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Статті в журналах з теми "Fluidizing"

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Автор: Grafiati

Опубліковано: 30 травня 2022

Оновлено: 31 травня 2022

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1

Yamada, Jun, Yasuo Kurosaki, and Takanori Nagai. "Radiation Heat Transfer Between Fluidizing Particles and a Heat Transfer Surface in a Fluidized Bed." Journal of Heat Transfer 123, no. 3 (January 8, 2001): 458–65. http://dx.doi.org/10.1115/1.1370503.

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We have investigated the radiation heat transfer occurring in a gas-solid fluidized bed between fluidizing particles and a cooled heat transfer surface. Experimental results reveal that cooled fluidizing particles exist near the surface and suppress the radiation heat transfer between the surface and the higher temperature particles in the depth of the bed. The results also clarify the effects of fluidizing velocity, optical characteristics of particles, and particle diameter on the radiation heat transfer. Based on these results, the authors propose a model for predicting the radiation heat transfer between fluidizing particles and a heat transfer surface.

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2

Jeong, Y., B. G. Park, and J. S. Chung. "High Performance Biofilm Process for Treating Wastewater Discharged from Coal Refining Plants Containing Nitrogen, Cyanide and Thiocyanate." Water Science and Technology 52, no. 10-11 (November 1, 2005): 325–34. http://dx.doi.org/10.2166/wst.2005.0709.

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Wastewater discharge from coal refining plants contains a number of biologically toxic compounds; 2000–2500mg/l of COD of which 40% is composed of phenol, 100–400mg/l of thiocyanate, 10–40mg/l of cyanide, 100–250mg/l of NH4+-N and 150–300mg/l of total nitrogen. In order to treat this kind of high strength wastewater, we have developed a high performance biofilm process using fluidizing bio-carriers of the tube chip type. The fluidizing biofilm carriers are made of a composite of polyethylene and several inorganic materials, whose density is controlled at 0.97–0.98g/ml. The fluidizing biofilm carriers show sound fluidization characteristics inside bioreactors. The wastewater is treated using three consecutive series reactors in oxic–anoxic–oxic arrangement. Each reactor is charged with the fluidizing biofilm carriers of 50 vol%. Furthermore, newly cultured active microorganisms for the thiocyanate biodegradation are added in the biofilm process. At total hydraulic retention time of 2.2 days, this process can achieve steady state removal efficiencies: COD, 99%; thiocyanate, 99%; NH4+-N, 99% and total nitrogen, 90%.

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3

Friedman, J., P. Koundakjian, D. Naylor, and D. Rosero. "Heat Transfer to Small Horizontal Cylinders Immersed in a Fluidized Bed." Journal of Heat Transfer 128, no. 10 (March 22, 2006): 984–89. http://dx.doi.org/10.1115/1.2345425.

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Heat transfer to horizontal cylinders immersed in fluidized beds has been extensively studied, but mainly in the context of heat transfer to boiler tubes in coal-fired beds. As a result, most correlations in the literature have been derived for cylinders of 25-50mm diameter in vigorously fluidizing beds. In recent years, fluidized bed heat treating furnaces fired by natural gas have become increasingly popular, particularly in the steel wire manufacturing industry. These fluidized beds typically operate at relatively low fluidizing rates (G∕Gmf<5) and with small diameter wires (1-6mm). Nusselt number correlations developed based on boiler tube studies do not extrapolate down to these small size ranges and low fluidizing rates. In order to obtain reliable Nusselt number data for these size ranges, an experimental investigation has been undertaken using two heat treating fluidized beds; one a pilot-scale industrial unit and the other a lab-scale (300mm diameter) unit. Heat transfer measurements were obtained using resistively heated cylindrical samples ranging from 1.3 to 9.5mm in diameter at fluidizing rates ranging from approximately 0.5×Gmf (packed bed condition) to over 10×Gmf using aluminum oxide sand particles ranging from dp=145-330μm (50–90 grit). It has been found that for all cylinder sizes tested, the Nusselt number reaches a maximum near 2×Gmf, then remains relatively steady (±5-10%) to the maximum fluidizing rate tested, typically 8-12×Gmf. A correlation for maximum Nusselt number is developed.

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4

Annamalai, Kalyan, Miguel Ruiz, Nhat Vo, and Vadakkath Anand. "Locally fluidizing feeder for powder transport." Powder Technology 73, no. 2 (December 1992): 181–90. http://dx.doi.org/10.1016/0032-5910(92)80079-c.

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5

PAN, T. W., D. D. JOSEPH, R. BAI, R. GLOWINSKI, and V. SARIN. "Fluidization of 1204 spheres: simulation and experiment." Journal of Fluid Mechanics 451 (January 25, 2002): 169–91. http://dx.doi.org/10.1017/s0022112001006474.

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Анотація:

In this paper we study the fluidization of 1204 spheres at Reynolds numbers in the thousands using the method of distributed Lagrange multipliers. The results of the simulation are compared with an experiment. This is the first direct numerical simulation of a fluidized bed at the finite Reynolds numbers encountered in applications. The simulations are processed to give straight lines in log–log plots leading to power laws as in the celebrated experimental correlations of Richardson & Zaki (1954). The numerical method allows the first direct calculation of the slip velocity and other averaged values used in two-fluid continuum models. The computation and the experiment show that a single particle may be in balance with respect to weight and drag for an interval of fluidizing velocities; the expectation that the fluidizing velocity is unique is not realized. The numerical method reveals that the dynamic pressure decreases slowly with the fluidizing velocity. Tentative interpretations of these new results are discussed.

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6

Wu, Xing, Yaxiang Li, Xiefei Zhu, Lingrui Huang, and Xifeng Zhu. "Experimental study on fluidization behaviors of walnut shell in a fluidized bed assisted by sand particles." RSC Advances 8, no. 70 (2018): 40279–87. http://dx.doi.org/10.1039/c8ra07959e.

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7

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 (February 14, 2019): 634. http://dx.doi.org/10.3390/app9040634.

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Анотація:

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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8

Karlicic, Nikola, Aleksandar Jovovic, Dejan Radic, Marko Obradovic, Dusan Todorovic, and Miroslav Stanojevic. "The Effect of Permeability on Lignite Fly Ash Pneumatic Conveying System Design." Revista de Chimie 69, no. 2 (March 15, 2018): 341–45. http://dx.doi.org/10.37358/rc.18.2.6103.

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The aim of this experimental study was to evaluate the effect of permeability on the mode of flow that lignite fly ash will support in a pneumatic conveying pipeline. This research was initiated by recurring problems with the long distance and high capacity low grade lignite ash pneumatic conveying system at the 1200 MWe thermal power plant, such as clogging, unsteady flow mode, significant increase of velocity due to pressure drop and erosive wear of pipeline. Ash samples were taken during pneumatic conveying system clogging for further analysis. The experiment was limited to measuring parameters that provide data to determine minimum fluidizing velocity and permeability. The results showed very heterogeneous materials of group B by Geldart, what caused specific phenomenon during the experimental fluidization tests. Minimum fluidizing velocity for this kind of material is not authoritative for defining pneumatic conveying system, since extremely heterogeneous materials at this air speed will remain stationary or will convey very slow or with stoppage, and that required velocities are from 10 to 15 times higher than minimum fluidizing velocity. According to the results, this ash is the most suitable for dense phase pneumatic conveying.

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9

Li, Hongzhong, Rouyu Hong, and Zhaolin Wang. "Fluidizing ultrafine powders with circulating fluidized bed." Chemical Engineering Science 54, no. 22 (November 1999): 5609–15. http://dx.doi.org/10.1016/s0009-2509(99)00293-6.

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10

Chyang, Chien-Song, and Yen-Chin Lin. "A Study in the Swirling Fluidizing Pattern." JOURNAL OF CHEMICAL ENGINEERING OF JAPAN 35, no. 6 (2002): 503–12. http://dx.doi.org/10.1252/jcej.35.503.

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11

Tsuchiya, H. "Structure-Specific Membrane-Fluidizing Effect Of Propofol." Clinical and Experimental Pharmacology and Physiology 28, no. 4 (April 2001): 292–99. http://dx.doi.org/10.1046/j.1440-1681.2001.03441.x.

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12

Li, Qian Jun, and Dong Ping Zhang. "Experimental Investigation on Flow Patterns of Cylindrical-Conical Spout-Fluidizing Bed." Advanced Materials Research 354-355 (October 2011): 338–43. http://dx.doi.org/10.4028/www.scientific.net/amr.354-355.338.

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Experimental investigations on hydrodynamic characteristics of cylindrical pressurized spout-fluidizing bed were carried out. Two kinds of millet were used as bed materials. The operational pressure is 0.1MPa~0.4MPa (absolutely pressure). Five distinct flow patterns, i.e, fixed bed(FB), jet in fluidized bed with bubbles(JFB), jet in fluidized bed with slugging(JFS), spout with aeration(SA) and spout-fluidizing bed(SF) were identified. Effects of the static bed height and operational pressure on the flow pattern map were particularly studied. Typical flow pattern images obtained by a high- resolution digital CCD camera were presented for classifying these flow patterns. Typical flow pattern maps were plotted for describing the transitions between flow patterns with operating conditions

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13

Smiley, R. W. "A Fluidizing Column for Extracting Cysts of Heterodera avenae from Soil." Plant Disease 96, no. 6 (June 2012): 820–26. http://dx.doi.org/10.1094/pdis-10-11-0892.

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The cereal cyst nematode Heterodera avenae can be extracted from soil using several different floatation or elutriation methods. Automated methods are prohibitively expensive for use in small labs and, for optimal efficiency, floatation methods require that the soil be air dried for an extended period. A method which suspends soil particles in a water column above a fluidizing plate was reported as being most efficient with wet and dry soils. Use of the fluidizing column for extracting H. avenae has not been reported in the United States and materials to construct the column using contemporary components have not been described. Objectives of this research were to construct a column with components available in the United States, and to compare numbers of cysts and eggs plus juveniles (from cysts) extracted by the column and three other floatation methods: Fenwick can, flask, and Cobb sieving. From a soil containing recently produced (more dense) cysts, the column extracted at least 18% more cysts and 23% more eggs plus juveniles than the Fenwick and flask methods. The fluidizing column was found to be useful for small laboratories because it is inexpensive ($253 for two columns), easily and quickly constructed by nonprofessional labor, and produces adequately repeatable results.

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14

Krishnan, Ramaswamy, Xavier Trepat, Trang T. B. Nguyen, Guillaume Lenormand, Madavi Oliver, and Jeffrey J. Fredberg. "Airway smooth muscle and bronchospasm: Fluctuating, fluidizing, freezing." Respiratory Physiology & Neurobiology 163, no. 1-3 (November 2008): 17–24. http://dx.doi.org/10.1016/j.resp.2008.04.006.

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15

Kai, Takami, and Takeshige Takahashi. "Formation of particle agglomerates after switching fluidizing gases." AIChE Journal 43, no. 2 (February 1997): 357–62. http://dx.doi.org/10.1002/aic.690430209.

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16

Wang, Alan L. T., John F. Stubington, and Jiangang Xu. "Hydrodynamic Performance of a Novel Design of Pressurized Fluidized Bed Combustor." Journal of Energy Resources Technology 128, no. 2 (June 3, 2005): 111–17. http://dx.doi.org/10.1115/1.2126987.

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A bench-scale fluidized bed combustor with a novel fluidizing gas injection manifold was successfully built for characterization of Australian black coals under PFBC conditions. Instead of the usual horizontal distributor plate to support the bed and distribute the fluidizing gas, the fluidizing gas was injected horizontally through 8 radial ports in the cylindrical wall of the combustor. To verify satisfactory hydrodynamic performance with the novel gas injection manifold, the fluidization was directly investigated by measuring differential pressure fluctuations under both ambient and PFBC conditions. In addition, a Perspex cold model was built to simulate the hydrodynamics of the hot bed in the PFBC facility. Under PFBC conditions, the bed operated in a stable bubbling regime and the solids were well mixed. The bubbles in the bed were effectively cloudless and no gas backmixing or slugging occurred; so the gas flow in the bed could be modeled by assuming two phases with plug flow through each phase. The ratio of Umf for the simulated bed to Umf for the hot PFBC bed matched the conditions proposed by Glicksman’s scaling laws. The bubbles rose along the bed with axial and lateral movements, and erupted from the bed surface evenly and randomly at different locations. Two patterns of particle movement were observed in the cold model bed: a circular pattern near the top section and a rising and falling pattern dominating in the lower section.

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17

YAMADA, Jun, Norihisa NAGAHARA, Isao SATOH, and Yasuo KUROSAKI. "Conductive Heat Transfer between Fluidizing Particles and a Heat Transfer Surface in a Fluidized Bed. Visualization of Temperature for Fluidizing Particles." Transactions of the Japan Society of Mechanical Engineers Series B 66, no. 648 (2000): 2141–49. http://dx.doi.org/10.1299/kikaib.66.648_2141.

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18

Yamada, Jun, Norihisa Nagahara, Isao Satoh, and Yasuo Kurosaki. "Direct-contact heat exchange between fluidizing particles and a heat transfer surface in a fluidized bed: Temperature visualization of fluidizing particles." Heat Transfer?Asian Research 31, no. 3 (April 18, 2002): 165–81. http://dx.doi.org/10.1002/htj.10027.

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19

DING, JIANMIN, and SHIU-WING TAM. "ASYMPTOTIC POWER SPECTRUM ANALYSIS OF CHAOTIC BEHAVIOR IN FLUIDIZED BEDS." International Journal of Bifurcation and Chaos 04, no. 02 (April 1994): 327–41. http://dx.doi.org/10.1142/s021812749400023x.

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The nonlinear behavior of fluidized beds is analyzed quantitatively using an asymptotic power spectrum method. A model based on kinetic theory is used to compute the voidage signals in a two-dimensional bubbling fluidized bed with a fluidization condition of U/Umf=4, where U is the fluidizing velocity and Umf is the minimum fluidizing velocity. The data for power versus frequency in the asymptotic frequency regime are shown to obey a power-law falloff. This means that the bubbling fluidization under such a fluidization condition cannot be a low-dimensional strange attractor. Pressure fluctuation data, obtained from a three-dimensional bubbling fluidized bed, are also analyzed and clearly show the power-law falloff. This is consistent with previous findings in that the correlation dimension for these data cannot be small (i.e., 2 or 3). The differences between our findings and others are discussed.

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20

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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21

Hussain, Ahmad, Faraz Junejo, Muhammad Nauman Qureshi, and Afzal Haque. "Hydrodynamic and combustion behavior of low grade coals in the riser of a circulating fluidized bed combustor." NUST Journal of Engineering Sciences 11, no. 1 (March 10, 2019): 1–11. http://dx.doi.org/10.24949/njes.v11i1.436.

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This study is conducted for understanding the fluidization behavior in a CFB combustor for low ranked coals. A lab-scale cold CFB test rig was built at the NFCIET Multan for understanding the fluidization behaviour. Influence of fluidizing air on the fluidization behavior was observed. It was found that voidage along the riser height is affected by riser geometry. The combustion behavior of low grade coals from Thar coal was also explored in a CFB Combustor. The influence of the fluidizing air on the combustion erformance was examined and their effect on emissions was established. The temperature in the riser of the CFB rose quickly to around 900°C. This rise in temperature has caused an increase in the amount of exhaust gasses which has their influence on the suspension density. From this study, a firsthand experience of combustion behavior of low grade Pakistani coals was documented.

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22

Ganguly, Amit, W. W. Lee, and K. J. Reid. "Cold model studies on fluidizing characteristics of taconite concentrates." Powder Technology 69, no. 3 (March 1992): 295–98. http://dx.doi.org/10.1016/0032-5910(92)80020-w.

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23

Chen, Kuiren, Tong Wang, Hong Wang, Haoyuan Geng, Jing Du, Dianyu Yu, Walid Elfalleh, Zouhaier Mehrez, and Liqi Wang. "Application of Magnetic Nano-Immobilized Enzyme in Soybean Oil Degumming: Numerical Simulation in a Liquid-Solid MFB." Journal of Food Quality 2021 (September 16, 2021): 1–14. http://dx.doi.org/10.1155/2021/6652780.

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Using crude soybean oil (CSO) as fluid and nanomagnetic immobilized phospholipase C (PLC) as fluidizing particles, the Eulerian–Lagrangian fluid-particle two-phase flow model was used to numerically simulate the law of motion of fluidizing particles in the magnetic fluidized bed (MFB). The main parameters were obtained by numerical simulation based on the discrete element method (DEM). The nanomagnetic PLC in the MFB was optimal to the enzymatic reaction by limiting the iteration step size to 3 × 10−5, the boundary condition to 20 × 300 mm, the opening rate to 37.5%, the condition of CSO flow rate to 0.01 m/s, and the magnetic field strength to 0.02T. After 2.0 h of reaction, the amount of residual phosphorus in the oil was 55.73 mg/kg, the content of 1, 2-DAG was 1.42%, and the nanomagnetic enzyme still had 97% relative activity. Hence, these optimal conditions can improve the efficiency and the stability of the nanomagnetic enzymatic reaction.

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24

Liu, Xing Yong, Hu Yang, You Cheng Wang, and Zhuo Xu Deng. "Study on Filter of Particle Concentration Signal in Silicon Powder Fluidized Bed." Advanced Materials Research 538-541 (June 2012): 2293–97. http://dx.doi.org/10.4028/www.scientific.net/amr.538-541.2293.

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The concentration signal of silica powder in the fluidizing gas i.e. air under different operation conditions were determined. The pretreating effects of concentration signal of silica powder by low pass filtering, wavelet transform de-noising and wavelet packet de-noising were compared. And the optimum method of de-noising has been determined.

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25

Jun, Goo Jia, Vijay R. Raghavan, and Chin Yee Sing. "Experimental Study on the Hydrodynamics of Swirling Fluidized Bed." Applied Mechanics and Materials 229-231 (November 2012): 756–60. http://dx.doi.org/10.4028/www.scientific.net/amm.229-231.756.

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In recent years, the Swirling Fluidized Bed has been regarded as one of the novel designs in fluidization technology. This new technique features an annular blade distributor which injects the fluidizing gas through a certain inclination, is capable of fluidizing the bed and at the same time causes swirling motion of particles in a circular trajectory. In the present work, the fluidization characteristics and hydrodynamics of a swirling bed are studied using an experimental approach. The behavior of gas-particle interaction in a swirling bed in terms of operation regimes, trend of pressure drop across the bed and the hysteresis effect, are explored with varying bed configurations. Seven sets of particles, three in spherical shape, two in cylindrical shape and two in irregular shape, are used as bed material by considering bed weights from 500 g to 2000 g and blade overlap angles 18° for air velocities up to approximately 3.5 m/s and blade inclination of 10°. The results evidently showed that particle configurations dramatically affect the beds’ behavior.

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26

Frey, Shelli L., Eva Y. Chi, Cristóbal Arratia, Jaroslaw Majewski, Kristian Kjaer, and Ka Yee C. Lee. "Condensing and Fluidizing Effects of Ganglioside GM1 on Phospholipid Films." Biophysical Journal 94, no. 8 (April 2008): 3047–64. http://dx.doi.org/10.1529/biophysj.107.119990.

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27

Kai, Takami, Takayuki Kamei, and Takeshige Takahashi. "Effect of gas adsorption on defluidization after switching fluidizing gases." AIChE Journal 44, no. 2 (February 1998): 491–94. http://dx.doi.org/10.1002/aic.690440226.

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28

Lin, Yeuh-Hui, Chun-Chieh Tseng, Ta-Tung Wei, and Chia-Tse Hsu. "Recycling of dual hazardous wastes in a catalytic fluidizing process." Catalysis Today 174, no. 1 (October 2011): 37–45. http://dx.doi.org/10.1016/j.cattod.2011.04.029.

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29

Davidson, Matthew T., and Shelli L. Frey. "Condensing and Fluidizing Effects of Gangliosides on Various Phospholipid Films." Biophysical Journal 98, no. 3 (January 2010): 286a. http://dx.doi.org/10.1016/j.bpj.2009.12.1560.

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30

Chen, Jin, Wen-li Shi, Jing Zhao, Wan-ming Lin, and Ke Liu. "Cold-state spout-fluidizing characteristics of high-carbon ferromanganese powders." International Journal of Minerals, Metallurgy, and Materials 18, no. 6 (December 2011): 741–47. http://dx.doi.org/10.1007/s12613-011-0505-y.

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31

Camargo, F. L., J. D. Pagliuso, and F. E. Milioli. "CONVERSION AND GLOBAL REACTION RATE COEFFICIENT IN THE ABSORPTION OF SO2 BY DIFFERENT TYPES OF LIMESTONE IN A FLUIDIZED BED REACTOR." Revista de Engenharia Térmica 2, no. 1 (June 30, 2003): 50. http://dx.doi.org/10.5380/reterm.v2i1.3519.

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This work concerns the study of the effect of limestone type on SO2 absorption in a bench fluidized bed reactor plant. Conversion and global reaction rate coefficients were established for conditions typical to fluidized bed combustion of coal. The bench plant is a bubbling bed reactor 160 mm internal diameter using silica sand as bed material, fluidized by pre-heated air. In order to simulate conditions close to the fluidized bed coal combustion ambience, the fluidizing air is pre-heated at high temperature (850 oC) and SO2 is added to the fluidizing air in a concentration typical of the process (1000 ppm). All the particulate, i.e. silica sand and limestone particles, was fed to the bed in a narrow size distribution between two subsequent ASTM sieves (with 545 μm mean diameter). In transient batch experiments charges of limestone are quickly injected into the bed, while the consequent variations of the exit concentrations of SO2, CO2 and O2 are continuously recorded. Analysis were performed on the effects of the type of limestone in the process, taking into account possible reaction controlling resistances, and considering possible effects of the calcination on the sulfation process.

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32

Veselý, Václav, Milan Čársky, Jaroslav Pata, and Miloslav Hartman. "Leakage of solids through the perforated distributor." Collection of Czechoslovak Chemical Communications 52, no. 3 (1987): 648–62. http://dx.doi.org/10.1135/cccc19870648.

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Experiments were conducted to explore the effect of free area, orifice diameter and grid thickness on the rate of backflow of particles (leakage, weeping) through the multi-orifice distributor. Air was used as a fluidizing medium. Two sieved fractions of glass beads and ash particles of different shape and density were employed in the experiments. The measured rates of backflow were fitted by an empirical correlation with an accuracy of ±30%.

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33

KAGE, Hiroyuki, Takayuki YOSHIDA, Hiromi MATSUI, and Yoshizo MATSUNO. "The Coating of Fluidizing Particles by Atomization of Fine Powder Suspension." Journal of the Society of Powder Technology, Japan 29, no. 6 (1992): 422–27. http://dx.doi.org/10.4164/sptj.29.422.

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34

OGATA, Toshio, Kensaku HARAGUCHI, Katsutoshi YAMADA, Masataka SASAMORI, Sougo SAYAMA, Yoshio SAKAI, and Hidehiko INOUE. "New Activated Carbon Production Process from Scrap Tire Using Fluidizing Bed." NIPPON KAGAKU KAISHI, no. 9 (2000): 645–49. http://dx.doi.org/10.1246/nikkashi.2000.645.

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35

Mohanty, Y. K., K. C. Biswal, and G. K. Roy. "Mixing characteristics of binary mixtures using promoters and secondary fluidizing medium." Powder Technology 187, no. 2 (October 2008): 103–9. http://dx.doi.org/10.1016/j.powtec.2008.01.028.

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36

RUTHERFORD, JAIN E., and S. W. HORSTMAN. "Generation of Mt. St. Helens Dust with a Fluidizing Dust Generator." American Industrial Hygiene Association Journal 46, no. 2 (February 1985): 94–96. http://dx.doi.org/10.1080/15298668591394464.

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37

Bhattacharya, B., D. Sathiyamoorthy, V. Govardhana Rao, and S. P. Mahajan. "Intermixing of fluidizing gas streams in a compartmented circulating fluidized bed." Chemical Engineering & Technology 20, no. 8 (November 1997): 522–32. http://dx.doi.org/10.1002/ceat.270200803.

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38

Ives, H. E., and A. S. Verkman. "Effects of membrane fluidizing agents on renal brush border proton permeability." American Journal of Physiology-Renal Physiology 249, no. 6 (December 1, 1985): F933—F940. http://dx.doi.org/10.1152/ajprenal.1985.249.6.f933.

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H+ permeability (PH) of brush border membrane vesicles isolated from rabbit renal cortex was measured from the rate of collapse of preformed pH gradients using acridine orange fluorescence quenching. n-Alkanols increased PH from 0.005 to 0.1 cm/s in a dose-dependent manner. At 25 degrees C, PH increased to 0.01 cm/s at [n-alkanol] = 90 mM (butanol), 30 mM (pentanol), 7 mM (hexanol), and 1.8 mM (heptanol). Activation energy (Ea) of PH was 21.6 kcal/mol (5-50 degrees C), which decreased to 18.5 kcal/mol in the presence of either 200 mM butanol or 12 mM hexanol. Membrane fluidity was estimated from diphenylhexatriene anisotropy (r). n-Alkanols decreased r from 0.25 to 0.18 in a dose-dependent manner. At 25 degrees C, r = 0.22 at [n-alkanol] = 200 mM (butanol), 27 mM (pentanol), 9.5 mM (hexanol), and 2 mM (heptanol). The effects of n-alkanols on PH and r correlated well with known n-alkanol lipid-water partition coefficients. Similar increases in PH and decreases in r were observed for nonalkanol lipid anesthetics. The effects of n-alkanols on the Na+-H+ antiporter and on osmotically driven water transport were also studied. At concentrations of n-alkanol that resulted in a 10-fold increase in PH, there was no significant effect on either Na+-H+ exchange or water transport. These results suggest a lipid pathway for brush border H+ diffusion that is distinct from both the Na+-H+ antiporter and the water transport pathway.

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39

Frey, Shelli L., Eva Y. Chi, Jaroslaw Majewski, Kristian Kjaer, and Ka Yee C. Lee. "Condensing And Fluidizing Effects Of Structurally Related Gangliosides On Phospholipid Films." Biophysical Journal 96, no. 3 (February 2009): 449a. http://dx.doi.org/10.1016/j.bpj.2008.12.2306.

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40

Ogata, Koichiro, Tomoya Furukawa, and Yusuke Yamamoto. "Fluidized powder conveying in a horizontal rectangular channel using fluidizing air." Advanced Powder Technology 23, no. 6 (November 2012): 761–70. http://dx.doi.org/10.1016/j.apt.2011.10.005.

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41

Bardonnet, Pierre-Louis, Vincent Faivre, Fabrice Pirot, Paul Boullanger, and Françoise Falson. "Cholesteryl oligoethyleneglycol glycosides: Fluidizing effect of their embedment into phospholipid bilayers." Biochemical and Biophysical Research Communications 329, no. 4 (April 2005): 1186–92. http://dx.doi.org/10.1016/j.bbrc.2005.02.092.

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42

Mele, Jernej, and Andrej Senegacnik. "Design of a Fast Internal Circulating Fluidized-Bed Gasifier with a conical bed angle." Thermal Science 23, no. 1 (2019): 33–45. http://dx.doi.org/10.2298/tsci161129171m.

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The main purpose of a fast internal circulating fluidized bed gasifier is the steam reforming of solid organic matter, like biomass, to a nearly nitrogen-free syngas. The calorific value of this syngas is approximately three times higher than the gas from common air-driven gasifiers. This article deals with a study of the particle dynamics in a 1 MWt fast internal circulating fluidized bed plant and focuses on the design of the gasification reactor?s geometry. Superheated steam is used for the fluidization and gasification in the reactor. The gasification of solid fuels causes an increase in the volume flow of the fluidizing gas and at the same time also a change in the fluidization regime. Approaching a turbulent fluidization regime or even fast fluidization is not desirable. However, with the proper design of reactor, i. e., an appropriately conical bed angle, suitable gasification conditions in the form of a fluidizing regime can be achieved across the entire height of the bed. For the purposes of the experimental research, a semi-industrial unit was set-up. The process was designed and experimentally tested on a lab-scale, cold-flow model and scaled-up to a semi-industrial process. The guidelines for designing the geometry of the gasification reactor were set.

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43

Pak, Daewon, and Wonseok Chang. "Decolorizing Dye Wastewater with Low Temperature Catalytic Oxidation." Water Science and Technology 40, no. 4-5 (August 1, 1999): 115–21. http://dx.doi.org/10.2166/wst.1999.0582.

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Novel oxidation technology to decolorize dye wastewater was discussed and the feasibility of color removal with Fe/MgO catalyst fluidizing in a reactor under continuous flow was demonstrated at room temperature. In batch tests, the oxidation reaction of reactive and disperse dye with an oxidizing agent, hydrogen peroxide, in the presence of Fe/MgO catalyst was performed. Through the catalytic oxidation, dyes were oxidized to molecules with lower molecular weight and then mineralized based on TOC analysis. The influence of hydrogen peroxide and catalyst dosage on the catalytic oxidation rate was verified. The catalytic oxidation rate increased with increasing hydrogen peroxide and catalyst dosage. Fe/MgO catalyst fluidizing in the reactor operated at room temperature was tested to decolorize the wastewater from a dye manufacturing industry. In the fluidized bed reactor, the wastewater was completely decolorized and about 30% of COD removal was obtained during 30 days of operation. Organic matters were degraded and part of them mineralized by the catalytic oxidation. BOD/COD ratio of the effluent from the fluidized bed reactor was increased compared to that of the influent. After 30 days of operation, the effluent from the fluidized bed reactor started becoming yellowish. COD and residual hydrogen peroxide concentration in the effluent started to increase due to the catalyst losing its activity.

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44

Azeem, Babar, Kuzilati KuShaari, Muhammad Naqvi, Lau Kok Keong, Mohammed Khaloofah Almesfer, Zakaria Al-Qodah, Salman Raza Naqvi, and Noureddine Elboughdiri. "Production and Characterization of Controlled Release Urea Using Biopolymer and Geopolymer as Coating Materials." Polymers 12, no. 2 (February 10, 2020): 400. http://dx.doi.org/10.3390/polym12020400.

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Synthetic polymers-based controlled release urea (CRU) leaves non-biodegradable coating shells when applied in soil. Several alternative green materials are used to produce CRU, but most of these studies have issues pertaining to nitrogen release longevity, process viability, and the ease of application of the finished product. In this study, we utilized tapioca starch, modified by polyvinyl alcohol and citric acid, as coating material to produce controlled release coated urea granules in a rotary fluidized bed equipment. Response surface methodology is employed for studying the interactive effect of process parameters on urea release characteristics. Statistical analysis indicates that the fluidizing air temperature and spray rate are the most influential among all five process parameters studied. The optimum values of fluidizing air temperature (80 °C), spray rate (0.13 mL/s), atomizing pressure (3.98 bar), process time (110 min), and spray temperature (70 °C) were evaluated by multi-objective optimization while using genetic algorithms in MATLAB®. Urea coated by modified-starch was double coated by a geopolymer to enhance the controlled release characteristics that produced promising results with respect to the longevity of nitrogen release from the final product. This study provides leads for the design of a fluidized bed for the scaled-up production of CRU.

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45

Khan, Wasi Z., Bernard M. Gibbs, and Assem Ayaganova. "Emissions of SO3 from a Coal-Fired Fluidized Bed under Normal and Staged Combustion." ISRN Environmental Chemistry 2013 (May 12, 2013): 1–7. http://dx.doi.org/10.1155/2013/514751.

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This paper reports the measurements of SO3 emissions with and without limestone under unstaged and staged fluidized-bed combustion, carried out on a m2 and 2 m high stainless-steel combustor at atmospheric pressure. The secondary air was injected 100 cm above the distributor. SO3 emissions were monitored for staging levels of 85 : 15, 70 : 30, and 60 : 40, equivalent to a primary air/coal ratio (PACR) of ~0.86, 0.75, and 0.67. Experiments were carried out at 0%–60% excess air level, 1-2 m/s fluidizing velocity, 800–850°C bed temperature, and 20–30 cm bed height. During unstaged combustion runs, SO3 emissions were monitored for a wide range of Ca/S ratios from 0.5 to 13. However, for the staged combustion runs, the Ca/S ratio was fixed at 3. SO3 was retained to a lesser extent than SO2, suggesting that SO2 reacts preferentially with CaO and that SO3 is involved in the sulphation process to a lesser degree. The SO3 emissions were found to be affected by excess air, whereas the fluidizing velocity and bed temperature had little effect. SO3 was depressed on the addition of limestone during both the staged and unstaged operations, and the extent of the reduction was higher under staged combustion.

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46

Bai, Chenxi, Yao Xiao, Ruifeng Peng, John Grace, and Yumin Chen. "Analysis of the Hydrodynamic Effects of Gas Permeation in a Pilot-Scale Fluidized Bed Membrane Reactor." Applied Sciences 9, no. 1 (December 25, 2018): 67. http://dx.doi.org/10.3390/app9010067.

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This study experimentally investigates the effects of gas extraction/addition, via multiple vertical membrane panels, on the hydrodynamics in different regions of a pilot-scale gas fluidized bed membrane reactor (FBMR), based on differential pressure signals measured at different vertical bed sections at high temperature. In a bed section where membrane panels were installed and activated, the extraction of gas caused the average bubble size to increase, but decreased the number of small- and medium-sized bubbles. This effect of gas extraction penetrated into bed sections above the active membrane panel, but attenuated with increasing distance away from the extraction location. The attenuation rate was much faster in FBMR with lower bed voidage, mainly due to the large decrease of the drag force exerted by gas extraction on fluidizing gas in a denser bed. With the same inlet gas velocity, gas addition favored the growth of bubbles, especially in the upper bed sections compared with operation without gas permeation. The increase of the effective fluidizing velocity was the major reason for the increase of the bubble size during gas addition. These findings preliminarily suggest that membrane units should not be installed in or below fast-reacting zones in a scale-up FBMR, and operation with a lower bed voidage is preferable to avoid the formation of large bubbles enhanced by gas extraction.

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47

Krzywanski, Jaroslaw, Karolina Grabowska, Marcin Sosnowski, Anna Zylka, Anna Kulakowska, Tomasz Czakiert, Karol Sztekler, Marta Wesolowska, and Wojciech Nowak. "Heat transfer in fluidized and fixed beds of adsorption chillers." E3S Web of Conferences 128 (2019): 01003. http://dx.doi.org/10.1051/e3sconf/201912801003.

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An innovative idea, shown in the paper constitutes in the use of the fluidized bed of sorbent, instead of the conventional, fixed-bed, commonly used in the adsorption chillers. Bed–to–wall heat transfer coefficients for fixed and fluidized beds of adsorbent are determined. Sorbent particles diameters and velocities of fluidizing gas are discussed in the study. The calculations confirmed, that the bed–to–wall heat transfer coefficient in the fluidized bed of adsorbent is muchhigher than that in a conventional bed.

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48

KAWAGUCHI, Toshio, Hiroshi KIMURA, and Toshihisa WAKASUGI. "Effects of bed shape on fluidizing characteristics in vinyl acetate synthesis reactor." Journal of The Japan Petroleum Institute 29, no. 4 (1986): 289–94. http://dx.doi.org/10.1627/jpi1958.29.289.

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49

Santos, A. "Oxidative coupling of methane in a vibrofluidized bed at low fluidizing velocities." International Journal of Multiphase Flow 22 (December 1996): 112. http://dx.doi.org/10.1016/s0301-9322(97)88289-4.

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50

Nakahara, Hiromichi. "Fluidizing and Solidifying Effects of Perfluorooctylated Fatty Alcohols on Pulmonary Surfactant Monolayers." Journal of Oleo Science 65, no. 2 (2016): 99–109. http://dx.doi.org/10.5650/jos.ess15222.

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