Mixing and gas dispersion in mineral flotation cells
Identifieur interne : 002253 ( PascalFrancis/Corpus ); précédent : 002252; suivant : 002254Mixing and gas dispersion in mineral flotation cells
Auteurs : G. M. Evans ; E. Doroodchi ; G. L. Lane ; P. T. L. Koh ; M. P. SchwarzSource :
- Chemical engineering research & design [ 0263-8762 ] ; 2008.
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.
English descriptors
- KwdEn :
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.
Notice en format standard (ISO 2709)
Pour connaître la documentation sur le format Inist Standard.
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Format Inist (serveur)
NO : | PASCAL 10-0514602 INIST |
---|---|
ET : | Mixing and gas dispersion in mineral flotation cells |
AU : | EVANS (G. M.); DOROODCHI (E.); LANE (G. L.); KOH (P. T. L.); SCHWARZ (M. P.); XUEREB (Catherine); TANGUY (Philippe) |
AF : | School of Engineering, University of Newcastle/Callaghan, NSW 2308/Australie (1 aut., 2 aut.); CSIRO Minerals, Box 312/Clayton South, Vic 3169/Australie (3 aut., 4 aut., 5 aut.); Laboratoire de Génie Chimique/Toulouse/France (1 aut.); Ecole Polytechnique/Montreal/Canada (2 aut.) |
DT : | Publication en série; Congrès; Niveau analytique |
SO : | Chemical engineering research & design; ISSN 0263-8762; Coden CERDEE; Pays-Bas; Da. 2008; Vol. 86; No. 12; Pp. 1350-1362; Bibl. 1 p.3/4 |
LA : | Anglais |
EA : | 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. |
CC : | 001D07Q06; 001D07E; 001D07D |
FD : | 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 |
ED : | Mixing; Dispersion; Flotation; Stirred vessel; Bubble; Liquid phase; Agitator; Collision; Turbulence; Correlation; Correlation analysis; Modeling; Gas liquid flow; Two phase flow; Computational fluid dynamics; Particle size; Gas holdup; Hydrodynamics; Prediction; Loading; Adhesion; Foam |
SD : | Mezclado; Dispersión; Flotación; Aparato agitado; Ampolla; Fase líquida; Agitador; Colisión; Turbulencia; Correlación; Análisis correlación; Modelización; Flujo gas líquido; Flujo difásico; Mecánica fluido numérica; Dimensión partícula; Detención gas; Hidrodinámica; Predicción; Cargamento; Adherencia; Espuma |
LO : | INIST-4284.354000185132680050 |
ID : | 10-0514602 |
Links to Exploration step
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<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>
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<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>
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<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>
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<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>
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<fC02 i1="03" i2="X"><s0>001D07D</s0>
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<s5>01</s5>
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<fC03 i1="01" i2="X" l="ENG"><s0>Mixing</s0>
<s5>01</s5>
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<fC03 i1="01" i2="X" l="SPA"><s0>Mezclado</s0>
<s5>01</s5>
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<fC03 i1="02" i2="X" l="FRE"><s0>Dispersion</s0>
<s5>02</s5>
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<s5>02</s5>
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<fC03 i1="02" i2="X" l="SPA"><s0>Dispersión</s0>
<s5>02</s5>
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<fC03 i1="03" i2="X" l="FRE"><s0>Flottation</s0>
<s5>03</s5>
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<fC03 i1="03" i2="X" l="ENG"><s0>Flotation</s0>
<s5>03</s5>
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<fC03 i1="03" i2="X" l="SPA"><s0>Flotación</s0>
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<fC03 i1="04" i2="X" l="FRE"><s0>Appareil agité</s0>
<s5>04</s5>
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<fC03 i1="04" i2="X" l="ENG"><s0>Stirred vessel</s0>
<s5>04</s5>
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<fC03 i1="04" i2="X" l="SPA"><s0>Aparato agitado</s0>
<s5>04</s5>
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<fC03 i1="05" i2="X" l="FRE"><s0>Bulle</s0>
<s5>05</s5>
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<fC03 i1="05" i2="X" l="SPA"><s0>Ampolla</s0>
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<fC03 i1="06" i2="X" l="FRE"><s0>Phase liquide</s0>
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<fC03 i1="06" i2="X" l="ENG"><s0>Liquid phase</s0>
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<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>
</pA>
<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>
</pR>
</standard>
<server><NO>PASCAL 10-0514602 INIST</NO>
<ET>Mixing and gas dispersion in mineral flotation cells</ET>
<AU>EVANS (G. M.); DOROODCHI (E.); LANE (G. L.); KOH (P. T. L.); SCHWARZ (M. P.); XUEREB (Catherine); TANGUY (Philippe)</AU>
<AF>School of Engineering, University of Newcastle/Callaghan, NSW 2308/Australie (1 aut., 2 aut.); CSIRO Minerals, Box 312/Clayton South, Vic 3169/Australie (3 aut., 4 aut., 5 aut.); Laboratoire de Génie Chimique/Toulouse/France (1 aut.); Ecole Polytechnique/Montreal/Canada (2 aut.)</AF>
<DT>Publication en série; Congrès; Niveau analytique</DT>
<SO>Chemical engineering research & design; ISSN 0263-8762; Coden CERDEE; Pays-Bas; Da. 2008; Vol. 86; No. 12; Pp. 1350-1362; Bibl. 1 p.3/4</SO>
<LA>Anglais</LA>
<EA>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.</EA>
<CC>001D07Q06; 001D07E; 001D07D</CC>
<FD>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</FD>
<ED>Mixing; Dispersion; Flotation; Stirred vessel; Bubble; Liquid phase; Agitator; Collision; Turbulence; Correlation; Correlation analysis; Modeling; Gas liquid flow; Two phase flow; Computational fluid dynamics; Particle size; Gas holdup; Hydrodynamics; Prediction; Loading; Adhesion; Foam</ED>
<SD>Mezclado; Dispersión; Flotación; Aparato agitado; Ampolla; Fase líquida; Agitador; Colisión; Turbulencia; Correlación; Análisis correlación; Modelización; Flujo gas líquido; Flujo difásico; Mecánica fluido numérica; Dimensión partícula; Detención gas; Hidrodinámica; Predicción; Cargamento; Adherencia; Espuma</SD>
<LO>INIST-4284.354000185132680050</LO>
<ID>10-0514602</ID>
</server>
</inist>
</record>
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