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Journal articles on the topic 'Fluidized-bed combustion. Fluidization. Chemical engineering'

Author: Grafiati

Published: 4 June 2021

Last updated: 5 February 2022

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1

Zabagło, Jadwiga, Jerzy Baron, Małgorzata Olek, Stanisław Kandefer, and Witold Żukowski. "The use of the fluidized bed boiler for the disposal of the multi-material packaging waste." Polish Journal of Chemical Technology 12, no. 4 (2010): 19–21. http://dx.doi.org/10.2478/v10026-010-0043-9.

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The use of the fluidized bed boiler for the disposal of the multi-material packaging waste The paper presents the results of the disposal of packaging waste from two companies: Tetra Pak and Combibloc, carried out in a fluidized bed boiler of rated thermal power 0.5 MW. The material introduced into the fluidized bed boiler underwent thermal and mechanical degradation in a sand bed of the temperature between 750 and 850°C. The process proceeds auto-thermally, without the need of additional fuel. The appropriately chosen fluidization parameters caused the separation of the solid products of combustion from the deposit material. Presence of aluminum, part of it in an un-oxidized form, was confirmed in separated dust. The gaseous products of combustion contained the traces of oxides of nitrogen and sulfur, mainly originating from the remnants of food products contained in the packaging. However, the concentration of these oxides met the requirements of emission standards.

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2

Szücs, Botond, and Pál Szentannai. "Experimental Investigation on Mixing and Segregation Behavior of Oxygen Carrier and Biomass Particle in Fluidized Bed." Periodica Polytechnica Mechanical Engineering 63, no. 3 (2019): 188–94. http://dx.doi.org/10.3311/ppme.13764.

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In this work, lab-scale cold fluidization equipment is designed and constructed to investigate the mixing and segregating phenomena of binary fluidized beds. The focus of the investigation is carbon reduction with the fluidized bed technology-based Chemical Looping Combustion (CLC). Nowadays, aspiration to carbon reduction focuses on the solid fuels. Therefore, it is of great importance to integrate the benefits of CLC technology with the use of solid fuels. The measurements of fuel particles in the fluidized bed are extended from the homogeneous and spherical shape to the inhomogeneous, non-spherical shape. During the tests, an iron-based oxygen carrier (OC) for chemical looping combustors is examined with different particle sizes. In addition, the tests included the examination of three different fuel samples (crushed coal, agricultural pellet, and Solid Recovered Fuel (SRF)), which can be utilized in chemical looping combustion with In-situ gasification. The experiments are carried out using the bed-frozen method. With this method, the vertical concentration of active particles could be measured. The results show that the particle size of the oxygen carrier does fundamentally influence its vertical placement, and the non-spherical character of most alternative fuels must also be considered for optimal reactor design.

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3

Dawson, M. Robert, and Robert C. Brown. "Bed material cohesion and loss of fluidization during fluidized bed combustion of midwestern coal." Fuel 71, no. 5 (1992): 585–92. http://dx.doi.org/10.1016/0016-2361(92)90158-k.

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4

Faravelli, Tiziano, Alessio Frassoldati, Eliseo Ranzi, Miccio Francesco, and Miccio Michele. "Modeling Homogeneous Combustion in Bubbling Beds Burning Liquid Fuels." Journal of Energy Resources Technology 129, no. 1 (2006): 33–41. http://dx.doi.org/10.1115/1.2424957.

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This paper introduces a model for the description of the homogeneous combustion of various fuels in fluidized bed combustors (FBC) at temperatures lower than the classical value for solid fuels, i.e., 850°C. The model construction is based on a key bubbling fluidized bed feature: A fuel-rich (endogenous) bubble is generated at the fuel injection point, travels inside the bed at constant pressure, and undergoes chemical conversion in the presence of mass transfer with the emulsion phase and of coalescence with air (exogenous) bubbles formed at the distributor and, possibly, with other endogenous bubbles. The model couples a fluid-dynamic submodel based on two-phase fluidization theory with a submodel of gas phase oxidation. To this end, the model development takes full advantage of a detailed chemical kinetic scheme, which includes both the low and high temperature mechanisms of hydrocarbon oxidation, and accounts for about 200 molecular and radical species involved in more than 5000 reactions. Simple hypotheses are made to set up and close mass balances for the various species as well as enthalpy balances in the bed. First, the conversion and oxidation of gaseous fuels (e.g., methane) were calculated as a test case for the model; then, n-dodecane was taken into consideration to give a simple representation of diesel fuel using a pure hydrocarbon. The model predictions qualitatively agree with some of the evidence from the experimental data reported in the literature. The fate of hydrocarbon species is extremely sensitive to temperature change and oxygen availability in the rising bubble. A preliminary model validation was attempted with results of experiments carried out on a prepilot, bubbling combustor fired by underbed injection of a diesel fuel. Specifically, the model results confirm that heat release both in the bed and in the freeboard is a function of bed temperature. At lower emulsion phase temperatures many combustible species leave the bed unburned, while post-combustion occurs after the bed and freeboard temperature considerably increases. This is a well-recognized undesirable feature from the viewpoint of practical application and emission control.

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5

Johari, Anwar, Tuan Amran Tuan Abdullah, Mimi Haryani Hassim, et al. "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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6

Raveendran, K., W. A. R. Jayarathna, A. D. U. S. Amarasinghe, and W. S. Botheju. "Modeling the effect of shrinkage on fluidized bed drying of orthodox broken type tea." Chemical Industry and Chemical Engineering Quarterly 25, no. 3 (2019): 299–307. http://dx.doi.org/10.2298/ciceq180821008r.

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Fermented tea particles (dhool) are a polydisperse system subject to shrinkage during fluidized bed drying, which is an important process in the production of orthodox broken type tea. The effect of shrinkage on the physical properties and the minimum fluidization velocity were studied. Five different moisture contents of dhool particles were chosen in the range of 3-106 mass% (dry basis) and the changes in particle diameters and particle densities were measured. For each of the moisture contents, the minimum fluidization velocity was found for three different bed loadings using ambient air at 25?C in a fluidized bed with an area of 351?345 mm2. Since the conventional industrial type fluidized bed dryers operate at 124?C, the new correlations among the Archimedes number, Reynolds number at minimum fluidization and dimensionless moisture content were developed using air properties at 124?C. The results were validated for orthodox broken type tea, drying at 124?C, in a fluidized bed dryer with bed loadings in the range of 44.5 to 50.5 kg/m2. The predicted fluidization velocity was found to be in good agreement with the experimental data and the difference was below 10% for most cases.

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7

Yamazaki, Ryohei, Ryokichi Sugioka, Osamu Ando, and Genji Jimbo. "Minimum fluidization velocity of inclined fluidized bed." KAGAKU KOGAKU RONBUNSHU 15, no. 2 (1989): 219–25. http://dx.doi.org/10.1252/kakoronbunshu.15.219.

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8

Tanaka, Zennosuke, Tadashi Miya, and Teruo Takahashi. "Fluidization Characteristics of a Centrifugal Fluidized Bed." KAGAKU KOGAKU RONBUNSHU 19, no. 4 (1993): 605–9. http://dx.doi.org/10.1252/kakoronbunshu.19.605.

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9

Fan, L. T., C. C. Chang, Y. S. Yu, Teruo Takahashi, and Zennosuke Tanaka. "Incipient fluidization condition for a centrifugal fluidized bed." AIChE Journal 31, no. 6 (1985): 999–1009. http://dx.doi.org/10.1002/aic.690310617.

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10

Zhang, Yi, Kheng-Lim Goh, Yuen-Ling Ng, Yvonne Chow, and Vladimir Zivkovic. "Design and Investigation of a 3D-Printed Micro-Fluidized Bed." ChemEngineering 5, no. 3 (2021): 62. http://dx.doi.org/10.3390/chemengineering5030062.

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Micro-fluidized bed has aroused much attention due to its low-cost, intensified-process and fast-screening properties. In this paper, a micro-fluidized bed (15 × 15 mm in cross-section) was designed and fabricated with the use of the stereolithography printing technique, for the investigation of bubbles’ hydrodynamics and comparison of the solids (3D-printed particles VS fungal pellets) fluidization characteristics. In a liquid–gas system, bubble flow regime started from mono-dispersed homogeneous regime, followed by poly-dispersed homogeneous regime, transition bubble regime and heterogeneous bubble regime with increasing gas flowrates from 3.7 mL/min to 32.7 mL/min. The impacts from operating parameters such as gas flowrate, superficial liquid velocity and gas sparger size on bubble size, velocity and volume fraction have been summarized. In liquid–solid fluidization, different solid fluidization regimes for both particles bed and pellets bed were identified. From the bed expansion results, much higher Umf of 7.8 mm/s from pellets fluidization was observed compared that of 2.3 mm/s in particles fluidization, because the hyphal structures of fungal pellets increased surface friction but also tended to agglomerate. The similar R–Z exponent n (5.7 and 5.5 for pellets and particles, respectively) between pellets and particles was explained by the same solid diameter, but much higher Ut of 436 µm/s in particles bed than that of 196 µm/s in pellets bed is a consequence of the higher density of solid particles. This paper gives insights on the development of MFB and its potential in solid processing.

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11

Mawatari, Yoshihide, Yuji Tatemoto, and Katsuji Noda. "Prediction of minimum fluidization velocity for vibrated fluidized bed." Powder Technology 131, no. 1 (2003): 66–70. http://dx.doi.org/10.1016/s0032-5910(02)00323-6.

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12

Liu, Zihan, Huaqing Ma, and Yongzhi Zhao. "CFD-DEM Simulation of Fluidization of Polyhedral Particles in a Fluidized Bed." Energies 14, no. 16 (2021): 4939. http://dx.doi.org/10.3390/en14164939.

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Fluidization of non-spherical particles is a common process in energy industries and chemical engineering. Understanding the fluidization of non-spherical particles is important to guide relevant processes. There already have been numerous studies which investigate the behaviors of different non-spherical particles during fluidization, but the investigations of the fluidization of polyhedral particles do not receive much attention. In this study, the investigation of the fluidization of polyhedral particles described by the polyhedron approach is conducted with a numerical CFD-DEM method. Experiments of the fluidization of three kinds of polyhedral particles are conducted under the same condition with corresponding simulations to validate the accuracy of our CFD-DEM model. The results indicate that our CFD-DEM model with the polyhedron approach can predict the behaviors of polyhedral particles with reasonable accuracy. Fluidization behaviors of different polyhedral particles are also investigated in this study. Compared to spherical particles, the motion of polyhedral particles is stronger, and mixing degree is higher under the same fluidization gas velocity.

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13

Skopec, Pavel, and Jan Hrdlička. "SPECIFIC FEATURES OF THE OXYFUEL COMBUSTION CONDITIONS IN A BUBBLING FLUIDIZED BED." Acta Polytechnica 56, no. 4 (2016): 312–18. http://dx.doi.org/10.14311/ap.2016.56.0312.

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Oxyfuel combustion is a promising approach for capturing CO<sub>2</sub> from power plants. This technology produces a flue gas with a high concentration of CO<sub>2</sub>. Our paper presents a verification of the oxyfuel combustion conditions in a bubbling fluidized bed combustor. It presents a theoretical analysis of oxyfuel combustion and makes a comparison with combustion using air. It is important to establish a proper methodology for stoichiometric calculations and for computing the basic characteristic fluidization properties. The methodology presented here has been developed for general purposes, and can be applied to calculations for combustion with air and with oxygen-enriched air, and also for full oxyfuel conditions. With this methodology, we can include any water vapour condensation during recirculation of the flue gas when dry flue gas recirculation is used. The paper contains calculations for a lignite coal, which is taken as a reference fuel for future research and for the experiments.

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14

Nemoda, Stevan, Milijana Paprika, Milica Mladenovic, Ana Marinkovic, and Goran Zivkovic. "Two-dimensional mathematical model of liquid fuel combustion in bubbling fluidized bed applied for a fluidized furnace numerical simulation." Thermal Science 22, no. 2 (2018): 1121–35. http://dx.doi.org/10.2298/tsci170922307n.

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Lately, experimental methods and numerical simulations are equally employed for the purpose of developing incineration bubbling fluidized bed (BFB) facilities. The paper presents the results of the 2-D CFD model of liquid fuel combustion in BFB, applied for numerical simulation of a fluidized bed furnace. The numerical procedure is based on the two-fluid Euler-Euler approach, where the velocity field of the gas and particles are modeled in analogy to the kinetic gas theory. The proposed numerical model comprises energy equations for all three phases (gas, inert fluidized particles, and liquid fuel), as well as the transport equations of chemical components that are participating in the reactions of combustion and devolatilization. The model equations are solved applying a commercial CFD package, whereby the user submodels were developed for heterogenic fluidized bed combustion of liquid fuels and for interphase drag forces for all three phases. The results of temperature field calculation were compared with the experiments, carried out in-house, on a BFB pilot facility. The numerical experiments, based on the proposed mathematical model, have been used for the purposes of analyzing the impacts of various fuel flow rates, and fluidization numbers, on the combustion efficiency and on the temperature fields in the combustion zone.

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15

Bai, D., Y. Masuda, N. Nakagawa, and K. Kato. "Transition to turbulent fluidization in a binary solids fluidized bed." Canadian Journal of Chemical Engineering 74, no. 1 (1996): 58–62. http://dx.doi.org/10.1002/cjce.5450740108.

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16

Leon, M. A., and A. Dutta. "Fluidization characteristics of rice husk in a bubbling fluidized bed." Canadian Journal of Chemical Engineering 88, no. 1 (2010): 18–22. http://dx.doi.org/10.1002/cjce.20245.

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17

Leon, M. A., and A. Dutta. "Fluidization characteristics of rice husk in a bubbling fluidized bed." Canadian Journal of Chemical Engineering 88, no. 2 (2010): 306. http://dx.doi.org/10.1002/cjce.20292.

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18

Hainley, D. C., M. Z. Haji-Sulaiman, S. Yavuzkurt, and A. W. Scaroni. "Operating Experience With a Fluidized Bed Test Combustor." Journal of Energy Resources Technology 109, no. 2 (1987): 58–65. http://dx.doi.org/10.1115/1.3231325.

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This paper presents operating experience with a fluidized bed combustor burning various coals. The primary focus is on the effect of relevant coal properties on combustor performance. Tests were carried out using anthracite, HVB and HVC bituminous and sub-bituminous A coals, and petroleum coke. Comparisons of the performance of the combustion on the various fuels are made. A two-stage fluidized bed combustor operating in a single-stage mode without recycle was employed. Experimental measurements included temperature, fuel feed rate, fluidization velocity and bed height. For some of the coals, bed agglomeration was found to occur. The results indicate that coal properties have an important effect upon the operation of the fluidized bed combustor.

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19

Nemoda, Stevan, Milica Mladenovic, Milijana Paprika, Dragoljub Dakic, Aleksandar Eric, and Mirko Komatina. "Euler-Euler granular flow model of liquid fuels combustion in a fluidized reactor." Journal of the Serbian Chemical Society 80, no. 3 (2015): 377–89. http://dx.doi.org/10.2298/jsc140130029n.

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The paper deals with the numerical simulation of liquid fuel combustion in a fluidized reactor using a two-fluid Eulerian-Eulerian fluidized bed modeling incorporating the kinetic theory of granular flow (KTGF) to gas and solid phase flow prediction. The comprehensive model of the complex processes in fluidized combustion chamber incorporates, besides gas and particular phase velocity fields? prediction, also the energy equations for gas and solid phase and the transport equations of chemical species conservation with the source terms due to the conversion of chemical components. Numerical experiments show that the coefficients in the model of inter-phase interaction drag force have a significant effect, and they have to be adjusted for each regime of fluidization. A series of numerical experiments was performed with combustion of the liquid fuels in fluidized bed (FB), with and without significant water content. The given estimations are related to the unsteady state, and the modeled time period corresponds to flow passing time throw reactor column. The numerical experiments were conducted to examine the impact of the water content in a liquid fuel on global FB combustion kinetics.

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20

Datta, Ahi Bhushan, Shib Shankar Nandi, and Debdas Bhaduri. "Fluidized bed combustion of coal." Fuel 64, no. 4 (1985): 564–67. http://dx.doi.org/10.1016/0016-2361(85)90094-8.

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21

Ataíde, Carlos Henrique, Cássia Regina Cardoso, and Lais Reis Borges. "Physical Characterization and Biomass Fluidization (Fume Powder)." Materials Science Forum 660-661 (October 2010): 1105–11. http://dx.doi.org/10.4028/www.scientific.net/msf.660-661.1105.

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The development of big cities and industrialization has been causing environmental degradation problems, damaging natural and energetic resources, besides the bigger production of wastes. So, it is essential the use of renewable alternative fuels, and industrial wastes processing. Biomass can be used in direct combustion, thermo chemical and biological processes. The fume powder is an important waste of tobacco industries. This work makes a characterization of fume powder, originated from Souza Cruz (Uberlândia unit); the objective is to realize the fast pyrolysis in a bubble fluidized bed. Physical analyses of the powder were made to determine the size distribution, and the medium diameter; the solids density and moisture content (dry base). The elementary composition of the material was also determined. The powder fluidization in an acrylic bed (160 cm heights, 10 cm id), was realized to obtain the minimum fluidization velocity.

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22

Priem, Richard J. "Pressurized fluidized bed combustion technology." Combustion and Flame 62, no. 1 (1985): 101. http://dx.doi.org/10.1016/0010-2180(85)90098-7.

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23

Babul, Tomasz, Aleksander Ciski, and Paweł Oleszczak. "The New Fluidized Bed Thermo-Chemical Treatment in Chemically Active Powders – CFD Analysis of the Method." Advanced Materials Research 902 (February 2014): 82–87. http://dx.doi.org/10.4028/www.scientific.net/amr.902.82.

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The paper describes the principles of carrying out of a new type of fluidized bed thermo-chemical treatment in chemically active powders with fluidization by chemically inert gas. The article presents selected results of a computer simulation of chemically active fluidized bed phenomena used in the thermo-chemical treatment of steel. For this purpose, a numerical model of the fluidized bed with a specific calculation area, has been prepared. The results of CFD (Computational Fluid Dynamics) computer simulation of temperature distribution and fluidizing gas mass distribution along the walls of samples placed in the fluidized bed are presented. Results of exemplary carburizing process are given. Metallographic observations and hardness measurements confirm the correctness of the of the carburized layer structure, which was formed on the C22 unalloyed carbon steel.

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24

Nakamura, Hideya, and Satoru Watano. "Numerical modeling of particle fluidization behavior in a rotating fluidized bed." Powder Technology 171, no. 2 (2007): 106–17. http://dx.doi.org/10.1016/j.powtec.2006.08.021.

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25

Tamarin, A. I., and L. I. Levental'. "Diffusion approximation for fluidized-bed coal combustion." Journal of Engineering Physics 58, no. 4 (1990): 465–69. http://dx.doi.org/10.1007/bf00877355.

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26

ATAKÜL, H., G. ÖNER, and M. F. YARDİM. "Fluidized Bed Combustion Research in Turkey." Energy Sources 15, no. 1 (1993): 1–15. http://dx.doi.org/10.1080/00908319308909006.

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27

el, Mafadi, Murielle Hayert, and Denis Poncelet. "Fluidization control in the wurster coating process." Chemical Industry 57, no. 12 (2003): 641–44. http://dx.doi.org/10.2298/hemind0312641e.

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Paniculate coating process in a fluidized bed involves different sub processes including particle wetting, spreading and also consolidation or drying of the coating applied. These sub processes are done simultaneously to particle fluidization and motion. All the parameters of fluidization are known to affect the coating quality. That is why the motion of particles in the Wurster coating process has been observed and described step by step. These observations have achieved a general understanding of phenomena which take place inside the bed during fluidization and have allowed the development of an easy method for optimizing all the parameters affecting this operation.

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28

Umez-Eronini, E. I., and J. N. Cannon. "Nonradiative Heat Transfer Coefficients and “Cold” Operating Experience With a Laboratory SCFBC Model." Journal of Energy Resources Technology 108, no. 2 (1986): 179–82. http://dx.doi.org/10.1115/1.3231259.

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A cold test model study of the staged cascade fluidized bed coal combustion process is described. Proper cascade flow of solids through the system was found to be sensitive to bed and downcomer distributor plate pressure drops. Control of bed depth by weir level was also complicated at high fluidization velocities by the process of entrained particles falling back into the downcomer. Bed to tube heat transfer coefficients ranging from 142 to 256W/m2•K were measured at the top surface of a simulated boiler tube in shallow beds, 0.15 to 0.23m deep.

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29

Wee, Siaw K., Vui S. Chok, C. Srinivasakannan, Han B. Chua, and Hong M. Yan. "Fluidization Quality Study in a Compartmented Fluidized Bed Gasifier (CFBG)†." Energy & Fuels 22, no. 1 (2008): 61–66. http://dx.doi.org/10.1021/ef700299a.

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30

Zhong, Wenqi, Baosheng Jin, Yong Zhang, Xiaofang Wang, and Rui Xiao. "Fluidization of Biomass Particles in a Gas−Solid Fluidized Bed." Energy & Fuels 22, no. 6 (2008): 4170–76. http://dx.doi.org/10.1021/ef800495u.

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31

Di Renzo, Alberto, Fabrizio Scala, and Stefan Heinrich. "Recent Advances in Fluidized Bed Hydrodynamics and Transport Phenomena—Progress and Understanding." Processes 9, no. 4 (2021): 639. http://dx.doi.org/10.3390/pr9040639.

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32

Hattori, Manabu, Hitoki Matsuda, Wojciech Nowak, and Masanobu Hasatani. "Fluidization characteristics of a circulating fluidized bed with an internal nozzle." JOURNAL OF CHEMICAL ENGINEERING OF JAPAN 25, no. 5 (1992): 592–97. http://dx.doi.org/10.1252/jcej.25.592.

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33

Zhu, Quanhong, Libo Zhang, and Weikang Hao. "Determining minimum fluidization velocity in magnetized fluidized bed with Geldart-B particles." Powder Technology 389 (September 2021): 85–95. http://dx.doi.org/10.1016/j.powtec.2021.05.018.

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34

Kim, Mi-Ran, Kyoung-Hee Kim, Jeong-Gook Jang, and Jea-Keun Lee. "Prediction of Bed Agglomeration Potential in Fluidized Bed Combustion Processes." JOURNAL OF CHEMICAL ENGINEERING OF JAPAN 41, no. 7 (2008): 721–28. http://dx.doi.org/10.1252/jcej.07we089.

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35

Duan, Feng, Chien-Song Chyang, Shih-Ho Hsu, and Jim Tso. "Combustion behavior and pollutant emissions of batch fluidized bed combustion." Journal of the Taiwan Institute of Chemical Engineers 44, no. 6 (2013): 1034–38. http://dx.doi.org/10.1016/j.jtice.2013.03.011.

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36

Wang, Jiaying, Zeneng Sun, Yuanyuan Shao, and Jesse Zhu. "Operating regimes in circulating fluidized bed combustors: fast fluidization or bubbling-entrained bed?" Fuel 297 (August 2021): 120727. http://dx.doi.org/10.1016/j.fuel.2021.120727.

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37

Anthony, E. J., A. MacKenzie, O. Trass, et al. "Advanced Fluidized Bed Combustion Sorbent Reactivation Technology." Industrial & Engineering Chemistry Research 42, no. 6 (2003): 1162–73. http://dx.doi.org/10.1021/ie020305h.

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38

Skrifvars, Bengt Johan, Mikko Hupa, and Matti Hiltunen. "Sintering of ash during fluidized bed combustion." Industrial & Engineering Chemistry Research 31, no. 4 (1992): 1026–30. http://dx.doi.org/10.1021/ie00004a008.

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39

Lee, Kyeong-Ook, Jon J. Cohen, and Kenneth Brezinsky. "Fluidized-bed combustion synthesis of titanium nitride." Proceedings of the Combustion Institute 28, no. 1 (2000): 1373–80. http://dx.doi.org/10.1016/s0082-0784(00)80352-5.

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40

Liang, Xizhen, Hao Duan, Tao Zhou, and Jiangrong Kong. "Fluidization behavior of binary mixtures of nanoparticles in vibro-fluidized bed." Advanced Powder Technology 25, no. 1 (2014): 236–43. http://dx.doi.org/10.1016/j.apt.2013.04.005.

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41

Anthony, E. J., and D. L. Granatstein. "Sulfation phenomena in fluidized bed combustion systems." Progress in Energy and Combustion Science 27, no. 2 (2001): 215–36. http://dx.doi.org/10.1016/s0360-1285(00)00021-6.

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42

Chirone, R., L. Massimilla, and P. Salatino. "Comminution of carbons in fluidized bed combustion." Progress in Energy and Combustion Science 17, no. 4 (1991): 297–326. http://dx.doi.org/10.1016/0360-1285(91)90006-9.

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43

Aronsson, Jesper, David Pallarès, Magnus Rydén, and Anders Lyngfelt. "Increasing Gas–Solids Mass Transfer in Fluidized Beds by Application of Confined Fluidization—A Feasibility Study." Applied Sciences 9, no. 4 (2019): 634. http://dx.doi.org/10.3390/app9040634.

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Fluidized bed applications where the bed material plays an active role in chemical reactions, e.g. chemical looping combustion, have seen an increase in interest over the past decade. When these processes are to be scaled up to industrial or utility scale mass transfer between the gas and solids phases can become a limitation for conversion. Confined fluidized beds were conceptualized for other purposes in the 1960’s but are yet to be applied to these recent technologies. Here it is investigated if they can prove useful to increase mass transfer but also if they are feasible from other perspectives such as pressure drop increase and solids throughflow. Four spherical packing solids, 6.35–25.4 mm in diameter at two different densities, were tested. For mass transfer experiments the fluidizing air was humidified and the water adsorption rate onto silica gel particles acting as fluidizing solids was measured. Olivine sand was used in further experiments measuring segregation of solids and packing, and maximum vertical crossflow of solids. It was found that mass transfer increased by a factor of 1.9–3.8 with packing solids as compared to a non-packed reference. With high-density packing, fluidizing solids voidage inside the packing was found to be up to 58% higher than in a conventional fluidized bed. Low density packing material favoured its flotsam segregation and with it higher fluidization velocities yield better mixing between packing and fluidizing solids. Maximum vertical cross-flow was found to be significantly higher with low density packing that fluidized, than with stationary high-density packing. Conclusively, the prospect of using confined fluidized beds for improving mass transfer looks promising from both performance and practical standpoints.

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Cui, Yunlei, Wenming Fu, Yaning Zhang, et al. "Experimental fluidization performances of silicon carbide in a fluidized bed." Chemical Engineering and Processing - Process Intensification 154 (August 2020): 108016. http://dx.doi.org/10.1016/j.cep.2020.108016.

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Sau, D. C., Swati Mohanty, and K. C. Biswal. "Minimum fluidization velocity at elevated temperature in tapered fluidized bed." Chemical Engineering and Processing: Process Intensification 47, no. 12 (2008): 2391–94. http://dx.doi.org/10.1016/j.cep.2007.11.016.

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Pejanovic, Srdjan. "Absorption in a three-phase fluidized bed I: Hydrodynamic investigations." Chemical Industry 57, no. 7-8 (2003): 326–29. http://dx.doi.org/10.2298/hemind0308326p.

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The hydrodynamic properties of a three phase fluidized bed with low density inert spherical packing, fluidized by the interaction of a gas flowing upwards and a liquid flowing downwards through the column, were investigated. It was found that the pressure drop, liquid hold up and dynamic bed height increase with both increasing liquid and gas flow rate. While the dynamic bed height and minimum fluidization velocity remain unchanged, both the pressure drop and liquid hold up increase with increasing density of the packing. Therefore, an increase in packing density causes more intensive mass transfer between the fluid phases than packed columns. It was shown that increase of the liquid flow rate causes an increase of both the effective liquid and gas velocity through the fluidized bed, which may also improve mass transfer.

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Hoteit, A., M. K. Chandel, S. Durécu, and A. Delebarre. "Biogas combustion in a chemical looping fluidized bed reactor." International Journal of Greenhouse Gas Control 3, no. 5 (2009): 561–67. http://dx.doi.org/10.1016/j.ijggc.2009.04.003.

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Han, Keun-Hee, Jaehyeon Park, Jung-In Ryu, and Gyoung-Tae Jin. "Coal combustion characteristics in a pressurized fluidized bed." Korean Journal of Chemical Engineering 16, no. 6 (1999): 804–9. http://dx.doi.org/10.1007/bf02698356.

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Scala, Fabrizio, Riccardo Chirone, and Piero Salatino. "Fluidized bed combustion of tyre derived fuel." Experimental Thermal and Fluid Science 27, no. 4 (2003): 465–71. http://dx.doi.org/10.1016/s0894-1777(02)00249-2.

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Scala, Fabrizio, and Riccardo Chirone. "Fluidized bed combustion of alternative solid fuels." Experimental Thermal and Fluid Science 28, no. 7 (2004): 691–99. http://dx.doi.org/10.1016/j.expthermflusci.2003.12.005.

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