Determination of the mixing coefficient in a fluidized bed reactor

1965 ◽  
Vol 8 (5) ◽  
pp. 427-430
Author(s):  
I. A. Burovoi ◽  
G. I. Svetozarova
Keyword(s):  
Fluidized Bed ◽  
Fluidized Bed Reactor ◽  
Mixing Coefficient

Design and Startup of an Anaerobic Fluidized Bed Reactor

1999 ◽  
Vol 40 (8) ◽  
pp. 63-70 ◽  
Author(s):  
P. Marín ◽  
D. Alkalay ◽  
L. Guerrero ◽  
R. Chamy ◽  
M. C. Schiappacasse
Keyword(s):  
Fluidized Bed ◽  
Hydraulic Retention Time ◽  
Fluidized Bed Reactor ◽  
Gas Production ◽  
Beach Sand ◽  
Organic Load ◽  
Load Rate ◽  
Anaerobic Fluidized Bed Reactor ◽  
Bed Expansion

A 10 1 anaerobic fluidized bed reactor (AFBR) was designed and constructed, using beach sand as the solid support for the biomass. Considering the complexity of this type of system, previously to the startup, several experiences were performed in a series of minireactors, such as: determination of the bed expansion and the feed distribution. The startup was made increasing gradually the organic load rate (OLR), using the alkalinity ratio (α) and the removal of the organic load, as mg/l of COD, as leading parameters. The system attained a COD removal of over 85%, for an OLR of 3.4 [kg COD/m3·d]. The best removal of 92% was obtained at an OLR of 1.04 [kg COD/m3·d], with a hydraulic retention time (HRT) of 12 hours. The best gas production of 1.8 [m3 of biogas/m3·d], equivalent to a production of 0.16 [m3/kg CODremoved], was obtained at an (HRT) of 4.8 hours. The best startup results were obtained using Ethanol as the Carbon source.

Determination of optimal biofilm activity in a biological fludized bed (BFB) reactor

1994 ◽  
Vol 29 (10-11) ◽  
pp. 347-351 ◽  
Author(s):  
B. Ruggeri ◽  
G. Caire ◽  
V. Specchia ◽  
G. Sassi ◽  
F. Bosco ◽  
...  
Keyword(s):  
Mass Transfer ◽  
Fluidized Bed ◽  
Experimental Tests ◽  
Fluidized Bed Reactor ◽  
Solid Mass ◽  
Specific Biomass ◽  
Biomass Activity ◽  
Reaction Regime ◽  
Bed Expansion

Experimental tests were carried out in order to ascertain the biomass activity in a biological fluidized bed reactor. A semi-pilot fluidized bed reactor was used with two different supports (sand and glass particles). The specific biomass activity was followed during the tests. It reached a maximum and after declined vs. biomass hold up and bed expansion. The results clearly put in evidence as the activity is strongly effected by liquid-solid mass transfer and support roughness which in turn determines the compactness of biofilm and its diffusive properties. By controlling the bed expansion it is possible to decide the macro reaction regime of work: external mass transfer, biokinetics or diffusive control according to incoming substrate concentration, in order to maximize the bioreactor performance.

Removal of microcystin-LR from drinking water with TiO2-coated activated carbon

2004 ◽  
Vol 4 (5-6) ◽  
pp. 21-28
Author(s):  
S.-C. Kim ◽  
D.-K. Lee
Keyword(s):  
Drinking Water ◽  
Activated Carbon ◽  
Synergistic Effect ◽  
Fluidized Bed ◽  
Continuous Flow ◽  
High Surface ◽  
High Surface Area ◽  
Fluidized Bed Reactor ◽  
Exterior Surface ◽  
Tio2 Particles

TiO2-coated granular activated carbon was employed for the removal of toxic microcystin-LR from water. High surface area of the activated carbon provided sites for the adsorption of microcystin-LR, and the adsorbed microcystin-LR migrated continuously onto the surface of TiO2 particles which located mainly at the exterior surface in the vicinity of the entrances of the macropores of the activated carbon. The migrated microcystin-LR was finally degraded into nontoxic products and CO2 very quickly. These combined roles of the activated carbon and TiO2 showed a synergistic effect on the efficient degradation of toxic microcystin-LR. A continuous flow fluidized bed reactor with the TiO2-coated activated carbon could successfully be employed for the efficient photocatalytic of microcystin-LR.

Influence of Seeding Conditions on Initial Biofilm Development during the Startup of Anaerobic Fluidized Bed Reactors

1989 ◽  
Vol 21 (4-5) ◽  
pp. 157-165 ◽  
Author(s):  
F. Ehlinger ◽  
J. M. Audic ◽  
G. M. Faup
Keyword(s):  
Fluidized Bed ◽  
Future Development ◽  
Protein Concentration ◽  
Specific Activity ◽  
Fluidized Bed Reactor ◽  
Fluidized Bed Reactors ◽  
Support Material ◽  
Biofilm Development ◽  
Initial Biofilm

The characterization of the biofilm of an anaerobic fluidized-bed reactor was completed under standard conditions. The distribution of the fixed protein concentration depended on the level in the reactor. The protein concentration reached 1520 µg.g−1 of support at the top of the reactor and only 1200 µg.g−1 at the bottom after 504 hours of operation but the specific activity of the biofilm was 33×10−4 µM acetate.h−1.mg−1 proteins at the bottom and only 26×10−4 µM.h−1.mg−1 at the top. The efficiency of a fluidized bed reactor and the composition of the biofilm changed with an increase of the pH from 7 to 8.5 during the seeding of the support material. Future development of the biofilm and the specific activity of the support were affected.

The Kinetics of Glucose Decomposition with Sulfate Reduction in the Anaerobic Fluidized Bed Reactor

1993 ◽  
Vol 28 (2) ◽  
pp. 135-144 ◽  
Author(s):  
S. Matsui ◽  
R. Ikemoto Yamamoto ◽  
Y. Tsuchiya ◽  
B. Inanc
Keyword(s):  
Sulfate Reduction ◽  
Fluidized Bed ◽  
Kinetic Equations ◽  
Fluidized Bed Reactor ◽  
Order Reaction ◽  
First Order Reaction ◽  
First Order ◽  
Glucose Decomposition ◽  
Reaction Equations ◽  
Kinetics Of

Using a fluidized bed reactor, experiments on glucose decomposition with and without sulfate reduction were conducted. Glucose in the reactor was mainly decomposed into lactate and ethanol. Lactate was mainly decomposed into propionate and acetate, while ethanol was decomposed into propionate, acetate, and hydrogen. Sulfate reduction was not involved in the decomposition of glucose, lactate, and ethanol, but was related to propionate and acetate decomposition. The stepwise reactions were modeled using either a Monod expression or first order reaction kinetics in respect to the reactions. The coefficients of the kinetic equations were determined experimentally. The modified Monod and first order reaction equations were effective at predicting concentrations of glucose, lactate, ethanol, propionate, acetate, and sulfate along the beight of the reactor. With sulfate reduction, propionate was decomposed into acetate, while without sulfate reduction, accumulation of propionate was observed in the reactor. Sulfate reduction accelerated propionate conversion into acetate by decreasing the hydrogen concentration.

Biological granulated activated carbon fluidized bed reactor for atrazine remediation

2004 ◽  
Vol 49 (11-12) ◽  
pp. 215-222 ◽  
Author(s):  
M. Herzberg ◽  
C.G. Dosoretz ◽  
S. Tarre ◽  
M. Beliavski ◽  
M. Green
Keyword(s):  
Fluidized Bed ◽  
Fluidized Bed Reactor ◽  
Batch Adsorption ◽  
Pseudomonas Sp ◽  
Partial Penetration ◽  
Biofilm Carrier ◽  
Degradation Rates ◽  
Degrading Bacteria ◽  
Atrazine Degradation ◽  
Granulated Activated Carbon

To show that an adsorbing biofilm carrier (GAC) can be advantageous for atrazine bioremediation over a non-adsorbing carrier, fluidized bed (FB) reactors were operated under atrazine limiting concentrations using Pseudomonas sp. strain ADP as the atrazine degrading bacteria. The following interrelated subjects were investigated: 1) atrazine adsorption to GAC under conditions of atrazine partial penetration in the biofilm, 2) differences in atrazine degradation rates and 3) stability of atrazine biodegradation under non-sterile anoxic conditions in the GAC reactor versus a reactor with a non-adsorbing biofilm carrier. Results from batch adsorption tests together with modeling best described the biofilm as patchy in nature with covered and non-biofilm covered areas. Under conditions of atrazine partial penetration in the biofilm, atrazine adsorption occurs in the non-covered areas and is consequently desorbed at the base of the biofilm substantially increasing the active biofilm surface area. The double flux of atrazine to the biofilm in the GAC reactor results in lower effluent atrazine concentrations as compared to a FB reactor with a non-adsorbing carrier. Moreover, under non-sterile denitrification conditions, atrazine degradation stability was found to be much higher (several months) using GAC as a biofilm carrier while non-adsorbing carrier reactors showed sharp deterioration within 30 days due to contamination of non-atrazine degrading bacteria.

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