Mixing and gas dispersion in mineral flotation cells
Identifieur interne :
003D41 ( PascalFrancis/Curation );
précédent :
003D40;
suivant :
003D42
Mixing and gas dispersion in mineral flotation cells
Auteurs : G. M. Evans [
Australie] ;
E. Doroodchi [
Australie] ;
G. L. Lane [
Australie] ;
P. T. L. Koh [
Australie] ;
M. P. Schwarz [
Australie]
Source :
-
Chemical engineering research & design [ 0263-8762 ] ; 2008.
RBID : Pascal:10-0514602
Descripteurs français
- Pascal (Inist)
- Mélangeage,
Dispersion,
Flottation,
Appareil agité,
Bulle,
Phase liquide,
Agitateur,
Collision,
Turbulence,
Corrélation,
Analyse corrélation,
Modélisation,
Ecoulement gaz liquide,
Ecoulement diphasique,
Mécanique fluide numérique,
Dimension particule,
Retenue gaz,
Hydrodynamique,
Prédiction,
Chargement,
Adhérence,
Mousse (émulsion),
Débit fluide.
- Wicri :
English descriptors
- KwdEn :
- Adhesion,
Agitator,
Bubble,
Collision,
Computational fluid dynamics,
Correlation,
Correlation analysis,
Dispersion,
Flotation,
Foam,
Gas holdup,
Gas liquid flow,
Hydrodynamics,
Liquid phase,
Loading,
Mixing,
Modeling,
Particle size,
Prediction,
Stirred vessel,
Turbulence,
Two phase flow.
Abstract
Mineral flotation in mechanically agitated vessels (cells) involves complex interaction between bubbles, particles and the liquid phase. Ideally, just enough power input from the impeller is needed to so that the frequency of particle-bubble collision and attachment is maximised, while at the same time detachment events are minimised. This paper firstly investigated how the slip velocity of 2-10 mm diameter bubbles, a size commonly encountered in flotation devices, was influenced by turbulence intensity. The measurements confirmed the earlier correlation by [Lane, G.L., 2005, Numerical modelling of gas-liquid flow in stirred tanks, Ph.D. Thesis, University of Newcastle, Australia], which was then inputted into a computational fluid dynamic model to describe the gas dispersion in a mechanically agitated tank. The model provided turbulence intensity values that were then coupled with both slip velocity and critical Weber number models to generate both bubble size and gas holdup profiles for the entire vessel. Moreover, a simple equation was introduced to allow prediction of cavity formation behind the rotating impeller blades, which is a common occurrence in most flotation cells they normally operate at high gas loadings. This inclusion allowed the model to predict power reduction resulting from the presence of the cavities. Finally, extension of the computational model to include flotation hydrodynamics, such as probabilities of collision, adhesion and stabilisation of the particles at the bubble surface, is also described. The model is able to compute net attachment rates, and hence the particle flux entering the froth recovery phase, as a function of bubble and particle diameter, gas flowrate and power input.
| pA |
| A01 | 01 | 1 | | @0 0263-8762 |
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| A02 | 01 | | | @0 CERDEE |
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| A03 | | 1 | | @0 Chem. eng. res. des. |
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| A05 | | | | @2 86 |
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| A06 | | | | @2 12 |
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| A08 | 01 | 1 | ENG | @1 Mixing and gas dispersion in mineral flotation cells |
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| A09 | 01 | 1 | ENG | @1 ISMIP-VI |
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| A11 | 01 | 1 | | @1 EVANS (G. M.) |
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| A11 | 02 | 1 | | @1 DOROODCHI (E.) |
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| A11 | 03 | 1 | | @1 LANE (G. L.) |
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| A11 | 04 | 1 | | @1 KOH (P. T. L.) |
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| A11 | 05 | 1 | | @1 SCHWARZ (M. P.) |
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| A12 | 01 | 1 | | @1 XUEREB (Catherine) @9 ed. |
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| A12 | 02 | 1 | | @1 TANGUY (Philippe) @9 ed. |
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| A14 | 01 | | | @1 School of Engineering, University of Newcastle @2 Callaghan, NSW 2308 @3 AUS @Z 1 aut. @Z 2 aut. |
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| A14 | 02 | | | @1 CSIRO Minerals, Box 312 @2 Clayton South, Vic 3169 @3 AUS @Z 3 aut. @Z 4 aut. @Z 5 aut. |
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| A15 | 01 | | | @1 Laboratoire de Génie Chimique @2 Toulouse @3 FRA @Z 1 aut. |
|---|
| A15 | 02 | | | @1 Ecole Polytechnique @2 Montreal @3 CAN @Z 2 aut. |
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| A18 | 01 | 1 | | @1 Procter & Gamble @3 INC @9 org-cong. |
|---|
| A20 | | | | @1 1350-1362 |
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| A21 | | | | @1 2008 |
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| A23 | 01 | | | @0 ENG |
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| A43 | 01 | | | @1 INIST @2 4284 @5 354000185132680050 |
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| A44 | | | | @0 0000 @1 © 2010 INIST-CNRS. All rights reserved. |
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| A45 | | | | @0 1 p.3/4 |
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| A47 | 01 | 1 | | @0 10-0514602 |
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| A60 | | | | @1 P @2 C |
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| A61 | | | | @0 A |
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| A64 | 01 | 1 | | @0 Chemical engineering research & design |
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| A66 | 01 | | | @0 NLD |
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| C01 | 01 | | ENG | @0 Mineral flotation in mechanically agitated vessels (cells) involves complex interaction between bubbles, particles and the liquid phase. Ideally, just enough power input from the impeller is needed to so that the frequency of particle-bubble collision and attachment is maximised, while at the same time detachment events are minimised. This paper firstly investigated how the slip velocity of 2-10 mm diameter bubbles, a size commonly encountered in flotation devices, was influenced by turbulence intensity. The measurements confirmed the earlier correlation by [Lane, G.L., 2005, Numerical modelling of gas-liquid flow in stirred tanks, Ph.D. Thesis, University of Newcastle, Australia], which was then inputted into a computational fluid dynamic model to describe the gas dispersion in a mechanically agitated tank. The model provided turbulence intensity values that were then coupled with both slip velocity and critical Weber number models to generate both bubble size and gas holdup profiles for the entire vessel. Moreover, a simple equation was introduced to allow prediction of cavity formation behind the rotating impeller blades, which is a common occurrence in most flotation cells they normally operate at high gas loadings. This inclusion allowed the model to predict power reduction resulting from the presence of the cavities. Finally, extension of the computational model to include flotation hydrodynamics, such as probabilities of collision, adhesion and stabilisation of the particles at the bubble surface, is also described. The model is able to compute net attachment rates, and hence the particle flux entering the froth recovery phase, as a function of bubble and particle diameter, gas flowrate and power input. |
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| C02 | 01 | X | | @0 001D07Q06 |
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| C02 | 02 | X | | @0 001D07E |
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| C02 | 03 | X | | @0 001D07D |
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| C03 | 01 | X | FRE | @0 Mélangeage @5 01 |
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| C03 | 01 | X | ENG | @0 Mixing @5 01 |
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| C03 | 01 | X | SPA | @0 Mezclado @5 01 |
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| C03 | 02 | X | FRE | @0 Dispersion @5 02 |
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| C03 | 02 | X | ENG | @0 Dispersion @5 02 |
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| C03 | 02 | X | SPA | @0 Dispersión @5 02 |
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| C03 | 03 | X | FRE | @0 Flottation @5 03 |
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| C03 | 03 | X | ENG | @0 Flotation @5 03 |
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| C03 | 03 | X | SPA | @0 Flotación @5 03 |
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| C03 | 04 | X | FRE | @0 Appareil agité @5 04 |
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| C03 | 04 | X | ENG | @0 Stirred vessel @5 04 |
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| C03 | 04 | X | SPA | @0 Aparato agitado @5 04 |
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| C03 | 05 | X | FRE | @0 Bulle @5 05 |
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| C03 | 05 | X | ENG | @0 Bubble @5 05 |
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| C03 | 05 | X | SPA | @0 Ampolla @5 05 |
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| C03 | 06 | X | FRE | @0 Phase liquide @5 06 |
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| C03 | 06 | X | ENG | @0 Liquid phase @5 06 |
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| C03 | 06 | X | SPA | @0 Fase líquida @5 06 |
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| C03 | 07 | X | FRE | @0 Agitateur @5 07 |
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| C03 | 07 | X | ENG | @0 Agitator @5 07 |
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| C03 | 07 | X | SPA | @0 Agitador @5 07 |
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| C03 | 08 | X | FRE | @0 Collision @5 08 |
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| C03 | 08 | X | ENG | @0 Collision @5 08 |
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| C03 | 08 | X | SPA | @0 Colisión @5 08 |
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| C03 | 09 | X | FRE | @0 Turbulence @5 09 |
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| C03 | 09 | X | ENG | @0 Turbulence @5 09 |
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| C03 | 09 | X | SPA | @0 Turbulencia @5 09 |
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| C03 | 10 | X | FRE | @0 Corrélation @5 10 |
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| C03 | 10 | X | ENG | @0 Correlation @5 10 |
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| C03 | 10 | X | SPA | @0 Correlación @5 10 |
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| C03 | 11 | X | FRE | @0 Analyse corrélation @5 11 |
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| C03 | 11 | X | ENG | @0 Correlation analysis @5 11 |
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| C03 | 11 | X | SPA | @0 Análisis correlación @5 11 |
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| C03 | 12 | X | FRE | @0 Modélisation @5 12 |
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| C03 | 12 | X | ENG | @0 Modeling @5 12 |
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| C03 | 12 | X | SPA | @0 Modelización @5 12 |
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| C03 | 13 | X | FRE | @0 Ecoulement gaz liquide @5 13 |
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| C03 | 13 | X | ENG | @0 Gas liquid flow @5 13 |
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| C03 | 13 | X | SPA | @0 Flujo gas líquido @5 13 |
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| C03 | 14 | X | FRE | @0 Ecoulement diphasique @5 14 |
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| C03 | 14 | X | ENG | @0 Two phase flow @5 14 |
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| C03 | 14 | X | SPA | @0 Flujo difásico @5 14 |
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| C03 | 15 | X | FRE | @0 Mécanique fluide numérique @5 15 |
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| C03 | 15 | X | ENG | @0 Computational fluid dynamics @5 15 |
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| C03 | 15 | X | SPA | @0 Mecánica fluido numérica @5 15 |
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| C03 | 16 | X | FRE | @0 Dimension particule @5 16 |
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| C03 | 16 | X | ENG | @0 Particle size @5 16 |
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| C03 | 16 | X | SPA | @0 Dimensión partícula @5 16 |
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| C03 | 17 | X | FRE | @0 Retenue gaz @5 17 |
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| C03 | 17 | X | ENG | @0 Gas holdup @5 17 |
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| C03 | 17 | X | SPA | @0 Detención gas @5 17 |
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| C03 | 18 | X | FRE | @0 Hydrodynamique @5 18 |
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| C03 | 18 | X | ENG | @0 Hydrodynamics @5 18 |
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| C03 | 18 | X | SPA | @0 Hidrodinámica @5 18 |
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| C03 | 19 | X | FRE | @0 Prédiction @5 19 |
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| C03 | 19 | X | ENG | @0 Prediction @5 19 |
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| C03 | 19 | X | SPA | @0 Predicción @5 19 |
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| C03 | 20 | X | FRE | @0 Chargement @5 20 |
|---|
| C03 | 20 | X | ENG | @0 Loading @5 20 |
|---|
| C03 | 20 | X | SPA | @0 Cargamento @5 20 |
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| C03 | 21 | X | FRE | @0 Adhérence @5 21 |
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| C03 | 21 | X | ENG | @0 Adhesion @5 21 |
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| C03 | 21 | X | SPA | @0 Adherencia @5 21 |
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| C03 | 22 | X | FRE | @0 Mousse (émulsion) @5 22 |
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| C03 | 22 | X | ENG | @0 Foam @5 22 |
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| C03 | 22 | X | SPA | @0 Espuma @5 22 |
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| C03 | 23 | X | FRE | @0 Débit fluide @4 INC @5 32 |
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| N21 | | | | @1 347 |
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| N44 | 01 | | | @1 OTO |
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| N82 | | | | @1 OTO |
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|
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| pR |
| A30 | 01 | 1 | ENG | @1 International Symposium on Mixing in Industrial Processes VI (ISMIP-6) @2 6 @3 Niagara Falls CAN @4 2008-08-17 |
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Le document en format XML
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</publicationStmt><sourceDesc><biblStruct><analytic><title xml:lang="en" level="a">Mixing and gas dispersion in mineral flotation cells</title>
<author><name sortKey="Evans, G M" sort="Evans, G M" uniqKey="Evans G" first="G. M." last="Evans">G. M. Evans</name>
<affiliation wicri:level="1"><inist:fA14 i1="01"><s1>School of Engineering, University of Newcastle</s1>
<s2>Callaghan, NSW 2308</s2>
<s3>AUS</s3>
<sZ>1 aut.</sZ>
<sZ>2 aut.</sZ>
</inist:fA14><country>Australie</country>
</affiliation><author><name sortKey="Doroodchi, E" sort="Doroodchi, E" uniqKey="Doroodchi E" first="E." last="Doroodchi">E. Doroodchi</name>
<affiliation wicri:level="1"><inist:fA14 i1="01"><s1>School of Engineering, University of Newcastle</s1>
<s2>Callaghan, NSW 2308</s2>
<s3>AUS</s3>
<sZ>1 aut.</sZ>
<sZ>2 aut.</sZ>
</inist:fA14><country>Australie</country>
</affiliation><author><name sortKey="Lane, G L" sort="Lane, G L" uniqKey="Lane G" first="G. L." last="Lane">G. L. Lane</name>
<affiliation wicri:level="1"><inist:fA14 i1="02"><s1>CSIRO Minerals, Box 312</s1>
<s2>Clayton South, Vic 3169</s2>
<s3>AUS</s3>
<sZ>3 aut.</sZ>
<sZ>4 aut.</sZ>
<sZ>5 aut.</sZ>
</inist:fA14><country>Australie</country>
</affiliation><author><name sortKey="Koh, P T L" sort="Koh, P T L" uniqKey="Koh P" first="P. T. L." last="Koh">P. T. L. Koh</name>
<affiliation wicri:level="1"><inist:fA14 i1="02"><s1>CSIRO Minerals, Box 312</s1>
<s2>Clayton South, Vic 3169</s2>
<s3>AUS</s3>
<sZ>3 aut.</sZ>
<sZ>4 aut.</sZ>
<sZ>5 aut.</sZ>
</inist:fA14><country>Australie</country>
</affiliation><author><name sortKey="Schwarz, M P" sort="Schwarz, M P" uniqKey="Schwarz M" first="M. P." last="Schwarz">M. P. Schwarz</name>
<affiliation wicri:level="1"><inist:fA14 i1="02"><s1>CSIRO Minerals, Box 312</s1>
<s2>Clayton South, Vic 3169</s2>
<s3>AUS</s3>
<sZ>3 aut.</sZ>
<sZ>4 aut.</sZ>
<sZ>5 aut.</sZ>
</inist:fA14><country>Australie</country>
</affiliation><series><title level="j" type="main">Chemical engineering research & design</title>
<title level="j" type="abbreviated">Chem. eng. res. des.</title>
<idno type="ISSN">0263-8762</idno>
<imprint><date when="2008">2008</date>
</imprint><seriesStmt><title level="j" type="main">Chemical engineering research & design</title>
<title level="j" type="abbreviated">Chem. eng. res. des.</title>
<idno type="ISSN">0263-8762</idno>
</seriesStmt><profileDesc><textClass><keywords scheme="KwdEn" xml:lang="en"><term>Adhesion</term>
<term>Agitator</term>
<term>Bubble</term>
<term>Collision</term>
<term>Computational fluid dynamics</term>
<term>Correlation</term>
<term>Correlation analysis</term>
<term>Dispersion</term>
<term>Flotation</term>
<term>Foam</term>
<term>Gas holdup</term>
<term>Gas liquid flow</term>
<term>Hydrodynamics</term>
<term>Liquid phase</term>
<term>Loading</term>
<term>Mixing</term>
<term>Modeling</term>
<term>Particle size</term>
<term>Prediction</term>
<term>Stirred vessel</term>
<term>Turbulence</term>
<term>Two phase flow</term>
</keywords><keywords scheme="Pascal" xml:lang="fr"><term>Mélangeage</term>
<term>Dispersion</term>
<term>Flottation</term>
<term>Appareil agité</term>
<term>Bulle</term>
<term>Phase liquide</term>
<term>Agitateur</term>
<term>Collision</term>
<term>Turbulence</term>
<term>Corrélation</term>
<term>Analyse corrélation</term>
<term>Modélisation</term>
<term>Ecoulement gaz liquide</term>
<term>Ecoulement diphasique</term>
<term>Mécanique fluide numérique</term>
<term>Dimension particule</term>
<term>Retenue gaz</term>
<term>Hydrodynamique</term>
<term>Prédiction</term>
<term>Chargement</term>
<term>Adhérence</term>
<term>Mousse (émulsion)</term>
<term>Débit fluide</term>
</keywords><keywords scheme="Wicri" type="topic" xml:lang="fr"><term>Chargement</term>
</keywords><front><div type="abstract" xml:lang="en">Mineral flotation in mechanically agitated vessels (cells) involves complex interaction between bubbles, particles and the liquid phase. Ideally, just enough power input from the impeller is needed to so that the frequency of particle-bubble collision and attachment is maximised, while at the same time detachment events are minimised. This paper firstly investigated how the slip velocity of 2-10 mm diameter bubbles, a size commonly encountered in flotation devices, was influenced by turbulence intensity. The measurements confirmed the earlier correlation by [Lane, G.L., 2005, Numerical modelling of gas-liquid flow in stirred tanks, Ph.D. Thesis, University of Newcastle, Australia], which was then inputted into a computational fluid dynamic model to describe the gas dispersion in a mechanically agitated tank. The model provided turbulence intensity values that were then coupled with both slip velocity and critical Weber number models to generate both bubble size and gas holdup profiles for the entire vessel. Moreover, a simple equation was introduced to allow prediction of cavity formation behind the rotating impeller blades, which is a common occurrence in most flotation cells they normally operate at high gas loadings. This inclusion allowed the model to predict power reduction resulting from the presence of the cavities. Finally, extension of the computational model to include flotation hydrodynamics, such as probabilities of collision, adhesion and stabilisation of the particles at the bubble surface, is also described. The model is able to compute net attachment rates, and hence the particle flux entering the froth recovery phase, as a function of bubble and particle diameter, gas flowrate and power input.</div>
</front><inist><standard h6="B"><pA><fA01 i1="01" i2="1"><s0>0263-8762</s0>
</fA01><fA02 i1="01"><s0>CERDEE</s0>
</fA02><fA03 i2="1"><s0>Chem. eng. res. des.</s0>
</fA03><fA08 i1="01" i2="1" l="ENG"><s1>Mixing and gas dispersion in mineral flotation cells</s1>
</fA08><fA09 i1="01" i2="1" l="ENG"><s1>ISMIP-VI</s1>
</fA09><fA11 i1="01" i2="1"><s1>EVANS (G. M.)</s1>
</fA11><fA11 i1="02" i2="1"><s1>DOROODCHI (E.)</s1>
</fA11><fA11 i1="03" i2="1"><s1>LANE (G. L.)</s1>
</fA11><fA11 i1="04" i2="1"><s1>KOH (P. T. L.)</s1>
</fA11><fA11 i1="05" i2="1"><s1>SCHWARZ (M. P.)</s1>
</fA11><fA12 i1="01" i2="1"><s1>XUEREB (Catherine)</s1>
<s9>ed.</s9>
</fA12><fA12 i1="02" i2="1"><s1>TANGUY (Philippe)</s1>
<s9>ed.</s9>
</fA12><fA14 i1="01"><s1>School of Engineering, University of Newcastle</s1>
<s2>Callaghan, NSW 2308</s2>
<s3>AUS</s3>
<sZ>1 aut.</sZ>
<sZ>2 aut.</sZ>
</fA14><fA14 i1="02"><s1>CSIRO Minerals, Box 312</s1>
<s2>Clayton South, Vic 3169</s2>
<s3>AUS</s3>
<sZ>3 aut.</sZ>
<sZ>4 aut.</sZ>
<sZ>5 aut.</sZ>
</fA14><fA15 i1="01"><s1>Laboratoire de Génie Chimique</s1>
<s2>Toulouse</s2>
<s3>FRA</s3>
<sZ>1 aut.</sZ>
</fA15><fA15 i1="02"><s1>Ecole Polytechnique</s1>
<s2>Montreal</s2>
<s3>CAN</s3>
<sZ>2 aut.</sZ>
</fA15><fA18 i1="01" i2="1"><s1>Procter & Gamble</s1>
<s3>INC</s3>
<s9>org-cong.</s9>
</fA18><fA20><s1>1350-1362</s1>
</fA20><fA21><s1>2008</s1>
</fA21><fA23 i1="01"><s0>ENG</s0>
</fA23><fA43 i1="01"><s1>INIST</s1>
<s2>4284</s2>
<s5>354000185132680050</s5>
</fA43><fA44><s0>0000</s0>
<s1>© 2010 INIST-CNRS. All rights reserved.</s1>
</fA44><fA45><s0>1 p.3/4</s0>
</fA45><fA47 i1="01" i2="1"><s0>10-0514602</s0>
</fA47><fA60><s1>P</s1>
<s2>C</s2>
</fA60><fA64 i1="01" i2="1"><s0>Chemical engineering research & design</s0>
</fA64><fA66 i1="01"><s0>NLD</s0>
</fA66><fC01 i1="01" l="ENG"><s0>Mineral flotation in mechanically agitated vessels (cells) involves complex interaction between bubbles, particles and the liquid phase. Ideally, just enough power input from the impeller is needed to so that the frequency of particle-bubble collision and attachment is maximised, while at the same time detachment events are minimised. This paper firstly investigated how the slip velocity of 2-10 mm diameter bubbles, a size commonly encountered in flotation devices, was influenced by turbulence intensity. The measurements confirmed the earlier correlation by [Lane, G.L., 2005, Numerical modelling of gas-liquid flow in stirred tanks, Ph.D. Thesis, University of Newcastle, Australia], which was then inputted into a computational fluid dynamic model to describe the gas dispersion in a mechanically agitated tank. The model provided turbulence intensity values that were then coupled with both slip velocity and critical Weber number models to generate both bubble size and gas holdup profiles for the entire vessel. Moreover, a simple equation was introduced to allow prediction of cavity formation behind the rotating impeller blades, which is a common occurrence in most flotation cells they normally operate at high gas loadings. This inclusion allowed the model to predict power reduction resulting from the presence of the cavities. Finally, extension of the computational model to include flotation hydrodynamics, such as probabilities of collision, adhesion and stabilisation of the particles at the bubble surface, is also described. The model is able to compute net attachment rates, and hence the particle flux entering the froth recovery phase, as a function of bubble and particle diameter, gas flowrate and power input.</s0>
</fC01><fC02 i1="01" i2="X"><s0>001D07Q06</s0>
</fC02><fC02 i1="02" i2="X"><s0>001D07E</s0>
</fC02><fC02 i1="03" i2="X"><s0>001D07D</s0>
</fC02><fC03 i1="01" i2="X" l="FRE"><s0>Mélangeage</s0>
<s5>01</s5>
</fC03><fC03 i1="01" i2="X" l="ENG"><s0>Mixing</s0>
<s5>01</s5>
</fC03><fC03 i1="01" i2="X" l="SPA"><s0>Mezclado</s0>
<s5>01</s5>
</fC03><fC03 i1="02" i2="X" l="FRE"><s0>Dispersion</s0>
<s5>02</s5>
</fC03><fC03 i1="02" i2="X" l="ENG"><s0>Dispersion</s0>
<s5>02</s5>
</fC03><fC03 i1="02" i2="X" l="SPA"><s0>Dispersión</s0>
<s5>02</s5>
</fC03><fC03 i1="03" i2="X" l="FRE"><s0>Flottation</s0>
<s5>03</s5>
</fC03><fC03 i1="03" i2="X" l="ENG"><s0>Flotation</s0>
<s5>03</s5>
</fC03><fC03 i1="03" i2="X" l="SPA"><s0>Flotación</s0>
<s5>03</s5>
</fC03><fC03 i1="04" i2="X" l="FRE"><s0>Appareil agité</s0>
<s5>04</s5>
</fC03><fC03 i1="04" i2="X" l="ENG"><s0>Stirred vessel</s0>
<s5>04</s5>
</fC03><fC03 i1="04" i2="X" l="SPA"><s0>Aparato agitado</s0>
<s5>04</s5>
</fC03><fC03 i1="05" i2="X" l="FRE"><s0>Bulle</s0>
<s5>05</s5>
</fC03><fC03 i1="05" i2="X" l="ENG"><s0>Bubble</s0>
<s5>05</s5>
</fC03><fC03 i1="05" i2="X" l="SPA"><s0>Ampolla</s0>
<s5>05</s5>
</fC03><fC03 i1="06" i2="X" l="FRE"><s0>Phase liquide</s0>
<s5>06</s5>
</fC03><fC03 i1="06" i2="X" l="ENG"><s0>Liquid phase</s0>
<s5>06</s5>
</fC03><fC03 i1="06" i2="X" l="SPA"><s0>Fase líquida</s0>
<s5>06</s5>
</fC03><fC03 i1="07" i2="X" l="FRE"><s0>Agitateur</s0>
<s5>07</s5>
</fC03><fC03 i1="07" i2="X" l="ENG"><s0>Agitator</s0>
<s5>07</s5>
</fC03><fC03 i1="07" i2="X" l="SPA"><s0>Agitador</s0>
<s5>07</s5>
</fC03><fC03 i1="08" i2="X" l="FRE"><s0>Collision</s0>
<s5>08</s5>
</fC03><fC03 i1="08" i2="X" l="ENG"><s0>Collision</s0>
<s5>08</s5>
</fC03><fC03 i1="08" i2="X" l="SPA"><s0>Colisión</s0>
<s5>08</s5>
</fC03><fC03 i1="09" i2="X" l="FRE"><s0>Turbulence</s0>
<s5>09</s5>
</fC03><fC03 i1="09" i2="X" l="ENG"><s0>Turbulence</s0>
<s5>09</s5>
</fC03><fC03 i1="09" i2="X" l="SPA"><s0>Turbulencia</s0>
<s5>09</s5>
</fC03><fC03 i1="10" i2="X" l="FRE"><s0>Corrélation</s0>
<s5>10</s5>
</fC03><fC03 i1="10" i2="X" l="ENG"><s0>Correlation</s0>
<s5>10</s5>
</fC03><fC03 i1="10" i2="X" l="SPA"><s0>Correlación</s0>
<s5>10</s5>
</fC03><fC03 i1="11" i2="X" l="FRE"><s0>Analyse corrélation</s0>
<s5>11</s5>
</fC03><fC03 i1="11" i2="X" l="ENG"><s0>Correlation analysis</s0>
<s5>11</s5>
</fC03><fC03 i1="11" i2="X" l="SPA"><s0>Análisis correlación</s0>
<s5>11</s5>
</fC03><fC03 i1="12" i2="X" l="FRE"><s0>Modélisation</s0>
<s5>12</s5>
</fC03><fC03 i1="12" i2="X" l="ENG"><s0>Modeling</s0>
<s5>12</s5>
</fC03><fC03 i1="12" i2="X" l="SPA"><s0>Modelización</s0>
<s5>12</s5>
</fC03><fC03 i1="13" i2="X" l="FRE"><s0>Ecoulement gaz liquide</s0>
<s5>13</s5>
</fC03><fC03 i1="13" i2="X" l="ENG"><s0>Gas liquid flow</s0>
<s5>13</s5>
</fC03><fC03 i1="13" i2="X" l="SPA"><s0>Flujo gas líquido</s0>
<s5>13</s5>
</fC03><fC03 i1="14" i2="X" l="FRE"><s0>Ecoulement diphasique</s0>
<s5>14</s5>
</fC03><fC03 i1="14" i2="X" l="ENG"><s0>Two phase flow</s0>
<s5>14</s5>
</fC03><fC03 i1="14" i2="X" l="SPA"><s0>Flujo difásico</s0>
<s5>14</s5>
</fC03><fC03 i1="15" i2="X" l="FRE"><s0>Mécanique fluide numérique</s0>
<s5>15</s5>
</fC03><fC03 i1="15" i2="X" l="ENG"><s0>Computational fluid dynamics</s0>
<s5>15</s5>
</fC03><fC03 i1="15" i2="X" l="SPA"><s0>Mecánica fluido numérica</s0>
<s5>15</s5>
</fC03><fC03 i1="16" i2="X" l="FRE"><s0>Dimension particule</s0>
<s5>16</s5>
</fC03><fC03 i1="16" i2="X" l="ENG"><s0>Particle size</s0>
<s5>16</s5>
</fC03><fC03 i1="16" i2="X" l="SPA"><s0>Dimensión partícula</s0>
<s5>16</s5>
</fC03><fC03 i1="17" i2="X" l="FRE"><s0>Retenue gaz</s0>
<s5>17</s5>
</fC03><fC03 i1="17" i2="X" l="ENG"><s0>Gas holdup</s0>
<s5>17</s5>
</fC03><fC03 i1="17" i2="X" l="SPA"><s0>Detención gas</s0>
<s5>17</s5>
</fC03><fC03 i1="18" i2="X" l="FRE"><s0>Hydrodynamique</s0>
<s5>18</s5>
</fC03><fC03 i1="18" i2="X" l="ENG"><s0>Hydrodynamics</s0>
<s5>18</s5>
</fC03><fC03 i1="18" i2="X" l="SPA"><s0>Hidrodinámica</s0>
<s5>18</s5>
</fC03><fC03 i1="19" i2="X" l="FRE"><s0>Prédiction</s0>
<s5>19</s5>
</fC03><fC03 i1="19" i2="X" l="ENG"><s0>Prediction</s0>
<s5>19</s5>
</fC03><fC03 i1="19" i2="X" l="SPA"><s0>Predicción</s0>
<s5>19</s5>
</fC03><fC03 i1="20" i2="X" l="FRE"><s0>Chargement</s0>
<s5>20</s5>
</fC03><fC03 i1="20" i2="X" l="ENG"><s0>Loading</s0>
<s5>20</s5>
</fC03><fC03 i1="20" i2="X" l="SPA"><s0>Cargamento</s0>
<s5>20</s5>
</fC03><fC03 i1="21" i2="X" l="FRE"><s0>Adhérence</s0>
<s5>21</s5>
</fC03><fC03 i1="21" i2="X" l="ENG"><s0>Adhesion</s0>
<s5>21</s5>
</fC03><fC03 i1="21" i2="X" l="SPA"><s0>Adherencia</s0>
<s5>21</s5>
</fC03><fC03 i1="22" i2="X" l="FRE"><s0>Mousse (émulsion)</s0>
<s5>22</s5>
</fC03><fC03 i1="22" i2="X" l="ENG"><s0>Foam</s0>
<s5>22</s5>
</fC03><fC03 i1="22" i2="X" l="SPA"><s0>Espuma</s0>
<s5>22</s5>
</fC03><fC03 i1="23" i2="X" l="FRE"><s0>Débit fluide</s0>
<s4>INC</s4>
<s5>32</s5>
</fC03><fN21><s1>347</s1>
</fN21><fN44 i1="01"><s1>OTO</s1>
</fN44><fN82><s1>OTO</s1>
</fN82><pR><fA30 i1="01" i2="1" l="ENG"><s1>International Symposium on Mixing in Industrial Processes VI (ISMIP-6)</s1>
<s2>6</s2>
<s3>Niagara Falls CAN</s3>
<s4>2008-08-17</s4>
</fA30>
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