Effect of deflecting ring on noise generated by outdoor set of a split-unit air conditioner

In order to analyze the influence of the deflecting ring on the noise generated by the outdoor set of a split-unit air conditioner, the flow field in the outdoor set is simulated with the CFD software STAR-CD, the relative turbulent intensities are computed and the influence of the width and contoured duct of the deflecting ring on the noise generated by the outdoor set is analyzed. The results of computation and experiment show that there is an optimal width of the deflecting ring, corresponding to the minimum noise generated by the outdoor set. In addition, the influence of the contoured duct of the deflecting ring on the noise generated by the outdoor set is analyzed and a double contoured duct is designed. The results of computation and experiment verify that the deflecting ring with double contoured duct can improve the aerodynamic performance and reduce the noise generated by the outdoor set.     

Photocatalytic Removal of Hg from Solid Wastes of Chlor-Alkali Plant

The removal of mercury from hazardous wastes of a chlor-alkali plant was investigated by a combined process of acid attack and photoreduction treatment. The solution obtained by acid attack of the solid wastes was treated with ultraviolet irradiation in the presence of titanium dioxide and an organic agent (citric acid), leading to the selective precipitation of reduced mercury, while the other metal compounds remained in the solution. In spite of the large excess of non-reducible metal ions (100 times or more on a molar basis), more than 99% of the mercury initially present in the solid wastes was removed. Competitive adsorption of the different metal compounds on the titanium dioxide surface led to lower rates of mercury reduction. This combined process can be an efficient alternative method for mercury separation because the final effluents have reached a quality close to that of the standards imposed by international environmental agencies.     

Terminal Electron Acceptor Mass Balance: Light Nonaqueous Phase Liquids and Natural Attenuation

Light nonaqueous phase liquids (LNAPLs) in subsurface systems may contain a relatively large amount of biodegradable organic material. During the biochemical oxidation of the organic compounds in the LNAPL, electrons are transferred to terminal electron acceptors (TEA) [i.e., O2, NO3?, Mn(IV), Fe(III), SO4?2, CO2] via coupled redox reactions. A mass balance between the TEA required for mineralization of benzene, toluene, ethyl benzene, and xylene (BTEX) compounds contained in the subsurface (ground water, soil, LNAPL) and the total TEA available from the ground water and aquifer sediments is proposed and evaluated. The total TEA available is predominantly attributed to the solid phase material; the aqueous phase TEA constitutes a minor amount; and the TEA required for BTEX mineralization is predominantly from the LNAPL. Consequently, a TEA deficit exists in the LNAPL source area. Under these conditions, it may be invalid to assume an infinite supply of TEA and sustained bioattenuation rates. LNAPL removal is one remedial option to reduce the TEA deficit in the source area.     

Modeling Substrate Interactions during Aerobic Biodegradation of Mixtures of Vinyl Chloride and Ethene

Ethene (ETH) is often associated with vinyl chloride (VC) in contaminated groundwater, as it is formed along with vinyl chloride during reductive dechlorination of higher chloroethenes (e.g., perchloroethylene and trichloroethylene). In the present study the interaction between VC and ETH during their aerobic biodegradation by enrichment cultures was investigated. The cultures were able to use both compounds as growth substrates. In mixture experiments, the degradation rate of one substrate was affected by the presence of the other. A biokinetic model based on competitive inhibition described well the observed substrate interactions over a range of initial VC (0–144 μmol?L?1) and ETH (0–37.5 μmol?L?1) concentrations, using parameters estimated from single-substrate experiments. Notably, half-velocity coefficients could be used as competitive inhibition coefficients. This finding shows the importance of obtaining accurate measurements of half-velocity coefficients in order model competitive inhibition processes. Simulation results showed that when the initial ETH concentration was raised from 0 to 30 μmol?L?1, the apparent half-velocity coefficient for VC (KVCAPP) increased by nearly three times, from 12.9 to 35.4 μmol?L?1. This finding has strong environmental implications because a low half-velocity coefficient for VC is regarded as the major prerequisite for achieving efficient and complete VC degradation. Moreover, the effect of ETH on the efficiency of VC removal is strongly dependent on the KVC/KETH ratio, consequently determination of KETH for VC-degrading microbes is important when biodegradation (or bioaugmentation) is considered for clean up of VC-contaminated sites. Additional model simulations, using the ratio of KVC to KETH for previously characterized VC- and ETH-utilizing microorganisms (values ranged from 0.06 to 1.2) showed that their ability to degrade VC in the presence of ETH may differ significantly.     

Oxidative and Reductive Pathways in Manganese-Catalyzed Fenton’s Reactions

Soluble manganese (II) and amorphous and crystalline manganese (IV) oxides were investigated as catalysts for the Fenton-like decomposition of hydrogen peroxide into oxidants and reductants. 1-Hexanol was used as a hydroxyl radical probe and carbon tetrachloride (CT) was used as a reductant probe. Soluble manganese (II)-catalyzed reactions at acidic pH resulted in >99% degradation of 1-hexanol and no measurable transformation of CT, indicating that hydroxyl radicals were generated but reductants were not. However, when these reactions were conducted at near-neutral pH, an amorphous manganese oxide precipitate formed and 89% of the CT degraded in 60?min, while 1-hexanol degradation was negligible. Using an amorphous manganese oxide synthesized in a separate reactor, CT was rapidly degraded while 1-hexanol oxidation was undetectable. Reactions catalyzed by the crystalline manganese oxide pyrolusite(β-MnO2) at near-neutral pH also resulted in significant CT degradation, indicating that reductants are generated by both the crystalline and amorphous manganese oxide-catalyzed decomposition of H2O2. The presence of manganese oxides in the subsurface and their ability to catalyze the generation of reductants in modified Fenton’s reactions has important implications for hydrogen peroxide stability and contaminant transformation pathways during the in situ Fenton’s treatment of contaminated soils and groundwater.     

Optimization of Internal Bypass Ratio for Complete Ammonium and Phosphate Removal in a Dephanox-Type Two-Sludge Denitrification System

The capacity of complete simultaneous ammonium and phosphate removal was studied in a laboratory scale Dephanox system in relation to its internal bypass ratio (BPR). In this configuration, most of the ammonium detected in the effluent is ammonium bypassed by the system’s internal settler. Therefore, this research studies the possibility of complete simultaneous ammonium and phosphate removal by means of the balance of bypassed ammonium with ammonium requirement for growth of denitrifying phosphorus accumulating organisms in the anoxic tank. During these experiments, ammonium removal was governed by internal BPR and limited by sludge settleability. The predominant anaerobic-anoxic sludge developed a high settleability, allowing the application of drastic low BPRs. The system studied under many BPRs proved to achieve almost complete simultaneous ammonium and phosphate removal for BPRs ranging from 0.08 to 0.13 of the influent. A BPR lower than the inferior limit produced extreme accumulation of sludge into the internal settler, interfering in the distribution of sludge and consequently in removal efficiency. A positive effect of the internal settler was the extension of anaerobic contact time and anaerobic solids retention time. The increased phosphorus release suggests that a higher volatile fatty acids production might have occurred when raw wastewater was used as influent.     

非热等离子体净化挥发性有机废气研究进展

文章就非热等离子技术在治理挥发性有机废气时的能量效率及副产物生成问题展开评述。     

烟囱高振型横风向共振的振害分析及减振设计

以实测 ( 2 1 0m/7 0m)钢筋混凝土烟囱动力特性数据为依据。研究分析指出了发生第 2、第 3阶振型的横风向共振是完全可能的。其计算应列入国家标准“烟囱设计规范”。     

Catalytic Oxidation of Volatile Organic Liquids

Metal oxide and supported-Pt catalysts were developed for complete oxidation of volatile organic compounds (VOCs) and other solvent-derived organic vapors (OVs) in air at relatively low temperatures. The goal for this work is to produce a simple, cost-effective technology for reducing the concentration of organic contaminants in air to acceptable levels before the air is released into the atmosphere or recirculated. Specific applications include ventilated work spaces for spray painting and engine maintenance, indoor air decontamination, dry cleaning, food processing, fume hoods, residential use, and solvent-intensive industrial processes. Catalyst powders and monolith-supported catalysts were screened for conversion of 1-butanol, toluene, and methyl ethyl ketone to carbon dioxide and water. The concentration of OVs in the feedstream was maintained at approximately 100 ppmv, and the space velocity was between 6,000 and 18,000 h?1. Metal oxide catalysts without Pt generated complete conversion of 1-butanol to CO2 at 150°C, 69% conversion at 100°C, and 15% conversion at 80°C. For toluene, complete conversion was achieved at 200°C, and greater than 75% conversion at 150°C. Addition of Pt to the metal oxide compositions typically lowered the temperature for a given OV oxidation rate by at least 20–50°C. Catalysts deposited onto standard commercial cordierite monoliths retained their composition and activity, and were stable in humid air, as well as nitrogen- and chlorine-containing OVs. However, the catalysts quickly deactivated in the presence of sulfur and phosphorus.     

Heavy Metals Removal from Acidic and Saline Soil Leachate Using Either Electrochemical Coagulation or Chemical Precipitation

This study compares electrocoagulation and chemical precipitation for heavy metals removal from acidic soil saline leachate (SSL) at the laboratory pilot scale. The electrocoagulation process was evaluated via an electrolytic cell [12 cm (width)×12 cm (length)×19 cm (depth)] using mild steel electrodes (10 cm width×11 cm high), whereas chemical precipitation was evaluated using either calcium hydroxide [Ca(OH)2] or sodium hydroxide (NaOH). By comparison with chemical precipitation at a pH varying between 7 and 8, electrocoagulation was more effective in removing metals from SSL having a relatively low contamination level (124?mg?Pb/L and 38?mg?Zn/L). For SSL enriched with different heavy metals (each concentration of metals was initially adjusted to 100 mg/L) and treated at a pH lower than 8.5, with the exception of Cd, the residual metal concentrations at the end of the experiments were below the acceptable level recommended for effluent discharge in urban sewage works (less than 4 mg/L of each residual metal concentration was recorded) using electrocoagulation, contrary to chemical precipitation using NaOH (more than 15 mg/L of each residual metal concentration was recorded). By comparison, chemical precipitation using Ca(OH)2 was effective in reducing Cr, Cu, Ni, and Zn under the permissive level, but not for Cd and Pb. However, both chemical precipitation processes needed to be operated at higher pH values (around 10.0) to be more effective in reducing metals from SSL and, therefore, required a pH adjustment of the effluent before discharge, whereas electrochemical treatment had a practical advantage of producing an effluent having a pH close to the neutral value and suitable for stream discharge in the receiving water. On the other hand, electrocoagulation was also found to be very efficient for removing Pb from very contaminated solutions (250–2,000 mg?Pb/L). At least 94% of Pb was removed regardless of the initial Pb concentration in the SSL. Electrochemical coagulation involves a total cost varying from 8.67 to 13.00 $/tds, whereas 0.84 to 16.73 $/tds is recorded using chemical precipitation. The cost included only energy consumption, chemicals consumption, and metallic sludge disposal.