1007/978-94-011-1626-8_29.

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5

Duduković, M. P., e N. Devanathan. "Bubble Column Reactors: Some Recent Developments". In Chemical Reactor Technology for Environmentally Safe Reactors and Products, 353–77. Dordrecht: Springer Netherlands, 1992. http://dx.doi.org/10.1007/978-94-011-2747-9_14.

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6

Nitsche, M., e R. Gbadamosi. "Equilibria, Bubble Points, Dewpoints, Flash Calculations, and Activity Coefficients". In Practical Column Design Guide, 39–83. Cham: Springer International Publishing, 2017. http://dx.doi.org/10.1007/978-3-319-51688-2_2.

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7

Godo, S., K. Junghans, A. Lapin e A. Lübbert. "Dynamics of the Flow in Bubble Column Reactors". In Bubbly Flows, 53–66. Berlin, Heidelberg: Springer Berlin Heidelberg, 2004. http://dx.doi.org/10.1007/978-3-642-18540-3_6.

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8

Deckwer, Wolf-Dieter. "Design and Simulation of Bubble Column Reactors". In Chemical Reactor Design and Technology, 411–61. Dordrecht: Springer Netherlands, 1986. http://dx.doi.org/10.1007/978-94-009-4400-8_12.

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9

Schmitz, D., e D. Mewes. "Experimental and theoretical investigation of instationary bubble flow and mass transfer in a bubble column". In Bubbly Flows, 117–27. Berlin, Heidelberg: Springer Berlin Heidelberg, 2004. http://dx.doi.org/10.1007/978-3-642-18540-3_10.

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10

Lecca, Paola, e Angela Re. "Observability of Bacterial Growth Models in Bubble Column Bioreactors". In Computational Intelligence Methods for Bioinformatics and Biostatistics, 309–22. Cham: Springer International Publishing, 2020. http://dx.doi.org/10.1007/978-3-030-63061-4_27.

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Atti di convegni sul tema "Bubble column"

1

Shimada, Naoki, Rina Saiki, Abhinav Dhar e Akio Tomiyama. "Liquid Mixing in a Bubble Column". In ASME-JSME-KSME 2011 Joint Fluids Engineering Conference. ASMEDC, 2011. http://dx.doi.org/10.1115/ajk2011-04006.

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Abstract (sommario):
In most of the bubble column design, it is assumed that liquid phase is well mixed and spatial distributions of molar concentrations for all components are uniform. However, there is liquid mixing in actual bubble column reactors. The performance of a bubble column strongly depends on the liquid mixing induced by bubbles in the column. Those assumptions therefore cause some errors in column optimum design. Only a few quantitative investigations have been carried out on two-phase turbulence and liquid mixing. In this study, numerical simulations for liquid mixing in a bubble column have been carried out and compared with experiments. The transient behavior of tracer concentration was measured for test columns of 0.3 m in diameter. The height of the columns was 1 m. Bubbles were supplied by using two types of spargers: ring spargers and a perforated plate. A hybrid method, NP2-3D, which is based on the combination of multi-fluid and interface tracking methods, was used to simulate the flow. In a two-phase turbulence model, linear superposition of bubble-induced turbulence and shear-induced turbulence was assumed. Numerical prediction could qualitatively describe the effects of column diameter and gas inlet on the liquid mixing in a column.
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2

Bai, W., Niels G. Deen, J. A. M. Kuipers, Liejin Guo, D. D. Joseph, Y. Matsumoto, Y. Sommerfeld e Yueshe Wang. "Bubble properties of heterogeneous bubbly flows in a square bubble column". In THE 6TH INTERNATIONAL SYMPOSIUM ON MULTIPHASE FLOW, HEAT MASS TRANSFER AND ENERGY CONVERSION. AIP, 2010. http://dx.doi.org/10.1063/1.3366427.

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3

Mohagheghian, Shahrouz, e Brian R. Elbing. "Study of Bubble Size and Velocity in a Vibrating Bubble Column". In ASME 2016 Fluids Engineering Division Summer Meeting collocated with the ASME 2016 Heat Transfer Summer Conference and the ASME 2016 14th International Conference on Nanochannels, Microchannels, and Minichannels. American Society of Mechanical Engineers, 2016. http://dx.doi.org/10.1115/fedsm2016-1056.

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Bubble columns are two-phase and three-phase reactors in which a gas flow drives a liquid flow and allows transport phenomena’s to take place. With a broad application from aeration of organic organisms in bio-rectors to hydrogenation of coal slurries in the Fischer-Tropsch process and production of synthetic fuel, bubble column reactors are cheap and easy to operate. In this work bubble size was studied in a bubble column and effect of injector size and gas superficial velocity was investigated. Results showed larger bubble size as gas superficial velocity was increased. It was previously shown that vibration increases the mass transfer between phases, which one active mechanism is that vibration increases the void fraction and with more gas in contact with liquid mass transfer rate increases. To check that a shaker table setup capable of generating vibration in the range of 5–15 Hz of frequency at 5 mm of amplitude using an eccentric drive mechanism was refurbished to study the bubble velocity and void fraction under vibration. The experimental setup was first verified to check if tests are repeatable and also the results are in agreement with literature. Void fraction, bubble size and velocity was measured and comparison with previously published data showed good agreement. Bubble size measurements in a stationary column showed that over the range tested bubble size increases with increasing gas superficial velocity. Bubble velocity decreases when gas superficial velocity was increased. Vibration showed a gradual reduction in bubble velocity as vibration frequency was increased.
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4

Chernyshev, Alexander, e Alexander Schmidt. "Bubble column dynamics with bubble induced turbulence and dispersion". In 11TH INTERNATIONAL CONFERENCE OF NUMERICAL ANALYSIS AND APPLIED MATHEMATICS 2013: ICNAAM 2013. AIP, 2013. http://dx.doi.org/10.1063/1.4825691.

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5

Maekawa, Munenori, Naoki Shimada, Kouji Kinoshita, Akira Sou e Akio Tomiyama. "Numerical Simulation of Heterogeneous Bubbly Flow in a Bubble Column". In ASME 2006 2nd Joint U.S.-European Fluids Engineering Summer Meeting Collocated With the 14th International Conference on Nuclear Engineering. ASMEDC, 2006. http://dx.doi.org/10.1115/fedsm2006-98178.

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Numerical methods for predicting heterogeneous bubbly flows are indispensable for the design of a Fisher-Tropsh reactor for GTL (Gas To Liquid). It is necessary to take into account bubble size distribution determined by bubble coalescence and breakup for the accurate prediction of heterogeneous bubbly flows. Hence we implemented several bubble coalescence and breakup models into the (N+2) field model, which is a hybrid combination of an interface tracking method and a multi-fluid model. Void and bubble size distributions in an open rectangular bubble column were measured and compared with predicted ones. As a result, the following conclusions were obtained: (1) Void and bubble size distributions were not affected by inlet bubble sizes because the bubble size distribution reaches an equilibrium state at which the birth rate is equal to the death rate, and (2) the combination of Luo’s bubble breakup model and a coalescence model consisting of Prince & Blanch’s model and Wang’s wake entrainment model gave good predictions.
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6

Mortuza, S. M., Anil Kommareddy, Stephen P. Gent e Gary A. Anderson. "Computational and Experimental Investigation of Bubble Circulation Patterns Within a Column Photobioreactor". In ASME 2011 5th International Conference on Energy Sustainability. ASMEDC, 2011. http://dx.doi.org/10.1115/es2011-54205.

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This research project investigates bubble and liquid circulation patterns in a vertical column photobioreactor (PBR) both experimentally as well as computationally using Computational Fluid Dynamics (CFD). Dispersed gas–liquid flow in the rectangular bubble column PBR are modeled using Eulerian–Lagrangian approach. A low Reynolds number k–ε CFD model is used to describe the flow pattern near the wall. Bubble size distribution measurements are carried out using a high-speed digital camera. A flat surface bubble column PBR is used to achieve sufficient light penetration into the system. Carbon dioxide, which is necessary for photosynthetic microalgae growth, is added to the sparged air. The results are validated with experimental data and from current literature. Design parameters, bubble flow pattern and internal hydrodynamics of a bubble column reactor were studied and the numerical simulations presented for the hydrodynamics in a bubble column PBR account for bubble phenomena that have not been sufficiently accounted for in previous research. Bubble size and shape affect the hydrodynamics as does bubble interaction with other bubbles (multiple bubbles in a flow versus single bubbles and wall effects on bubble(s) which are not symmetrical or bubbles not centered on the reactor cross-section). Understanding the bubble movement patterns will aid in predicting other design parameters like mass transfer (bubble to liquid and liquid to bubble), heat transfer (within the PBR and between the PBR and environment surrounding the PBR), and interaction forces inside the PBR.
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7

Pradeep, Arjun, Anil Kumar Sharma, M. P. Rajiniganth, N. Malathi, M. Sivaramakrishna, D. Ponraju, B. K. Nashine e P. Selvaraj. "BUBBLE RISE DYNAMICS IN WATER COLUMN". In Proceedings of the 24th National and 2nd International ISHMT-ASTFE Heat and Mass Transfer Conference (IHMTC-2017). Connecticut: Begellhouse, 2018. http://dx.doi.org/10.1615/ihmtc-2017.990.

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8

Ahmadi, Goodarz, e Xinyu Zhang. "Three-Phase Liquid-Gas-Solid Flows in a Bubble Column". In ASME 2005 Fluids Engineering Division Summer Meeting. ASMEDC, 2005. http://dx.doi.org/10.1115/fedsm2005-77071.

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An Eulerian-Lagrangian computational model for simulations of gas-liquid-solid flows in three-phase slurry reactors is developed. In this approach, the liquid flow is modeled using a volume-averaged system of governing equations, whereas motions of bubbles and particles are evaluated by Lagrangian trajectory analysis procedure. It is assumed that the bubbles remain spherical and their shape variations are neglected. The two-way interactions between bubble-liquid and particle-liquid are included in the analysis. The discrete phase equations include drag, lift, buoyancy, and virtual mass forces. Particle-particle interactions and bubble-bubble interactions are accounted for by the hard sphere model approach. The bubble coalescence is also included in the model. The predicted results are compared with the experimental data, and good agreement is obtained. The transient flow characteristics of the three-phase flow are studied and the effects of bubble size on variation of flow characteristics are discussed. The simulations show that the transient characteristics of the three-phase flow in a column are dominated by time-dependent staggered vortices. The bubble plume moves along the S-shape path and exhibits an oscillatory behavior. While particles are mainly located outside the vortices, some bubbles and particles are retained in the vortices. Bubble upward velocities are much larger than both liquid and particle velocities. In the lower part of the column, particle upward velocities are slightly smaller than the liquid velocities, while in the upper part of the column, particle upward velocities are slightly larger. The bubble size significantly affects the characteristics of the three-phase flows and flows with larger bubbles appear to evolve faster.
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9

Moreira de Freitas, Ana Paula, Jonathan Utzig e João Marcelo Vedovotto. "Bubbles Coalescence Modeling and Phase Interactions in a Squared Bubble Column". In 13th Spring School on Transition and Turbulence. ABCM, 2022. http://dx.doi.org/10.26678/abcm.eptt2022.ept22-0003.

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10

Tow, Emily W., e John H. Lienhard. "Analytical Modeling of a Bubble Column Dehumidifier". In ASME 2013 Heat Transfer Summer Conference collocated with the ASME 2013 7th International Conference on Energy Sustainability and the ASME 2013 11th International Conference on Fuel Cell Science, Engineering and Technology. American Society of Mechanical Engineers, 2013. http://dx.doi.org/10.1115/ht2013-17763.

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Bubble column dehumidifiers are a compact, inexpensive alternative to conventional fin-tube dehumidifiers for humidification-dehumidification (HDH) desalination, a technology that has promising applications in small-scale desalination and industrial water remediation. In this paper, algebraic equations for relevant mean heat and mass transfer driving forces are developed for improved modeling of bubble column dehumidifiers. Because mixing in the column ensures a uniform liquid temperature, the bubble column can be modeled as two single stream heat exchangers in contact with the column liquid: the seawater side, for which a log-mean temperature difference is appropriate, and the gas side, which has a varying heat capacity and mass exchange. Under typical conditions, a log-mean mass fraction difference is shown to drive latent heat transfer, and an expression for the mean temperature difference of the moist gas stream is presented. These expressions will facilitate modeling of bubble column heat and mass exchangers.
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Rapporti di organizzazioni sul tema "Bubble column"

1

Dudukovic, M. P. Novel techniques for slurry bubble column hydrodynamics. Office of Scientific and Technical Information (OSTI), maggio 1999. http://dx.doi.org/10.2172/775467.

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2

Dimitri Gidaspow. Hydrodynamic models for slurry bubble column reactors. Office of Scientific and Technical Information (OSTI), ottobre 1996. http://dx.doi.org/10.2172/750375.

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3

Dimitri Gidaspow. Hydrodynamic models for slurry bubble column reactor. Office of Scientific and Technical Information (OSTI), gennaio 1997. http://dx.doi.org/10.2172/750383.

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4

Shollenberger, K. A., J. R. Torczynski, N. B. Jackson e T. J. O`Hern. Experimental characterization of slurry bubble-column reactor hydrodynamics. Office of Scientific and Technical Information (OSTI), settembre 1997. http://dx.doi.org/10.2172/292851.

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5

Sankaran, Ramanan, Vimal Ramanuj, Luka Malenica, Leonardo Spanu e Guoqiang Yang. Simulation of Transport Phenomena in Bubble Column Reactors. Office of Scientific and Technical Information (OSTI), settembre 2022. http://dx.doi.org/10.2172/1894210.

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6

Bernard A. Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR)TECHNOLOGY. Office of Scientific and Technical Information (OSTI), giugno 2000. http://dx.doi.org/10.2172/783047.

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Bernard A. Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), giugno 2000. http://dx.doi.org/10.2172/783049.

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8

Toseland, B. A. Engineering Development of Slurry Bubble Column Reactor (SBCR) Technology. Office of Scientific and Technical Information (OSTI), ottobre 1998. http://dx.doi.org/10.2172/1304.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), gennaio 2000. http://dx.doi.org/10.2172/793999.

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Bernard A Toseland, Ph D. ENGINEERING DEVELOPMENT OF SLURRY BUBBLE COLUMN REACTOR (SBCR) TECHNOLOGY. Office of Scientific and Technical Information (OSTI), gennaio 2002. http://dx.doi.org/10.2172/794000.

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