Aerobic biodegradation of a mixture of sulfonated azo dyes by a bacterial consortium immobilized in a two‐stage sparged packed‐bed biofilm reactor

The biodegradation of the sulfonated azo dyes, Acid Orange 7 (AO7) and Acid Red 88 (AR88), by a bacterial consortium isolated from water and soil samples obtained from sites receiving discharges from textile industries, was evaluated. For a better removal of azo dyes and their biodegradation byproducts, an aerobically operated two‐stage rectangular packed‐bed biofilm reactor (2S‐RPBR) was constructed. Because the consortium's metabolic activity is affected by oxygen, the effect of the interstitial air flow rate Q_GI on 2S‐RPBR's zonal values of the oxygen mass transfer coefficient k_La was estimated. In the operational conditions probed in the bioreactor, the k_La values varied from 3 to 60 h^?1, which roughly correspond to volumetric oxygen transfer rates, dc_L/dt, ranging from 20 to 375 mg O₂ L^?1h^?1. Complete biodegradation of azo dyes was attained at loading rates B_V,AZ up to 40 mg L^?1d^?1. At higher B_V,AZ values (80 mg L^?1 d^?1), dye decolorization and biodegradation of the intermediaries 4‐amino‐naphthalenesulphonic acid (4‐ANS) and 1‐amino‐2‐naphthol (1‐A2N) was almost complete. However, a diminution in COD and TOC removal efficiencies was observed in correspondence to the 4‐aminobenzenesulfonic acid (4‐ABS) accumulation in the bioreactor. Although the oxygen transport rate improved the azo dye mineralization, the results suggest that the removal efficiency of azo dyes was affected by biofilm detachment at relatively high Q_GI and B_V,AZ values. After 225 days of continuous operation of the 2S‐RFBR, eight bacterial strains were isolated from the biofilm attached to the porous support. The identified genera were: Arthrobacter, Variovorax, Agrococcus, Sphingomonas, Sphingopyxis, Methylobacterium, Mesorhizobium, and Microbacterium.     

Bacterial decolorization and degradation of azo dyes

Azo compounds constitute the largest and the most diverse group of synthetic dyes and are widely used in a number of industries such as textile, food, cosmetics and paper printing. They are generally recalcitrant to biodegradation due to their xenobiotic nature. However microorganisms, being highly versatile, have developed enzyme systems for the decolorization and mineralization of azo dyes under certain environmental conditions. Several genera of Basidomycetes have been shown to mineralize azo dyes. Reductive cleavage of azo bond, leading to the formation of aromatic amines, is the initial reaction during the bacterial metabolism of azo dyes. Anaerobic/anoxic azo dye decolorization by several mixed and pure bacterial cultures have been reported. Under these conditions, this reaction is non-specific with respect to organisms as well as dyes. Various mechanisms, which include enzymatic as well as low molecular weight redox mediators, have been proposed for this non-specific reductive cleavage. Only few aerobic bacterial strains that can utilize azo dyes as growth substrates have been isolated. These organisms generally have a narrow substrate range. Degradation of aromatic amines depends on their chemical structure and the conditions. It is now known that simple aromatic amines can be mineralized under methanogenic conditions. Sulfonated aromatic amines, on the other hand, are resistant and require specialized aerobic microbial consortia for their mineralization. This review is focused on the bacterial decolorization of azo dyes and mineralization of aromatic amines, as well as the application of these processes for the treatment of azo-dye-containing wastewaters.     

Autotrophic denitrification by Thiobacillus denitrificans in a packed bed reactor

Summary An upflow packed bed reactor with lava stones as support for the microbial growth proved to be very useful for the denitrification of industrial waste water by Thiobacillus denitrificans. The application of the plug flow principle allowed higher concentrations of nitrate to be employed than in a stirred tank reactor because inhibitory concentrations of sulfate from thiosulfate oxidation built up only in the upper part of the column — if at all. In experiments with synthetic media nitrate solutions of different strength (NO ₃ ^– g/l: 1.8; 3.0; 4.3; 6.1) were tested, each at 5 different residence times (5; 3.3; 2.5; 2.0; 1.7 h). The combination of the two parameters which still allowed 95% denitrification was 3 g NO ₃ ^- /l and 2.5 h residence time; this corresponded to a volumetric nitrate loading of about 25 kg/m³·d. Higher nitrate loadings led to incomplete denitrification coupled with the occurence of nitrite in the outflow. Below the critical loading rate nitrite accumulated only in the lower part of the column and was then gradually reduced. Experiments with simulated middle active waste from processing nuclear fuel which contained numerous heavy metals yielded similar results. — Although pure inorganic media were fed into the reactor the microflora developing as a dense layer covering the lava stones consisted not only of T. denitrificans but also of heterotrophic denitrifiers, mainly Pseudomonas aeruginosa.     

Toxicity assessment and microbial degradation of azo dyes

Toxic effluents containing azo dyes are discharged from various industries and they adversely affect water resources, soil fertility, aquatic organisms and ecosystem integrity. They pose toxicity (lethal effect, genotoxicity, mutagenicity and carcinogenicity) to aquatic organisms (fish, algae, bacteria, etc.) as well as animals. They are not readily degradable under natural conditions and are typically not removed from waste water by conventional waste water treatment systems. Benzidine based dyes have long been recognized as a human urinary bladder carcinogen and tumorigenic in a variety of laboratory animals. Several microorganisms have been found to decolourize, transform and even to completely mineralize azo dyes. A mixed culture of two Pseudomonas strains efficiently degraded mixture of 3-chlorobenzoate (3-CBA) and phenol/cresols. Azoreductases of different microorganisms are useful for the development of biodegradation systems as they catalyze reductive cleavage of azo groups (-N=N-) under mild conditions. In this review, toxic impacts of dyeing factory effluents on plants, fishes, and environment, and plausible bioremediation strategies for removal of azo dyes have been discussed.     

The microbial degradation of azo dyes: minireview

The removal of dyes in wastewater treatment plants still involves physical or chemical processes. Yet numerous studies currently exist on degradation based on the use of microbes—which is a well-studied field. However progress in the use of biological methods to deal with this environmentally noxious waste is currently lacking. This review focuses on the largest dye class, that is azo dyes and their biodegradation. We summarize the bacteria identified thus far which have been implicated in dye decolorization and discuss the enzymes involved and mechanisms by which these colorants are broken down.     

Time dependent degradation of mixture of structurally different azo and non azo dyes by using Galactomyces geotrichum MTCC 1360

Galactomyces geotrichum MTCC 1360, a yeast species showed 88% ADMI (American dye manufacturing institute) removal of mixture of structurally different dyes (Remazol red, Golden yellow HER, Rubine GFL, Scarlet RR, Methyl red, Brown 3 REL, Brilliant blue) (70 mg l⁻¹) within 24 h at 30 °C and pH 7.0 under shaking condition (120 rpm). Glucose (0.5%) as a carbon source was found to be more effective than other sources used. The medium with metal salt (CaCl₂, ZnSO₄, FeCl₃, MgCl₂, CuSO₄) (0.5 mM) showed less ADMI removal as compared to control, but did not inhibit complete decolorization. The presence of tyrosinase, NADH-DCIP reductase and induction in laccase activity during decolorization indicated their role in degradation. HPTLC (High performance thin layer chromatography) analysis revealed the removal of individual dyes at different time intervals from dye mixture, indicating preferential degradation of dyes. FTIR (Fourier transform infrared spectroscopy) and HPLC (High performance liquid chromatography) analysis of samples before and after decolorization confirmed the biotransformation of dye. The reduction of COD (Chemical oxygen demand) (69%), TOC (Total organic carbon) (43%), and phytotoxicity study indicated the conversion of complex dye molecules into simpler oxidizable products having less toxic nature.     

Butanol production by Clostridium acetobutylicum in a continuous packed bed reactor

In this study, we report on a butanol production process by immobilized Clostridium acetobutylicum in a continuous packed bed reactor (PBR) using Tygon^® rings as a carrier. The medium was a solution of lactose (15–30 g/L) and yeast extract (3 g/L) to emulate the cheese whey, an abundant lactose-rich wastewater. The reactor was operated under controlled conditions with respect to the pH and to the dilution rate. The pH and the dilution rate ranged between 4 and 5, the dilution rate between 0.54 and 2.4 h^?1 (2.5 times the maximum specific growth rate assessed for suspended cells). The optimal performance of the reactor was recorded at a dilution rate of 0.97 h^?1: the butanol productivity was 4.4 g/Lh and the selectivity of solvent in butanol was 88%_w.     

Phenol removal in packed bed reactor under denitrifying conditions

Detailed studies on the efficiency of phenol degradation by a biofilm in an anaerobic packed bed reactor were carried out. The efficiency of phenol degradation depended on both the concentration of phenol in the medium and the phenol load in anaerobic packed bed reactor. Increasing phenol concentrations from 200 to 1,250 mg l(-1) and retention time (Tr)= 12 h were paralleled by increasing efficiency of the process, which reached a maximum value of 1,390 mg l(-1) day(-1) at 700 mg phenol l(-1). The highest concentration of phenol used inhibited growth by approximately 95%. When the phenol load in medium containing 200, 300, 400 and 500 mg l(-1) was increased through a shortening of the retention time (Tr from 24 to 2 h) a maximum efficiency of phenol degradation of 2,200 mg l(-1) day(-1) was obtained at Tr=4 h and phenol concentrations in the medium of 200 mg l(-1). Phenol in concentrations from 300 to 500 mg l(-1) was fully degraded at Tr>9 h and phenol load reaching 530-1330 mg l(-1) day(-1) for the individual concentrations. The post-denitrification effluent leaving packed bed reactor in spite of the absence or even trace amounts of phenol in it requires further purification.     

Production of 6-APA using a recirculated packed bed batch reactor

Summary A recirculated packed bed batch reactor has been designed for the production of 6-aminopenicillanic acid. It was observed that the flow rate of penicillin G solution is a rate limiting step for its hydrolysis. Under the conditions used, the maximum rate of hydrolysis of penicillin G was observed at a flow rate of 3.0 L/min.     

Biological phenol degradation in a gas-liquid-solid fluidized bed reactor

Biological phenol degradation was performed experimentally in a gas-liquid-solid fluidized bed bioreactor using a mixed culture of living cells immobilized on activated carbon particles. A comprehensive model was developed for this system utilizing double-substrate limiting kinetics. The model was used to simulate the effects of changing inlet phenol concentration and biofilm thickness on the rate of biodegradation for two different types of support particles. The model shows that gas-liquid mass transfer is the limiting step in the rate of phenol biodegradation when the phenol loading is high.     

Azo dyes decolorization under high alkalinity and salinity conditions by Halomonas sp. in batch and packed bed reactor

Biodecolorization and biodegradation of azo dyes are a challenge due to their recalcitrance and the characteristics of textile effluents. This study presents the use of Halomonas sp. in the decolorization of azo dyes Reactive Black 5 (RB5), Remazol Brilliant Violet 5R (RV5), and Reactive Orange 16 (RO16) under high alkalinity and salinity conditions. Firstly, the effect of air supply, pH, salinity and dye concentration was evaluated. Halomonas sp. was able to remove above 84% of all dyes in a wide range of pH (6–11) and salt concentrations (2–10%). The decolorization efficiency of RB5, RV5, and RO16 was found to be ≥ 90% after 24, 13 and 3 h, respectively, at 50 mg L⁻¹ of dyes. The process was monitored by HPLC-DAD, finding a reduction of dyes along the time. Further, Halomonas sp. was immobilized in volcanic rocks and used in a packed bed reactor for 72 days, achieving a removal rate of 3.48, 5.73, and 8.52 mg L⁻¹ h⁻¹, for RB5, RV5 and RO16, respectively, at 11.8 h. The study has confirmed the potential of Halomonas sp. to decolorize azo dyes under high salinity and alkalinity conditions and opened a scope for future research in the treatment of textile effluents.

     

Lactic acid production by Lactobacillus delbrueckii in a dual reactor system using packed bed biofilm reactor

Aims:  An integrated dual reactor system for continuous production of lactic acid by Lactobacillus delbrueckii using biofilms developed on reticulated polyurethane foam (PUF) is demonstrated.
Methods and Results:  Lactobacillus delbrueckii was immobilized on PUF, packed in a bioreactor and used in lactic acid fermentation. The rate of lactic acid production was significantly high with a volumetric productivity of 5 g l⁻¹ h⁻¹ over extended period of time. When coupled to a bioreactor, the system could be operated as dual reactor for over 1000 h continuously without augmentation of inoculum and no compromise on productivity.
Conclusions:  Polyurethane foams offer an excellent support for biofilm formation.
Significance and Impact of the Study:  The system was very robust and could be operated for prolonged period at a volumetric productivity of 4–6 g l⁻¹ h⁻¹.     

A comparative study of immobilized amyloglucosidase in a packed bed reactor and a continuous feed stirred tank reactor

The catalytic activity of amyloglucosidase covalently attached to DEAE-cellulose was studied in a packed bed reactor and a continuous feed stirred tank reactor (CSTR) for the reaction maltose → glucose. At low flow rates mass-transfer limitations in the bed reactor lead to lower conversions for this reactor compared to the CSTR. Simple theoretical expressions for these reactors were compared with the experimental results. There are significant differences between the kinetic parameters and pH profile of the immobilized and free enzyme. The immobilized enzyme also showed greater stability at 50°C than did free amyloglucosidase. The temperature dependence of the reaction rate was the same for immobilized and free enzyme.     

Kinetics of pyridine degradation along with toluene and methylene chloride with Bacillus sp. in packed bed reactor

Bacillus coagulans strain isolated from contaminated soil was immobilised on activated carbon for degradation of pyridine, toluene and methylene chloride containing synthetic wastewaters. Pyridine was supplied as the only source of nitrogen in the wastewaters. Continuous runs in a packed bed laboratory reactor showed that immobilized B. coagulans can degrade pyridine along with other organics rapidly and the effluent ammonia is also controlled in presence of “organic carbon”. About 644?mg/l of influent TOC was efficiently degraded (82.85%) at 64.05?mg/l/hr loading.     

Phenol degradation in a three-phase biofilm fluidized sand bed reactor

A previous three phase fluidized sand bed reactor design was improved by adding a draft tube to improve fluidization and submerged effluent tubes for sand separation. The changes had little influence on the oxygen transfer coefficients(K _L a), but greatly reduced the aeration rate required for sand suspension. The resulting 12.5 dm³ reactor was operated with 1 h liquid residence time, 10.2dm³/min aeration rate, and 1.7–2.3 kg sand (0.25–0.35 mm diameter) for the degradation of phenol as sole carbon source. The K _La of 0.015 s^–1 gave more than adequate oxygen transfer to support rates of 180g phenol/h · m³ and 216 g oxygen/h · m³. The biomass-sand ratios of 20–35 mg volatiles/g gave estimated biomass concentrations of 3–6 g volatiles/dm³. Offline kinetic measurements showed weak inhibition kinetics with constants ofK _s=0.2 mg phenol/dm³, K _o2=0.5 mg oxygen/dm³ and KinI= 122.5 mg phenol/dm³. Very small biofilm diffusion effects were observed. Dynamic experiments demonstrated rapid response of dissolved oxygen to phenol changes below the inhibition level. Experimentally simulated continuous stagewise operation required three stages, each with 1 h residence time, for complete degradation of 300 mg phenol/dm³ · h.     

Aerobic degradation of the azo dye acid red 151 in a sequencing batch biofilter

The azo dye acid red 151 (AR151) was aerobically biodegraded in a sequencing batch biofilter packed with a porous volcanic rock. AR151 was used as the sole source of carbon and energy for acclimated microorganisms. Acclimation was followed using the degradation time and the oxygen uptake rate. A maximal oxygen uptake rate of 0.5 mg O(2)/(lmin) was obtained. Mineralization studies showed that 73% (as carbon) of the initial azo dye was transformed to CO(2) by the consortia. A maximal substrate degradation rate of 247 mg AR151/(l(reactor)d) was obtained. Color removal was up to 99% using an initial concentration of 50 mg AR151/l. Anaerobic tests suggested that in the interior of the porous material, anaerobic biotransformations can occur, contributing from 14% to 16% of the decoloration of the azo dye.     

Basic and applied aspects in the microbial degradation of azo dyes

Azo dyes are the most important group of synthetic colorants. They are generally considered as xenobiotic compounds that are very recalcitrant against biodegradative processes. Nevertheless, during the last few years it has been demonstrated that several microorganisms are able, under certain environmental conditions, to transform azo dyes to non-colored products or even to completely mineralize them. Thus, various lignolytic fungi were shown to decolorize azo dyes using ligninases, manganese peroxidases or laccases. For some model dyes, the degradative pathways have been investigated and a true mineralization to carbon dioxide has been shown. The bacterial metabolism of azo dyes is initiated in most cases by a reductive cleavage of the azo bond, which results in the formation of (usually colorless) amines. These reductive processes have been described for some aerobic bacteria, which can grow with (rather simple) azo compounds. These specifically adapted microorganisms synthesize true azoreductases, which reductively cleave the azo group in the presence of molecular oxygen. Much more common is the reductive cleavage of azo dyes under anaerobic conditions. These reactions usually occur with rather low specific activities but are extremely unspecific with regard to the organisms involved and the dyes converted. In these unspecific anaerobic processes, low-molecular weight redox mediators (e.g. flavins or quinones) which are enzymatically reduced by the cells (or chemically by bulk reductants in the environment) are very often involved. These reduced mediator compounds reduce the azo group in a purely chemical reaction. The (sulfonated) amines that are formed in the course of these reactions may be degraded aerobically. Therefore, several (laboratory-scale) continuous anaerobic/aerobic processes for the treatment of wastewaters containing azo dyes have recently been described.     

Lipase-mediated acidolysis of butteroil with free conjugated linoleic acid in a packed bed reactor

Acidolysis of butteroil with free conjugated linoleic acid (CLA) was studied in a packed bed reactor containing an immobilized Candida antarctica (fraction B) lipase. Kinetic data were used to develop quantitative reversible rate expressions of the general Michaelis-Menten form that also incorporate a term for first-order deactivation of the enzyme. The extent of incorporation of CLA in the triacylglycerols of butteroil was characterized for reactions carried out at several temperatures (namely 45 degrees, 50 degrees, and 55 degrees C) with different weight ratios of butteroil to CLA (namely 10:1 and 2:1). At the optimum operating temperature of 50 degrees C, similar levels of incorporation of CLA (60% to 85%) were achieved at low space times (<3 h) for both 10:1 and 2:1 (w/w) ratios of butteroil to CLA.     

Enzymatic synthesis of alpha-butylglucoside linoleate in a packed bed reactor for future pilot scale-up

The enzymatic synthesis of a mixture of unsaturated fatty acid alpha-butylglucoside esters, containing more than 60% alpha-butylglucoside linoleate, was achieved through lipase-catalyzed esterification. The continuous evaporation under reduced pressure of the water produced enabled substrate conversions greater than 95% to be reached. Two immobilized lipases from Candida antarctica (Chirazyme L2, c.-f., C2) and Rhizomucor miehei (Chirazyme L9, c.-f.) were compared in stirred batch and packed bed configurations. When the synthesis was carried out in stirred batch mode, C. antarctica lipase appeared to be of greater interest than the R. miehei enzyme in terms of stability and regioselectivity. Surprisingly, a change in the process design to a packed bed configuration enabled the stability of R. miehei lipase to be significantly improved, while the C. antarctica lipase efficiency to synthesize unsaturated fatty acid alpha-butylglucoside esters was slightly decreased. Water content in the microenvironment of the biocatalyst was assumed to be responsible for such changes. When the process is run in stirred batch mode, the conditions used promote the evaporation of the essential water surrounding the enzyme, which probably leads to R. miehei lipase dehydration. In contrast, the packed bed design enabled such water evaporation in the microenvironment of the biocatalyt to be avoided, which resulted in a tremendous improvement of R. miehei lipase stability. However, C. antarctica lipase led to the formation of 3% diesters, whereas the final percentage of diesters reached 21% when R. miehei enzyme was used as biocatalyst. A low content of diesters is of greater interest in terms of alpha-butylglucoside linoleate application as linoleic acid carrier, and therefore the enzyme choice will have to be made depending on the properties expected for the final product.