Process aspects of three-phase inverse fluidized bed bioreactor: A review

Sur, Dharmesh H.; Mukhopadhyay, Mausumi

doi:10.1016/j.jece.2017.06.052

Cited by 24 publications

(4 citation statements)

References 47 publications

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“…Gas–liquid–solid three‐phase fluidization system is extensively used in environmental engineering, petrochemical, pharmaceutical, and biochemical fields because of its excellent mass and heat transfer efficiency. [ 1–3 ] Research on three‐phase fluidized bed include experimental and numerical methods. Due to three‐phase flow's complication, numerical simulation presents advantages in revealing flow details, which to a large extent can replace the expensive experiments.…”

Section: Introductionmentioning

confidence: 99%

“…The former system is defined as a bubble‐induced gas–liquid–solid fluidized bed, and the latter is termed a bubble‐driven gas–liquid–solid fluidized bed. These two kinds of fluidized systems consume less energy than the traditional heavy particle fluidized bed [ 19 ] and have broad application prospect in sewage treatment, [ 2 ] microbial fermentation, [20 ] and other fields. [ 21 ] Recently, Liu et al reported a research on the flow of polyethylene particles in a bubble‐induced inverse three‐phase fluidized bed.…”

Section: Introductionmentioning

confidence: 99%

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Euler multiphase‐CFD simulation on a bubble‐driven gas–liquid–solid fluidized bed

2022

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An integrated flow model was developed to simulate the fluidization hydrodynamics in a new bubble‐driven gas–liquid–solid fluidized bed using the computational fluid dynamic (CFD) method. The results showed that axial solids holdup is affected by grid size, bubble diameter, and the interphase drag models used in the simulation. Good agreements with experimental data could be obtained by adopting the following parameters: 5 mm grid, 1.2 mm bubble diameter, the Tomiyama gas–liquid model, the Schiller–Naumann liquid–solid model, and the Gidaspow gas–solid model. At full fluidization state, an internal circulation of particles flowing upward near the wall and downward in the centre is observed, which is in the opposite direction compared with the traditional core‐annular flow structure in a gas–solid fluidized bed. The simulated results are very sensitive to bubble diameters. Using smaller bubble diameters would lead to excessive liquid bed expansions and more solid accumulated at the bottom due to a bigger gas–liquid drag force, while bigger bubble diameters would result in a higher solid bed height caused by a smaller gas–solid drag force. Considering the actual bubble distribution, population balance model (PBM) is employed to characterize the coalescence and break up of bubbles. The calculated bubble diameters grow up from 2–4 mm at the bottom to 5–10 mm at the upper section of the bed, which are comparable to those observed in experiments. The simulation results could provide valuable information for the design and optimization of this new type of fluidized system.

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Section: Introductionmentioning

confidence: 99%

Section: Introductionmentioning

confidence: 99%

Euler multiphase‐CFD simulation on a bubble‐driven gas–liquid–solid fluidized bed

2022

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“…Minimum fluidization velocity and pressure drops will also depend on the shape of beds used for the experiments [6]. Generally, parameters like hydraulic retention time, bio-carriers, reactor aspect ratio, superfacial gas velocity, superficial liquid velocity, bed expansion, and mass transfer coefficient affect the performance of a three-phase fluidized-bed bioreactor (TPIFB) [7]. The biofilm bed porosity depends on different flow rates and shape of the particles [8].…”

Section: Introductionmentioning

confidence: 99%

Effect of temperature and apparent liquid viscosity on the hydrodynamics of liquid–solid tapered inverse fluidized bed: experimental studies compared with empirical models

Upender

Kishore

2020

SN Appl. Sci.

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In the present work, immersed heater to bed heat transfer coefficient and related hydrodynamics were determined along with different angles (7.85 and 6.8) of the tapered inversed fluidized bed. Carboxyl methylcellulose was used to change the water viscosity by using a power-law model. The hydrodynamics was compared for two different angles of beds. Furthermore, minimum fluidization velocities were carried out for different liquid apparent viscosities and different angles of beds and compared with previous models. The heat transfer coefficient was found to be increasing with liquid velocity and bed voidage, respectively, and it was also found that the bed voidage is high for a high diameter of particles. The correlation was developed between the bed expansion ratio and independent parameters by response surface methodology in design expert software v.9.

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“…Inverse three-phase fluidization is more efficient when applied for biological aerobic treatment (Sur and Mukhopadhyay 2017b;Nikolov and Karamanev 1987). When the fluidized bed expands downwards-against the net buoyancy force of the particles-it is termed as the inverse fluidized bed.…”

Section: Introductionmentioning

confidence: 99%

Process parametric study for COD removal of electroplating industry effluent

Sur

Mukhopadhyay

2018

3 Biotech

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This paper investigated the effects of parameters, like inoculum size (15, 10 and 5% of the working volume of the reactor), gas velocities (0.0027, 0.00342 and 0.0068 m/s), bed heights (0.3, 0.6 and 0.9 m), static bed heights (4.85 and 2.43 cm), sizes of solid media particles (12, 4 mm), and the height to diameter ratio (/: 0.25 and 0.5) onto COD reduction process for electroplating effluent (initial COD values: 1140 ppm) using and. The authors derived simple mathematical correlations representing the entire COD reduction process. The correlation between the inoculum volume and gas velocities was in the form of an equation = + +, as deduced from nonlinear regressions. The correlations were validated, and percentage errors were found out to infer the effects of all parameters in the COD reduction process. The maximum COD reduction was achieved to 28.30 ppm (97.52%), in a batch mode, at 10% inoculum size, 0.0027 m/s low gas velocity and a static bed height of 2.43 cm.

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Process aspects of three-phase inverse fluidized bed bioreactor: A review

Cited by 24 publications

References 47 publications

Euler multiphase‐CFD simulation on a bubble‐driven gas–liquid–solid fluidized bed

Euler multiphase‐CFD simulation on a bubble‐driven gas–liquid–solid fluidized bed

Effect of temperature and apparent liquid viscosity on the hydrodynamics of liquid–solid tapered inverse fluidized bed: experimental studies compared with empirical models

Process parametric study for COD removal of electroplating industry effluent

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