Jin Anotai

Temperature effect on microbial community of enhanced biological phosphorus removal system

Microbial population dynamics to gradual temperature change in an enhanced biological phosphorus removal system was kinetically investigated. As the temperature rose from 20.0 degrees C to 30.0 degrees C, and to 35.5 degrees C, the predominant microbial group changed from the phosphorus-accumulating organisms, PAOs (47-70% of total VSS) to the glycogen-accumulating organisms (64-75% of total VSS), and to the ordinary heterotrophs (90% of total VSS), respectively. Despite the species alteration, the phosphorus contents of the PAOs appeared to be steady within 0.182-0.308 mg/mg VSS(PAO) regardless of the temperature level. The initial specific phosphorus release rates, which are solely due to the PAOs activities, increased with the temperature from 37.5-55.9 to 51.8-61.3, 52.0-76.9, 147.2-210.3, and 374.2-756.3 mgP/gmVSS(PAO) h, at 20.0 degrees C, 25.0 degrees C, 30.0 degrees C, 32.5 degrees C, and 35.0 degrees C, respectively. On the other hand, mean initial specific phosphorus uptake rates of the biomass decreased as the temperature increased; however, the data implied that the rate of the PAOs was higher than the other two microbial groups. These results indicate that the PAOs are lower-range mesophiles or possibly psychrophiles. As the temperature rises, the portion of energy required for maintenance increases substantially which reduces the energy availability for cell reproduction; hence, the PAOs are washed out from the system.

Effect of hydrogen peroxide on aniline oxidation by electro-Fenton and fluidized-bed Fenton processes

In this study, the electro-Fenton and fluidized-bed Fenton processes under the given conditions were used to oxidize aniline. Factors such as feeding mode and concentration of the hydrogen peroxide were explored. Results showed that the feeding mode of H(2)O(2) did not significantly affect the aniline oxidation in the electro-Fenton process. However, the aniline oxidation slightly decreased with the two-step addition of H(2)O(2) in the fluidized-bed Fenton process. Presumably the decline of remaining Fe(2+) led to destitute hydrogen radicals from the Fe(2+)-catalyzed H(2)O(2). In addition, the removal efficiency of aniline was maintained at a maximum as H(2)O(2) concentration was higher than 0.04 M in the electro-Fenton process. Meanwhile, the almost exhausted H(2)O(2) would increase the amount of Fe(2+) in the solution for the electro-Fenton process. This is because the Fe(2+) is regenerated through the reduction of Fe(3+) on the cathode. The electro-Fenton process has a stronger oxidative ability with regard to the production of the oxalic acid than fluidized-bed Fenton process which was attributed to a higher consumption of H(2)O(2). Therefore, in the aspect of H(2)O(2) depletion, the mineralization efficiency of the fluidized-bed Fenton process was higher than that of the electro-Fenton process.

Decolorization of azo-reactive dye by polyphosphate- and glycogen-accumulating organisms in an anaerobic–aerobic sequencing batch reactor

An anaerobic-aerobic sequencing batch reactor with a sludge age of 8 days and anaerobic + aerobic + settling times of 18 + 5 + 1 h, was used to decolorize an azo-reactive dye wastewater. The nutrient broth (NB) and sodium acetate (SA) solution at 500 + 0, 350 + 150, 250 + 250 and 0 + 500 mg/l as COD was fed to the system to promote the polyphosphate-accumulating organisms (PAOs), while only glucose (500 mg/l COD) was used as a glycogen-accumulating organisms (GAOs) promoting substrate. The decolorization capability of the process was about 73-77 and 59-64% in terms of ADMI for the systems which the PAOs and GAOs proliferated, respectively. The color reduction was mainly achieved within the first 2 h of the anaerobic stage.

Iron crystallization in a fluidized-bed Fenton process.

The mechanisms of iron precipitation and crystallization in a fluidized-bed reactor were investigated. Within the typical Fentons reagent dosage and pH range, ferric ions as a product from ferrous ion oxidation would be supersaturated and would subsequently precipitate out in the form of ferric hydroxide after the initiation of the Fenton reaction. These precipitates would simultaneously crystallize onto solid particles in a fluidized-bed Fenton reactor if the precipitation proceeded toward heterogeneous nucleation. The heterogeneous crystallization rate was controlled by the fluidized material type and the aging/ripening period of the crystallites. Iron crystallization onto the construction sand was faster than onto SiO(2), although the iron removal efficiencies at 180 min, which was principally controlled by iron hydroxide solubility, were comparable. To achieve a high iron removal rate, fluidized materials have to be present at the beginning of the Fenton reaction. Organic intermediates that can form ferro-complexes, particularly volatile fatty acids, can significantly increase ferric ion solubility, hence reducing the crystallization performance. Therefore, the fluidized-bed Fenton process will achieve exceptional performance with respect to both organic pollutant removal and iron removal if it is operated with the goal of complete mineralization. Crystallized iron on the fluidized media could slightly retard the successive crystallization rate; thus, it is necessary to continuously replace a portion of the iron-coated bed with fresh media to maintain iron removal performance. The iron-coated construction sand also had a catalytic property, though was less than those of commercial goethite.

Kinetics and mechanism of 2,6-dimethyl-aniline degradation by hydroxyl radicals

This research investigated the intrinsic second-order rate constant between 2,6-dimethyl-aniline (2,6-DMA) and hydroxyl radicals (OH) using Fentons reactions under both batch and continuous operations. The competitive kinetics technique with aniline as a reference compound was employed. In the batch study under various conditions, the second-order rate constants of 2,6-DMA with OH were between 1.59 x 10(10) and 1.80 x 10(10)M(-1)s(-1) with a mean of 1.71 x 10(10)M(-1)s(-1) which equals the average value obtained from the continuous study as well. The concentrations of OH at the steady state under the continuous mode were estimated to be between 4.85 x 10(-10) and 6.82 x 10(-10)mM. 2,6-dimethyl-nitrobenzene, 2,6-dimethyl-phenol, 2,6-dimethyl-nitrophenol, 2,6-dimethyl-hydroquinone, 2,6-dimethyl-p-benzoquinone, and 2,6-dimethyl-3-hydroxy-p-benzoquinone were identified as the aromatic by-products indicating that the methyl group on the aromatic ring was not susceptible to OH attack. Maleic, lactic, oxalic, acetic, and formic acids were found as generated carboxylic acids. An oxidation pathway of 2,6-DMA by OH is also proposed.

Treatment of TFT-LCD wastewater containing ethanolamine by fluidized-bed Fenton technology.

The objectives of this study are: (1) to determine the effect of pH, initial concentration of Fe(2+) and H(2)O(2) dosage on the removal efficiency of MEA by fluidized-bed Fenton process and Fenton process, (2) to determine the optimal conditions for the degradation of ethanolamine from TFT-LCD wastewater by fluidized-bed Fenton process. In the design of experiment, the Box-Behnken design was used to optimize the operating conditions. A removal efficiency of 98.9% for 5mM MEA was achieved after 2h under optimal conditions of pH3, [Fe(2+)]=5mM and [H(2)O(2)]=60mM.

Photocatalytic activity of tungsten-doped TiO2 with hydrothermal treatment under blue light irradiation

Tungsten doping and hydrothermal treatment were found to significantly improve the visible-light photoactivity of TiO(2) synthesized by the sol-gel method. It was observed that TiO(2) doped with a 0.5% W:Ti mole ratio and treated with 4 h of hydrothermal curing showed photoactivity under blue light irradiation equal to 74% of the commercial Degussa P-25 under UV irradiation, i.e., 0.01 mM 2-chlorophenol was completely removed in 120 and 90 min, respectively. Light absorptivity and photocatalytic activity under blue light irradiation were not dependent on the crystallite structure of the TiO(2). The oxidation kinetics under blue light irradiation can be effectively explained by the Langmuir-Hinshelwood model with an apparent reaction rate constant and a Langmuir constant of 3.60 × 10(-4) mM min(-1) and 206.53 mM(-1), respectively.

Comparison of o-toluidine degradation by Fenton, electro-Fenton and photoelectro-Fenton processes

A Box-Behnken design (BBD) statistical experimental design was used to investigate the degradation of o-toluidine by the electro-Fenton process. This method can be used to determine the optimal conditions in multivariable systems. Fe(2+) concentration (0.2-1.0mM), H(2)O(2) concentration (1-5mM), pH (2-4), and current (1-4A) were selected as independent variables. The removal efficiencies for o-toluidine and chemical oxygen demand (COD) were represented by the response function. Result by 2-level factorial design show that the pH and the Fe(2+) and H(2)O(2) concentrations were the principal parameters. Among the main parameters, the removal efficiencies for o-toluidine and COD were significantly affected by pH and Fe(2+) concentration. From the Box-Behnken design predictions, the optimal conditions in the electro-Fenton process for removing 90.8% of o-toluidine and 40.9% of COD were found to be 1mM of Fe(2+) and 4.85 mM of H(2)O(2) at pH 2. Under these optimal conditions, the experimental data showed that the removal efficiencies for o-toluidine and COD in the electro-Fenton process and the photoelectro-Fenton process were more than 91% and 43%, respectively, after 60 min of reaction. The removal efficiencies for o-toluidine and COD in the Fenton process are 56% and 27%, respectively.

Treatment of explosive-contaminated wastewater through the Fenton process

Abstract Owing to the extremely high chemical oxygen demand (COD), toxicity, and acidity of the explosive-contaminated wastewater, biological processes cannot be directly applied for its treatment. Therefore, Fenton’s reagent was employed to treat the explosive wastewater before discharge. The Fenton process is also the easiest and most reliable method of advanced oxidation. The treatment of this wastewater with pH, COD, acetate, nitrate, and sulfate contents of 2.32, 200 g L−1, 160 g L−1, 40 g L−1, and 35 g L−1, respectively, was investigated in this study. The effects of the hydrogen peroxide feeding rate, ferrous ion dosage, and hydrogen peroxide dosage on the efficiency of the Fenton process were investigated. The optimal conditions obtained in this study for the treatment of explosive wastewater were 358 mM of Fe2+ and continuous feeding of hydrogen peroxide (0.33 mL min−1), without pH adjustment or temperature control. The highest COD removal efficiency was 70% with an oxidation efficiency (OE) of 7...

Verification of competitive kinetics technique and oxidation kinetics of 2,6-dimethyl-aniline and o-toluidine by Fenton process

The competitive kinetics technique is shown to be a useful and reliable tool for determining rate constants. Regardless of the conditions of the reaction and the operation mode, the intrinsic second-order rate constants of 2,6-dimethyl-aniline and hydroxyl radicals were 1.65 × 10(10), 1.60 × 10(10), and 1.71 × 10(10)M(-1)s(-1) in the absence of SiO(2) under complete-mix conditions, in the presence of SiO(2) under complete-mix conditions, and in a fluidized-bed Fenton reactor with SiO(2) as the media, respectively, demonstrating that the rates are comparable under a variety of reaction conditions. The average intrinsic second-order rate constant of o-toluidine and hydroxyl radicals obtained in a homogeneous system under various conditions was 7.36 × 10(9)M(-1)s(-1), indicating that o-toluidine is less susceptible to hydroxyl radicals than 2,6-dimethyl-anilne. Hydroxyl radicals primarily attacked the amine group rather than the methyl group of the o-toluidine to form o-cresol and 2-nitrotoluene, which sequentially transformed to carboxylic acids including acetic, oxalic, lactic, and maleic acids after the collapse of the benzene ring.