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.     

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.     

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.     

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.     

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.     

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.     

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.

     

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.     

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.     

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.     

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.     

Oxidative degradation of azo dyes by manganese peroxidase under optimized conditions

The application of enzyme-based systems in waste treatment is unusual, given that many drawbacks are derived from their use, including low efficiency, high costs and easy deactivation of the enzyme. The goal of this study is the development of a degradation system based on the use of the ligninolytic enzyme manganese peroxidase (MnP) for the degradation of azo dyes. The experimental work also includes the optimization of the process, with the objective of determining the influence of specific physicochemical factors, such as organic acids, H(2)O(2) addition, Mn(2+) concentration, pH, temperature, enzyme activity and dye concentration. A nearly total decolorization was possible at very low reaction times (10 min) and at high dye concentration (up to 1500 mg L(-)(1)). A specific oxidation capacity as high as 10 mg dye degraded per unit of MnP consumed was attained for a decolorization higher than 90%. Among all, the main factor affecting process efficiency was the strategy of H(2)O(2) addition. The continuous addition at a controlled flow permitted the progressive participation of H(2)O(2) in the catalytic cycle through a suitable regeneration of the oxidized form of the enzyme, which enhanced both the extent and the rate of decolorization. It was also found that, in this particular case, the presence of a chelating organic acid (e.g., malonic) was not required for an effective operation. Probably, Mn(3+) was chelated by the dye itself. The simplicity and high efficiency of the process open an interesting possibility of using of MnP for solving other environmental problems.     

Production of structured triacylglycerols by acidolysis catalyzed by lipases immobilized in a packed bed reactor

The aim of this work was to produce structured triacylglycerols (STAGs), with caprylic acid located at positions 1 and 3 of the glycerol backbone and docosohexaenoic acid (DHA) at position 2, by acidolysis of tuna oil and caprylic acid (CA) catalyzed by lipases Rd, from Rhizopus delemar, and Palatase 20000L from Mucor miehei immobilized on Accurel MP1000 in a packed bed reactor (PBR), working in continuous and recirculation modes. First, different lipase/support ratios were tested for the immobilization of lipases and the best results were obtained with ratios of 0.67 (w/w) for lipase Rd and 6.67 (w/w) for Palatase. Both lipases were stable for at least 4 days in the operational conditions. In the storage conditions (5 °C) lipases Rd and Palatase maintained constant activity for 5 months and 1 month, respectively.These catalysts have been used to obtain STAGs by acidolysis of tuna oil and CA in a PBR operating with recirculation of the reaction mixture through the lipase bed. Thus, STAGs with 52–53% CA and 14–15% DHA were obtained. These results were the basis for establishing the operational conditions to obtain STAGs operating in continuous mode. These new conditions were established maintaining constant intensity of treatment (IOT, lipase amount × reaction time/oil amount). In this way STAGs with 44–50% CA and 17–24% DHA were obtained operating in continuous mode. Although the compositions of STAGs obtained with both lipases were similar, Palatase required an IOT about four times higher than lipase Rd.To separate the acidolysis products (free fatty acids, FFAs, and STAGs) an extraction method of FFAs by water–ethanol solutions was tested. The following variables were optimized: water/ethanol ratio (the best results were attained with a water/ethanol ratio of 30:70, w/w), the solvent/FFA–STAG mixture ratio (3:1, w/w) and the number of extraction steps (3–5). In these conditions highly pure STAGs (93–96%) were obtained with a yield of 85%. The residual FFAs can be eliminated by neutralization with a hydroethanolic KOH solution to obtain pure STAGs. The positional analysis of these STAGs, carried out by alcoholysis catalyzed by lipase Novozym 435, has shown that CA represents 55% of fatty acids located at positions 1 and 3 and DHA represents 42% of fatty acids at position 2.     

Simulation of a multicolumn recirculated packed bed reactor (MRPBR) for penicillin acylase

Enzyme reactors for the industrial hydrolysis of penicillin are analyzed in terms of biocatalyst stability to pH. A multicolumn system with packed beds placed in parallel and operating under recirculating conditions is proposed as an adequate reactor for this process. The system is studied both experimentally and with the aid of a simulation program.List of Symbols A transversal area (cm²) - C _A ammonia concentration in the reaction mixture (M) - C ₁ concentration of KH₂PO₄ in buffer (M) - C ₂ concentration of K₂HPO₄ in buffer (M) - d _p biocatalyst diameter (cm) - E enzyme or biocatalyst concentration (gcat l^–1) - K _APA APA non competitive inhibition constant (M) - K _IS excess substrate inhibition constant (M) - Km constant Michaelis-Menten (M) - K _PAA PAA competitive inhibition constant (M) - Q recirculation flow rate (cm³ min^–1) - Q _T recirculation flow rate per column (cm³ min^–1) - Re Reynolds number - S _E substrate concentration entering the neutralization tank (M) - S ₀ initial substrate concentration (M) - S _T substrate concentration in neutralization tank (M) - t time (min) - v _i initial reactor rate (mol min^–1 gcat^–1) - V _s superficial velocity (cm seg^–1) - V _T volume of neutralization tank (cm³) - X _E substrate conversion entering tank - X _T substrate conversion in neutralization tank - X conversion - Z reactor length (cm) - z axial position in reactor (cm) - z ^* non-dimensional axial position in reactor - biocatalyst's density (gcat cm^–3) - p pressure drop in the packed-bed reactor     

R-mandelic acid production with immobilized recombinant Escherichia coli cells in a recirculating packed bed reactor

A recirculating packed bed reactor (RPBR) was used for efficient production of R-mandelic acid (R-MA) by kinetic resolution of racemic R,S-mandelonitrile (R,S-MN) using the recombinant E. coli cells crosslinked with diatomite (DA)/glutaraldehyde (GA)/polyethyleneimine (PEI). The performance and productivity of RPBR were evaluated by several parameters, including cell load, substrate feeding rate, height diameter (H/D) ratio, reactor structures, and operation stability. The kinetic resolution process showed higher initial reaction rate (1.52?mM/min) and yield (100%) by recycling 100?mL of substrate solution (70?mM) through RPBR packed with 6.0?g immobilized cells at a substrate-feeding rate of 19?mL/min while the H/D ratio was 2.8. The immobilized cells were successfully applied into kinetic resolution of R,S-MN in the RPBR for 50 batches with an average productivity of 4.12?g/L/h for R-MA with >99% of enantiomeric excess.     

Proposed pathways for the reduction of a reactive azo dye in an anaerobic fixed bed reactor

Some process has been proposed for azo dye degradation and anaerobic bioreactors are one of them, since for their reduction, the dye has to be the electron acceptor. An anaerobic fixed bed bioreactor packed with activated carbon (AC) is proposed to degradate the Reactive Red 272 azo dye. In the present paper a dye degradation mechanism in an anaerobic environment is explained. It is very important to consider the interaction dye-microorganism-AC, because the groups in the AC surface take part in the reaction besides being an excellent carrier for microorganism and an adsorbent for the dye. The aromatic compounds produced in the dye reduction are partially degraded as a function of inlet dye concentration and reactor residence time. In anaerobic environment the aromatic compounds are decomposed through hydroxylation, carboxylation and redox reactions, due to enzymatic reactions.