Experiment and 3D simulation of slugging regime in a circulating fluidized bed

Amornsirirat, Cholthicha; Chalermsinsuwan, Benjapon; Mekasut, Lursuang; Kuchonthara, Prapan; Piumsomboon, Pornpote

doi:10.1007/s11814-010-0407-0

Cited by 8 publications

(4 citation statements)

References 15 publications

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“…4 illustrates a typical velocity vector field obtained for the 750‐g bed of 2900‐µm spherical particles at superficial air velocity of 2 m s −1 . Understanding of the velocity profile of particles in an SFB may be a useful tool in designing and operating an efficient fluidization system 8. Despite their importance, experimental studies on particle velocity in SFBs are scarce.…”

Section: Resultsmentioning

confidence: 99%

“…5 a, it is shown that the highest particle velocity occurred near the cone or midway between the cone and the bed column wall. However, different patterns of velocity profile could be obtained depending on the superficial air velocity 7–10. Tab.…”

Section: Resultsmentioning

confidence: 99%

“…The SFB minimizes the fluid's momentum in the axial direction and transfers it to the tangential and radial directions 6, 7. As a result, it provides excellent particle mixing, reduces elutriation, allows application of a wide range of particle sizes, and lowers the pressure drop 8.…”

Section: Introductionmentioning

confidence: 99%

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Particle Image Velocimetry of a Swirling Fluidized Bed at Different Blade Angles

et al. 2016

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The particle motion within a stable swirling operation regime of a fluidized bed is investigated. Particle image velocimetry was used to elaborate the hydrodynamics of multi-sized particles fluidized at different air distributor blade angles. The experimental results revealed that the superficial velocity is the most prominent aspect affecting the hydrodynamics of a swirling fluidized bed (SFB) followed by the bed weight, particle shape, and blade inclination angle. Particles of different sizes and shapes fluidized well in the SFB which emphasizes its superiority over contemporary techniques. The slug-wavy regime in the SFB is promising and has considerable potential, especially for diffusion-controlled reactions and processes in the industry. The particle velocity increased with air flow rate at shallow bed height but decreased with bed weight.

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Section: Resultsmentioning

confidence: 99%

Section: Resultsmentioning

confidence: 99%

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Particle Image Velocimetry of a Swirling Fluidized Bed at Different Blade Angles

et al. 2016

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“…The known conventional beds are centrifugal fluidized beds, circulating fluidized beds, vibro-fluidized beds, tapered fluidized beds, spouted fluidized beds, etc. (Amornsirirat et al, 2011). The fluidized beds are being used in combustion, gasification, drying, heating and catalytic cracking, surface treatment, surface coating, gas separation, mass transfer, etc.…”

Section: Introductionmentioning

confidence: 99%

Image velocimetry and statistical analysis of a mesh-coupled axial blade distributor for mass transfer in a swirling bed

Javed¹,

Shukrullah²,

Naz³

et al. 2020

Journal of Theoretical and Applied Mechanics

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A mesh-coupled axial blade distributor was tested for fluidization of particles in a swirling fluidized bed. The bed velocity was estimated experimentally using a high-speed imaging device and MATLAB supported particle image velocimetry (PIV). The bed velocity was also predicted statistically with a response surface analysis method. During statistical analysis, the confidence interval of bed velocity remained between 0.49485 and 0.49998. The bed velocity was measured about 0.49741 m/s and 0.538 m/s through experimental and statistical methods, respectively. The experimental and statistical analysis revealed similar bed weights and superficial velocities with a slight difference of 6.4 • in blade angles.

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Heat transfer in a swirling fluidized bed with geldart type-D particles

Mohideen

Sreenivasan

Sulaiman

et al. 2012

Korean J. Chem. Eng.

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The wall-tekd heat transfer coefficients were measued by fixing a thin constaztan foil heater on the bed wall. Thermocouples located at diffemt heigh~s on the foil show a decrease in the wall heat transfer coefficient with bed height It was seen that only a discrete particle model which accounts for the conduction between the particle and the heat transfer s h c e and the gaxonvective augmentation can adequately represent the mechanism ofheat transfer in the swuline, fluidized bed. As the jet of gas enters the bed at a certain small angle, 8, to the horizantal plane, the jet will have two componentF ofvelocity. The vatical component of the jet yelocity, wlich is given by V sin 8, will mate fluididon ofmticles, while the h h t a l c o m m a V cos 8, will cmte s\v%kg [4]. The dish7iitor used in this bed ~i~. 1. ~~~i~ ofa swirling fluidized bed, consists of overlapping blades that are truncated sectors of a circle forming an mular region for gas flow The wne in the centn. of the bed avoiak a dead zone while graduaUy inueasing the 8oss-Many of the early works on wall-bed heat k f e r in fluidized sectional area of gas flow to the fRe nubx abve the bed beds held tha[ theprhcipal resiskce to heathsfer is a fluid film and that moving fluid&d pahcles acting as ttnin~lence promoters ' To whom corresnandence should be addressed.sw1u the 6lm to reduce the resistrmce. Ihe solid particle-surface

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Experiment and 3D simulation of slugging regime in a circulating fluidized bed

Cited by 8 publications

References 15 publications

Particle Image Velocimetry of a Swirling Fluidized Bed at Different Blade Angles

Particle Image Velocimetry of a Swirling Fluidized Bed at Different Blade Angles

Image velocimetry and statistical analysis of a mesh-coupled axial blade distributor for mass transfer in a swirling bed

Heat transfer in a swirling fluidized bed with geldart type-D particles

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