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Journal articles on the topic 'Particle size determination Fluidization'

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Published: 4 June 2021

Last updated: 12 February 2022

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1

Wang, X. S., V. Palero, J. Soria, and M. J. Rhodes. "Laser-based planar imaging of nano-particle fluidization: Part I—determination of aggregate size and shape." Chemical Engineering Science 61, no. 16 (August 2006): 5476–86. http://dx.doi.org/10.1016/j.ces.2006.04.012.

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2

Sun, Guanglin, and John R. Grace. "Effect of particle size distribution in different fluidization regimes." AIChE Journal 38, no. 5 (May 1992): 716–22. http://dx.doi.org/10.1002/aic.690380508.

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3

Chen, Heng Zhi, and Zheng Kui Guo. "Characteristics of Mixing/Segregation in a Bubbling/Slugging Fluidized Bed with Binary Mixtures." Advanced Materials Research 396-398 (November 2011): 322–25. http://dx.doi.org/10.4028/www.scientific.net/amr.396-398.322.

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Fluidization behavior of binary mixtures with titanic slag particles and carbon particles had been investigated. Three solids states in the bed: fixed bed, transient fluidization and steady fluidization, emerges as increasing gas velocity. The extent of segregation of solids mixture in transient fluidization regime depended on the size difference between jetsam particles and flotsam particles. The effects of flotsam particle size, initial jetsam concentration and the superficial gas velocity on the segregation of binary solids had been measured.

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4

Sahoo, Pranati, and Abanti Sahoo. "Fluidization and Spouting of Fine Particles: A Comparison." Advances in Materials Science and Engineering 2013 (2013): 1–7. http://dx.doi.org/10.1155/2013/369380.

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The fluidization characteristics of fine particles have been studied in both the fluidized bed and spouted bed. The effect of different system parameters (viz. static bed height, particle size, particle density and superficial velocity of the fluidizing medium, rotational speed of stirrer, and spout diameter) on the fluidization characteristics such as bed expansion/fluctuation ratios, bed pressure drop, minimum fluidizing/spouting velocity, and fluidization index of fine particles (around 60 micron particle size) have been analyzed. A stirrer/rod promoter has been used in the bed to improve the bed fluidity for fluidization process and spout diameter has been varied for spouted bed. Mathematical expressions for these bed dynamics have been developed on the basis of dimensionless analysis. Finally calculated values of these bed dynamics are compared with the experimentally observed values thereby indicating the successful applications of these developed correlations over a wide range of parameters.

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5

Fang, Sheng, Yanding Wei, Lei Fu, Geng Tian, and Haibin Qu. "Modeling of the Minimum Fluidization Velocity and the Incipient Fluidization Pressure Drop in a Conical Fluidized Bed with Negative Pressure." Applied Sciences 10, no. 24 (December 8, 2020): 8764. http://dx.doi.org/10.3390/app10248764.

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The modeling of the minimum fluidization velocity (U0mf) and the incipient fluidization pressure drop (ΔPmf) is a valuable research topic in the fluidization field. In this paper, first, a series of experiments are carried out by changing the particle size and material mass to explore their effects on U0mf and ΔPmf. Then, an Ergun equation modifying method and the dimensional analysis method are used to obtain the modeling correlations of U0mf and ΔPmf by fitting the experimental data, and the advantages and disadvantages of the two methods are discussed. The experimental results show that U0mf increases significantly with increasing particle size but has little relationship with the material mass; ΔPmf increases significantly with increasing material mass but has little relationship with the particle size. Experiments with small particles show a significant increase at large superficial gas velocity; we propose a conjecture that the particles’ collision with the fluidization chamber’s top surface causes this phenomenon. The fitting accuracy of the modified Ergun equation is lower than that of the dimensionless model. When using the Ergun equation modifying method, it is deduced that the gas drag force is approximately 0.8995 times the material total weight at the incipient fluidized state.

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6

Korkerd, Krittin, Chaiwat Soanuch, Pornpote Piumsomboon, and Benjapon Chalermsinsuwan. "Effect of Particle Size Distributions on Minimum Fluidization Velocity with Varying Gas Temperature." International Journal of Environmental Science and Development 11, no. 11 (2020): 524–29. http://dx.doi.org/10.18178/ijesd.2020.11.11.1302.

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The particle size distribution (PSD) is an important property that can influence the hydrodynamics and chemical conversion in fluidized bed system. The objective of this study is to investigate the effect of PSDs of particle and gas temperature on minimum fluidization velocity (Umf). Here, the silica sand with three average diameters and five PSDs including narrow cut, Gaussian, Gaussian with high standard deviation, negative skewed distribution and positive skewed distribution were used. The considered gas temperature ranged from 30 to 120 °C. The results showed that the Umf values with wide PSDs were lower than the Umf values for narrow cut particle with the same average diameter. The reason can be explained by the addition of smaller particle will improve the fluidization characteristics. The standard deviation and skewness of PSD also influenced on the Umf. The Umf was observed to decrease with increasing gas temperature. In addition, the effect of average particle diameter could also be seen. The Umf increased with the increasing of average particle diameter.

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7

Wu, Zhenqun, Hui Jin, Guobiao Ou, Liejin Guo, and Changqing Cao. "Three-dimensional numerical study on flow dynamics characteristics in supercritical water fluidized bed with consideration of real particle size distribution by computational particle fluid dynamics method." Advances in Mechanical Engineering 10, no. 6 (June 2018): 168781401877987. http://dx.doi.org/10.1177/1687814018779871.

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Supercritical water fluidized bed is a promising reactor which can realize the efficient and clean gasification of coal to produce hydrogen. As the high pressure and temperature inside supercritical water fluidized bed, the study of the detail flow behaviors needs the help of numerical method. Considering the limitation of the two-fluid method and discrete element method, the computational particle fluid dynamics method was applied to this work. When particle size distribution was taken into consideration, the simulated results showed that the transformation from fixed bed regime to fluidized bed regime is a gradual process. With the increase in superficial fluid velocity, particles in small diameter migrate to the top of the bed and there exits layering phenomenon in the bed. Besides, though the particles are categorized as Geldart B group, the minimum fluidization velocity is not equal to the minimum bubbling fluidization velocity and there is a complicated bed expansion process after incipient fluidization. The bed expansion process is also influenced by the particle size distribution.

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8

Ali, Syed, Avijit Basu, Sulaiman Alfadul, and Mohammad Asif. "Nanopowder Fluidization Using the Combined Assisted Fluidization Techniques of Particle Mixing and Flow Pulsation." Applied Sciences 9, no. 3 (February 9, 2019): 572. http://dx.doi.org/10.3390/app9030572.

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In the present study, we report the fluidization behavior of ultrafine nanopowder using the assisted fluidization technique of particle mixing, which was further superimposed with the pulsation of the inlet gas flow to the fluidized bed. The powder selected in the present study was hydrophilic nanosilica, which shows strong agglomeration behavior leading to poor fluidization hydrodynamics. For particle mixing, small proportions of inert particles of Geldart group A classification were used. The inlet gas flow to the fluidized bed was pulsed with a square wave of frequency 0.1 Hz with the help of a solenoid valve controlled using the data acquisition system (DAQ). In addition to the gas flow rate to the fluidized bed, pressure transients were carefully monitored using sensitive pressure transducers connected to the DAQ. Our results indicate a substantial reduction in the effective agglomerate size as a result of the simultaneous implementation of the assisted fluidization techniques of particle mixing and flow pulsation.

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9

Khoe, G. K., T. L. Ip, and J. R. Grace. "Rheological and fluidization behaviour of powders of different particle size distribution." Powder Technology 66, no. 2 (May 1991): 127–41. http://dx.doi.org/10.1016/0032-5910(91)80094-y.

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10

Arima, Kenichi, Isao Torii, Ryuhei Takashima, Tetsuya Sawatsubashi, Masaaki Kinoshita, Koji Oura, and Hiromi Ishii. "Fluidization of Wet Brown Coal Particles with Wide Particle Size Distribution." Journal of Chemical Engineering of Japan 48, no. 3 (2015): 190–96. http://dx.doi.org/10.1252/jcej.14we166.

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11

Rousset, P., K. Fernandes, A. Vale, L. Macedo, and A. Benoist. "Change in particle size distribution of Torrefied biomass during cold fluidization." Energy 51 (March 2013): 71–77. http://dx.doi.org/10.1016/j.energy.2013.01.030.

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12

Han, Li Ning, and Lu Min Wang. "CFD Simulation Research on Flow Characteristics of Fluidized Beds." Advanced Materials Research 881-883 (January 2014): 1809–13. http://dx.doi.org/10.4028/www.scientific.net/amr.881-883.1809.

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The Euler-Euler two-fluid model incorporating the kinetic theory of granular flow was applied to simulate the gas-solid flow in fluidized beds. The pressure drop, particle distribution and motion characteristics were studied in this paper. In order to investigate the effect of structure of the fluidized bed on flow characteristics, fluidized beds with different diameters and structures were applied. User defined functions (UDF) were applied to study the flow characteristics when the particle size and mass changed over time. The results showed that with the increase of particle size, higher minimum fluidization velocity was required, but lower pressure drop was obtained. For a certain fluidizing medium, the bed critical fluidization velocity depended only on the size and nature of the particles. The structure of a fluidized bed had an influence on the particle distribution and motion characteristics.

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13

Hartman, Miloslav, Zdeněk Beran, Karel Svoboda, and Václav Veselý. "Operation Regimes of Fluidized Beds." Collection of Czechoslovak Chemical Communications 60, no. 1 (1995): 1–33. http://dx.doi.org/10.1135/cccc19950001.

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The state of the art has been reviewed in the analysis and description of flow or contacting pattern in gas-solid contacting units where a gas flows upwards through a bed of solids. The flow regime or contacting mode varies widely, depending on the particle size, particle density, gas density, gas viscosity, gas velocity and column geometry. The influence of such variables is reflected in the particle classification schemes and regime diagrams to cover the operation regions of common gas-solid reactors and contactors. In general, fluidized beds can be operated in six different regimes: particulate (homogeneous) fluidization, bubbling fluidization, slugging fluidization, turbulent fluidization, fast fluidization and pneumatic conveying. The bubbling beds can be further classified into three different modes of contacting: fast bubble regime, slow bubble regime and rapidly growing bubble regime. Characteristic features of all the regimes as well as the transitions between them are discussed. Current research interests, supported by practical needs, are oriented toward the operation conditions and contactor geometry of high velocity units.

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14

Hartman, Miloslav, and Robert W. Coughlin. "On the Incipient Fluidized State of Solid Particles." Collection of Czechoslovak Chemical Communications 58, no. 6 (1993): 1213–41. http://dx.doi.org/10.1135/cccc19931213.

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A comprehensive study has been reported on all aspects of the transition of packed bed to the state of incipient fluidization (point of minimum fluidization, onset of fluidization): particle size and shape, size distribution in a batch of particles, fixed bed voidage, pressure drop through a packed bed and oneset of fluidization. A number of predictive equations have been compared that were proposed to estimate the minimum fluidization velocity. All the equations tested do not have any flow limitations and are applicable to laminar, transitional as well as to turbulent flow regime. While some equations have some foundation in theory, the other are more or less generalized correlations of experimental data amassed by different authors under various conditions. The influence of temperature and pressure on the minimum fluidization velocity has been explored with respect to the important applications such as combustion and gasification. Problems have also been discussed with transition from fixed to fluidized bed of binary and polydisperse systems.

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15

Vasconcelos, David da Silva, Sirlene Barbosa Lima, Ana Cristina Morais da Silva, José Mário Ferreira Júnior, and Carlos Augusto de Moraes Pires. "Evaluation of an empirical model used for deriving the fluidization velocity of binary mixtures of biomasses and sand." Research, Society and Development 9, no. 9 (August 11, 2020): e49996648. http://dx.doi.org/10.33448/rsd-v9i9.6648.

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In a previous study, a statistical model was developed using the experimental planning technique for evaluating the influence of its variables on fluidization velocity. In this study, we investigated the Vasconcelos-statistical model (VSM) in data representation, considering fluidization with and without segregation. The methodology used was based on the simulation of the fluidization velocity of nine binary systems, comprising sand, and eight biomasses published by six authors. In addition, the results obtained using VSM were compared with those obtained using five other models, reported by different authors, but adjusted to the experimental data of these biomasses. The result obtained by the proposed models mainly indicated a discrepancy between the experimental and calculated fluidization velocities. VSM, using only three variables (particle size, particle diameter, and biomass mass fraction), yielded results of smaller discrepancy values in all simulations (2.23–12.51%), as opposed to the other comparative models, which presented more significant numbers of variables. Thus, VSM is defined as one of the most interesting models for predicting the fluidization velocity of several biomasses.

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16

Vaidya, Tanuja. "Fluidization Behavior of Alumina Nano-Particles." Applied Mechanics and Materials 110-116 (October 2011): 1833–40. http://dx.doi.org/10.4028/www.scientific.net/amm.110-116.1833.

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The experimental study is conducted to determine the fluidization behavior and heat transfer variations across the bed in the bubbling fluidized bed having very fine particles. The powder is analyzed using scanning electron microscope (SEM) and Mastersizer analyzer. The bubbling fluidized bed set-up was designed, developed and installed for the hydrodynamic and heat transfer studies. From the experiments, it is found that the alumina powder with particle size range of 200nm to 10μm has agglomerate bubbling fluidized bed (ABF).

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17

Arima, Kenichi, Isao Torii, Ryuhei Takashima, Tetsuya Sawatsubashi, Masaaki Kinoshita, Koji Oura, and Hiromi Ishii. "Effect of Moisture Content on Fluidization of Wet Brown Coal Particle with Wide Particle Size Distribution." KAGAKU KOGAKU RONBUNSHU 40, no. 4 (2014): 299–305. http://dx.doi.org/10.1252/kakoronbunshu.40.299.

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18

Lin, Chiou-Liang, Ming-Yen Wey, and Shr-Da You. "The effect of particle size distribution on minimum fluidization velocity at high temperature." Powder Technology 126, no. 3 (August 2002): 297–301. http://dx.doi.org/10.1016/s0032-5910(02)00074-8.

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19

Guardiola, Jesús, Victor Rojo, and Guadalupe Ramos. "Influence of particle size, fluidization velocity and relative humidity on fluidized bed electrostatics." Journal of Electrostatics 37, no. 1-2 (May 1996): 1–20. http://dx.doi.org/10.1016/0304-3886(96)00002-2.

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20

Ramakrishna, V., and S. R. Rao. "Particle size determination and hindered settling." Journal of Applied Chemistry 15, no. 10 (May 4, 2007): 473–79. http://dx.doi.org/10.1002/jctb.5010151007.

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21

Hubbard, Arthur. "Powder Sampling and Particle Size Determination." Journal of Colloid and Interface Science 277, no. 2 (September 2004): 505. http://dx.doi.org/10.1016/j.jcis.2004.05.019.

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22

Liu, Xuemin, Hairui Yang, and Junfu Lyu. "Optimization of Fluidization State of a Circulating Fluidized Bed Boiler for Economical Operation." Energies 13, no. 2 (January 13, 2020): 376. http://dx.doi.org/10.3390/en13020376.

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To reduce the auxiliary power consumption and improve the reliability of large-scale circulating fluidized bed (CFB) boilers, we developed energy-saving CFB combustion technology based on the fluidization state re-specification. A calculation model of coal comminution energy consumption was used to analyze the change in comminution energy consumption, and a 1D CFB combustion model was modified to predict the operation parameters under the fluidization state optimization conditions. With a CFB boiler of 480 t/h, the effect of fluidization state optimization on the economical operation was analyzed using the above two models. We found that combustion efficiency presents a nonmonotonic trend with the change in the bed pressure drop and feeding coal size. There are an optimal bed pressure drop and a corresponding feeding coal size distribution, under which the net coal consumption is the lowest. Low bed pressure drop operation achieved by reducing the coal particle size is not beneficial to SO2 and NOx emission control, and the pollutant control cost increases. The effect of fluidization state optimization on the gross cost of power supply can be calculated, and the optimal bed pressure drop can be obtained.

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23

Kamranian Marnani, Abbas, Andreas Bück, Sergiy Antonyuk, Berend van Wachem, Dominique Thévenin, and Jürgen Tomas. "The Effect of the Presence of Very Cohesive Geldart C Ultra-Fine Particles on the Fluidization of Geldart A Fine Particle Beds." Processes 7, no. 1 (January 11, 2019): 35. http://dx.doi.org/10.3390/pr7010035.

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The effect of the presence of ultra-fines (d < 10 μm) on the fluidization of a bed containing fine particles (d < 100 μm), is the subject of this paper. Practically, it can happen due to breakage or surface abrasion of the fine particles in some processes which totally changes the size distribution and also fluidization behaviour. The materials used in this study are both ground calcium carbonate (GCC); fine is CALCIT MVT 100 (Geldart’s group A) and ultra-fine is CALCIT MX 10 (group C). The experimental results for different binary mixtures of these materials (ultra-fines have 30%, 50%, or 68% of the total mixture weight) show that the physical properties of the mixtures are close to those of pure ultra-fine powders. Using mean values of the bed pressure drop calculated from several independent repetitions, the fluidization behaviour of different mixtures are compared and discussed. The fluidization behaviour of the mixtures is non-reproducible and includes cracking, channelling and agglomeration (like for pure ultra-fine powders). Increasing the portion of ultra-fine materials in the mixture causes a delay in starting partial fluidization, an increase in the bed pressure drop as well as a delay in reaching the peak point.

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24

Campbell, Charles S., and David G. Wang. "Particle pressures in gas-fluidized beds." Journal of Fluid Mechanics 227 (June 1991): 495–508. http://dx.doi.org/10.1017/s0022112091000216.

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The particle pressure is the surface force that is exerted due to the motion of particles and their interactions. This paper describes measurements of the particle pressure exerted on the sidewall of a gas-fluidized bed. As long as the bed remains in a packed state, the particle pressure decreases with increasing gas velocity as progressively more of the bed is supported by fluid forces. It appropriately reaches a minimum fluidization and then begins to rise again when the bed is fluidized, reflecting the agitation of the bed by bubbles. In this fully fluidized region, the particle pressure scales with the particle density and the bubble size.

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25

Branco Jr, A. M. C., A. L. A. Mesquita, and J. R. P. Vaz. "APPLICATION OF THE LINEAR SPRING-DASHPOT MODEL IN THE CFD-DEM SIMULATION OF ALUMINA FLUIDIZATION." Revista de Engenharia Térmica 14, no. 2 (December 31, 2015): 95. http://dx.doi.org/10.5380/reterm.v14i2.62141.

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The coupling of the Computational Fluid Dynamics (CFD) to the Discrete Element Method (DEM) to simulate fluidization is computationally demanding. Although the Linear Spring-Dahspot (LSD) model can help to reduce the CFD-DEM simulation runtime due to its simplicity, its applicability is not reasonable for all sorts of problems. The objective of the present work is to show the application of the LSD model to the CFD-DEM simulation of alumina fluidization. The simulations were carried out with the software ANSYS FLUENT 14.5 and divided into two parts: (1) the reproduction with ANSYS FLUENT of simulations from the literature in which the LSD model and a representative particle approach were used. (2) the simulation of alumina fluidization and validation with experimental data. The results of three main sets of parameters were analysed to include different DEM and CFD time steps, drag models, the representation of particles with both uniform size and particle size distribution, etc. The main conclusion of this work is that the LSD model and the CFD-DEM approach can be used to model the actual behaviour of alumina fluidized beds, but the high simulation runtime and the correct setting of the strategies used to control it are still limiting factors which deserve special attention.

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26

Egorov, Ivan N., Svetlana I. Egorova, and Viktor P. Kryzhanovsky. "Particle Size Distribution and Structural State Analysis of Mechanically Milled Strontium Hexaferrite." Materials Science Forum 946 (February 2019): 293–97. http://dx.doi.org/10.4028/www.scientific.net/msf.946.293.

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Article presents an experimental study result of milling coarse strontium hexaferrite in beater mill with formation of magneto fluidized bed and without it. Magneto fluidized bed is formed by mutually perpendicular constant and alternating gradient magnetic fields. We studied the dynamics of particle size distribution from milling time and parameters of magnetic fields. Microstructure dynamics of strontium hexaferrite powder particles milled in various regimes was studied by X-ray diffraction methods. Milling efficiency and energy efficiency of milling process were studied in conditions with and without powder fluidization by magnetic fields. Analysis of experimental data showed advantages of milling in magneto fluidized bed in increased efficiency, particle size distribution homogeneity and powder chemical activity because of lattice micro-stresses.

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27

Islam, Md Tariqul, and Anh V. Nguyen. "Effect of particle size and shape on liquid–solid fluidization in a HydroFloat cell." Powder Technology 379 (February 2021): 560–75. http://dx.doi.org/10.1016/j.powtec.2020.10.080.

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28

Johari, Anwar, Tuan Amran Tuan Abdullah, Mimi Haryani Hassim, Kamarizan Kidam, Mohd Johari Kamaruddin, Zaki Yamani Zakaria, and Wan Rosli Wan Sulaiman. "Effect of Fluidization Number on the Combustion of Empty Fruit Bunch in a Fluidized Bed." Advanced Materials Research 1125 (October 2015): 301–5. http://dx.doi.org/10.4028/www.scientific.net/amr.1125.301.

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The effect of fluidization number on the sustainability of fluidized bed combustion of empty fruit bunch was investigated. Proximate and ultimate analyses were conducted to determine the physical and chemical properties of empty fruit bunch. Sand mean particle size was determined at 0.34 mm and the sand bed height was set at 1 Dcwhich is equivalent to the diameter of the reactor. Combustion study was carried out in a circular reactor of 0.21 m diameter and operated at stoichiometric condition (Air Factor = 1). The range of fluidization numbers under investigation was from 3 to 8 Umf. The fluidized bed operated in a bubbling mode at operating temperature at about 700°C. Results showed that the most optimum fluidization number was 5 Umfbeing the most optimum with respect to the sustainability of the bed temperature.

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29

Langton, Maud, and Anne-Marie Hermansson. "Image analysis determination of particle size distribution." Food Hydrocolloids 7, no. 1 (March 1993): 11–22. http://dx.doi.org/10.1016/s0268-005x(09)80021-0.

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30

ATHERTON, E., and D. TOUGH. "Particle-size Determination with the Disc Centrifuge." Journal of the Society of Dyers and Colourists 81, no. 12 (October 22, 2008): 624–31. http://dx.doi.org/10.1111/j.1478-4408.1965.tb02639.x.

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31

Dulog, L., and T. Schauer. "Field flow fractionation for particle size determination." Progress in Organic Coatings 28, no. 1 (May 1996): 25–31. http://dx.doi.org/10.1016/0300-9440(95)00584-6.

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32

Bommireddi, A., L. C. Li, D. Stephens, D. Robinson, and E. Ginsburg. "Particle Size Determination of a Flocculated Suspension Using a Light-Scattering Particle Size Analyzer." Drug Development and Industrial Pharmacy 24, no. 11 (January 1998): 1089–93. http://dx.doi.org/10.3109/03639049809089954.

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33

Tian, Y., and P. Mehrani. "Effect of particle size in fluidization of polyethylene particle mixtures on the extent of bed electrification and wall coating." Journal of Electrostatics 76 (August 2015): 138–44. http://dx.doi.org/10.1016/j.elstat.2015.05.020.

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34

van Ommen, J. Ruud, Jaap C. Schouten, and Cor M. van den Bleek. "Monitoring Fluidization Dynamics for Detection of Changes in Fluidized Bed Composition and Operating Conditions." Journal of Fluids Engineering 121, no. 4 (December 1, 1999): 887–94. http://dx.doi.org/10.1115/1.2823551.

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In many industrial applications of gas-solids fluidized beds, it is worthwhile to have an on-line monitoring method for detecting changes in the hydrodynamics of the bed (due for example to agglomeration) quickly. In this paper, such a method, based on the short-term predictability of fluidized bed pressure fluctuations, is examined. Its sensitivity is shown by experiments with small step changes in the superficial gas velocity and by experiments with a gradual change in the particle size distribution of the solids in the bed. Furthermore, it is demonstrated that the method is well able to indicate if a stationary hydrodynamic state has been reached after a change in the particle size distribution (a ‘grade change’).

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35

Feng, Rongtao, Junguo Li, Zhonghu Cheng, Xin Yang, and Yitian Fang. "Influence of particle size distribution on minimum fluidization velocity and bed expansion at elevated pressure." Powder Technology 320 (October 2017): 27–36. http://dx.doi.org/10.1016/j.powtec.2017.07.024.

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36

Rao, Akhil, Jennifer S. Curtis, Bruno C. Hancock, and Carl Wassgren. "Classifying the fluidization and segregation behavior of binary mixtures using particle size and density ratios." AIChE Journal 57, no. 6 (July 26, 2010): 1446–58. http://dx.doi.org/10.1002/aic.12371.

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37

Mohideen, Mohd Faizal, Suzairin Md Seri, and Vijay Raj Raghavan. "Fluidization of Geldart Type-D Particles in a Swirling Fluidized Bed." Applied Mechanics and Materials 110-116 (October 2011): 3720–27. http://dx.doi.org/10.4028/www.scientific.net/amm.110-116.3720.

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Geldart Type-D particles are often associated with poor fluidization characteristics due to their large sizes and higher densities. This paper reports the hydrodynamics of various Geldart Type-D particles when fluidized in a swirling fluidized bed (SFB). Four different sizes of particles ranging from 3.85 mm to 9.84 mm with respective densities ranging from 840 kg/m3 to 1200 kg/m3 were used as bed material to study the effect of various bed weights (500 gram to 2000 gram) and centre bodies (cone and cylinder) for superficial velocities up to 6 m/s. The performance of the SFB was assessed in terms of pressure drop values, minimum fluidization velocity, Umf and fluidization quality by physical observation on regimes of operation. The swirling fluidized bed showed excellent capability in fluidizing Geldart Type-D particles in contrast to the conventional fluidized beds. The bed pressure drop of increased with superficial velocity after minimum fluidization as a result of increasing centrifugal bed weight. It was also found that the particle size and centre body strongly influence the bed hydrodynamics.

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38

Xu, Qiyan, Zhanghan Gu, Ziwei Wan, Baoguo Wu, and Qian Xie. "Influence of the Application of a Sound Field on the Flow State Reduction of Newman Fine Iron Ore." Processes 9, no. 4 (April 20, 2021): 725. http://dx.doi.org/10.3390/pr9040725.

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To improve the fluidization of the fluidized bed in ironmaking, the particle loss and bonding during the fluidized bed are largely removed by changing the properties of the particle surface or by adding an external field. Currently, the vibration, magnetic, sound, and electric fields have been commonly applied to provide external energy to the fluidization bed systems. In this work, experiments are conducted for Newman ore particles under the application of an external sound field at a reduction temperature of 1023 K, linear velocity of 0.6 m/s, duration of 60 min, pressure of 0.2 MPa, and typical mineral powder particle size of 80–100 mesh, with H2 used as the reducing gas. The power and frequency of the ultrasonic field are varied, and the effects of sound field are evaluated by the comparative analysis of the effects of the sound field with different powers of sound fields and application times on the metallization rate and binder ratio of the samples. The acoustic pressure and frequency were varied to determine the critical speed and influence on the bed and to study the interactions of the iron ore powder particles in the sound field and the bonding mechanism of the particles. The results of this paper reproduce the actual particle fluidization process and analysis of the interactions of the particles in the sound field well. The influence of the external sound field on the gas-solid flow was studied from the perspective of macroscopic motion and force analysis.

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Rosli, Masli, Abdul Abdul Nasir, Mohd Takriff, and Lee Chern. "Simulation of a Fluidized Bed Dryer for the Drying of Sago Waste." Energies 11, no. 9 (September 10, 2018): 2383. http://dx.doi.org/10.3390/en11092383.

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The large amount of sago waste produced by sago processing industries can cause serious environmental problems. When dried, these residues usually have a high starch content (around 58%) and have many potential applications. In this study, the drying of sago waste using a fluidized bed dryer (FBD), which offers more advantages than other drying methods, is analyzed via computational fluid dynamics (CFD) modeling. A two-dimensional (2D) FBD model is also developed and a mesh independency test is conducted immediately afterwards. A fine mesh is selected for the CFD model and a simulation is conducted using ANSYS Fluent 17.1 software (Ansys Inc., version 17.1, Canonsburg, PA, USA). The governing and discretized algebraic equations are solved by applying the phase-coupled semi-implicit method for pressure-linked equations. Both the Eulerian–Eulerian multiphase model approach and the turbulence model are applied in the simulation due to the turbulent flow in the dryer. A velocity of 1.30 m/s and temperature of 50 °C are selected as boundary conditions based on the optimum parameter values from previous experiments. The final moisture content that we aim to achieve is 10% or a moisture ratio of 0.25 in sago waste for the purpose of animal feed, so as to prevent bacterial growth and for packaging purposes based on common industrial practice. Both the drying rate and fluidization profile are examined at air velocities of 0.6, 1.0, 1.3, 1.8, and 2.2 m/s. Based on the results, the velocity range of 1.0 m/s to 2.2 m/s is deemed suitable for the fluidization and drying of sago waste with a particle size of 2000 μm for a drying simulation of 1 h. The drying rate is further examined at air temperatures of 50 °C, 60 °C, 70 °C, and 80 °C, whereas the fluidization profile is examined at particle sizes of 200, 500, 1000, and 2000 μm. The results reveal excellent fluidization at a particle size range of 500 μm to 2000 μm and a velocity of 1.3 m/s.

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Xu, Qiyan, Zhiping Li, and Zhanghan Gu. "Experimental Investigation of the Fluidization Reduction Characteristics of Iron Particles Coated with Carbon Powder under Pressurized Conditions." Molecules 25, no. 8 (April 15, 2020): 1810. http://dx.doi.org/10.3390/molecules25081810.

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The purpose of this study was to comprehensively analyze the effects of the carbon powder coating mass fraction, pressure, reduction temperature, reduction time, gas linear velocity, and particle size on fluidization reduction. Brazilian fine iron ore particles were the experimental object, and reduction experiments were performed under added carbon powder coating and pressure conditions. A six-factor, three-level orthogonal experiment method was used to obtain the optimal operating conditions and investigate the adhesion and inhibition mechanisms of fine iron ore during reduction. The experimental results show that with the addition of a carbon powder coating, an appropriate increase in pressure can increase the metallization rate, improve the fluidization state, and reduce the sticking ratio. The optimal operating conditions for pure hydrogen to reduce Brazilian fine iron ore was found to be a reduction temperature of 923–1023 K, the linear velocity of the reducing gas was 0.6 m/s, the reducing time was 30–50 min, the reducing pressure was 0.25 MPa, the mass content of the coated carbon powder was 2–6% (accounting for the mass of the mineral powder), and the particle size of the carbon powder was 4–7 µm. Iron whiskers cohesion and agglomeration were the main reasons for the adhesion of ore powder particles. It was found that carbon powder coating can effectively change the morphology of metal iron, as metal iron generates spherical particles around the carbon powder to improve the fluidization state.

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Sha, Jie, Guang Yuan Xie, Yao Li Peng, and Ben Xuan Shi. "Hydrodynamics of Coarse Coal Slime and Quartz Particles in a Liquid-Solid Fluidized Bed Separator." Advanced Materials Research 279 (July 2011): 350–55. http://dx.doi.org/10.4028/www.scientific.net/amr.279.350.

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The hydrodynamics of particles of coarse coal slime and quartz of different sizes in a liquid-solid fluidized bed separator were investigated experimentally, including minimum fluidization velocities, bed expansion ratios, and segregation of mixed particles with two methods. Experimental parameters studied included density and size of particle, superficial water velocity and initial static bed height. The results provide a reference for choice of size scope on coarse coal slime separation by liquid-solid fluidized bed separators.

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Peng, Jian, Wei Sun, Haisheng Han, and Le Xie. "CFD Modeling and Simulation of the Hydrodynamics Characteristics of Coarse Coal Particles in a 3D Liquid-Solid Fluidized Bed." Minerals 11, no. 6 (May 27, 2021): 569. http://dx.doi.org/10.3390/min11060569.

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In this study, a Eulerian-Eulerian liquid-solid two-phase flow model combined with kinetic theory of granular flow was established to study the hydrodynamic characteristics and fluidization behaviors of coarse coal particles in a 3D liquid-solid fluidized bed. First, grid independence analysis was conducted to select the appropriate grid model parameters. Then, the developed computational fluid dynamics (CFD) model was validated by comparing the experimental data and simulation results in terms of the expansion degree of low-density fine particles and high-density coarse particles at different superficial liquid velocities. The simulation results agreed well with the experimental data, thus validating the proposed CFD mathematical model. The effects of particle size and particle density on the homogeneous or heterogeneous fluidization behaviors were investigated. The simulation results indicate that low-density fine particles are easily fluidized, exhibiting a certain range of homogeneous expansion behaviors. For the large and heavy particles, inhomogeneity may occur throughout the bed, including water voids and velocity fluctuations.

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Kofman, C. D., J. E. Balinotti, and A. M. Teper. "Particle size determination of a generic nebulized tobramycin." Journal of Cystic Fibrosis 9 (June 2010): S62. http://dx.doi.org/10.1016/s1569-1993(10)60242-1.

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Kupfer, Michael, Klaus Gast, Dietrich Zirwer, and Hasso Meinert. "Determination of particle size distribution in perfluorocarbon emulsions." Journal of Fluorine Chemistry 29, no. 1-2 (August 1985): 233. http://dx.doi.org/10.1016/s0022-1139(00)83475-2.

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Folly, Walter S. D., and Ronaldo S. de Biasi. "Determination of particle size distribution by FMR measurements." Brazilian Journal of Physics 31, no. 3 (September 2001): 398–401. http://dx.doi.org/10.1590/s0103-97332001000300009.

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Westesen, K., and T. Wehler. "Particle size determination of a submicron-sized emulsion." Colloids and Surfaces A: Physicochemical and Engineering Aspects 78 (October 1993): 125–32. http://dx.doi.org/10.1016/0927-7757(93)80318-9.

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Hietala, S. L., and D. M. Smith. "Porosity effects on particle size determination via sedimentation." Powder Technology 59, no. 2 (October 1989): 141–44. http://dx.doi.org/10.1016/0032-5910(89)80038-5.

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Nam, Sang Sung, Lennox E. Iton, Steven L. Suib, and Z. Zhang. "Particle size determination of cobalt clusters in zeolites." Chemistry of Materials 1, no. 5 (September 1989): 529–34. http://dx.doi.org/10.1021/cm00005a014.

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Tillery, Marvin, and Roy Buchan. "Determination of Large Aerosol Particle Size by Elutriation." Applied Occupational and Environmental Hygiene 17, no. 10 (October 2002): 717–22. http://dx.doi.org/10.1080/10473220290106695.

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Aref’ev, I. M., and A. V. Lebedev. "Determination of maximum particle size in magnetic fluids." Colloid Journal 78, no. 2 (March 2016): 269–72. http://dx.doi.org/10.1134/s1061933x16020022.

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