Treatment of reverse osmosis concentrate from industrial coal wastewater using an electro-peroxone process with a natural air diffusion electrode

Electrochemical oxidation of reverse osmosis concentrate using a pilot-scale reactive electrochemical membrane filtration system: Performance and mechanisms

Scale-up treatment of real wastewater holds the key to promoting the practical application of electrochemical filtration technology. This work used a pilot-scale Ti/Pd reactive electrochemical membrane (REM) system (12 REM modules with a total REM area of 0.144 m2) to treat high-salinity reverse osmosis concentrate (ROC) from a chemical industry park. The pilot-scale Ti/Pd REM system demonstrated effective electrochemical degradation of ROC wastewater, achieving removal efficiencies of 82.3 ± 1.9% for COD and 46.7 ± 5.6% for TN at a membrane flux of 90 L/(m2·h) and a cell voltage of 5 V, with an energy consumption of 0.045 kWh/g-COD. Singlet oxygen (1O2) and reactive chlorine species were identified as the two primary reactive oxygen species generated in the Ti/Pd REM system. Fluorescence spectroscopy and Fourier transform ion cyclotron resonance mass spectrometry (FT-ICR-MS) analysis indicated that the pilot-scale Ti/Pd REM treatment effectively oxidized humic acid-like substance and unsaturated aromatic compounds. Overall, the Ti/Pd REM technology shows a promising application potential for the treatment of high-salinity ROC from the chemical industry.

Upgrading the peroxi-coagulation treatment of complex water matrices using a magnetically assembled mZVI/DSA anode: Insights into the importance of ClO radical

The electrochemical technologies for water treatment have flourished over the last decades. However, it is still challenging to treat the actual complex water effluents by a single electrochemical process, often requiring coupling of technologies. In this study, an upgraded peroxi-coagulation (PC) process with a magnetically assembled mZVI/DSA anode has been devised for the first time. COD, NH₃-N and total phosphorous were simultaneously and effectively removed from livestock wastewater. The advantages, influence of key parameters and evolution of electrogenerated species were systematically investigated to fully understand this novel PC process. The fluorescent substances in livestock wastewater could also be almost removed under optimal conditions (300 mA, 0.2 g ZVI particles and pH 6.8). The interaction between OH and active chlorine yielded ClO with a high steady-state concentration of 6.85 × 10^-13 M, which did not cause COD removal but accelerated the oxidation of NH₃-N. The Mulliken population suggested that OH and NH₃-N had similar electron-donor behavior, whereas ClO acted as an electron-withdrawing species. Besides, although the energy barrier for the reaction between OH and NH₃-N (17.0 kcal/mol) was lower than that with ClO (18.8 kcal/mol), considering the tunneling in the H abstraction reaction, the Skodje-Truhlar method adopted for calculations evidenced a 17-fold faster NH₃-N oxidation rate with ClO. In summary, this work describes an advantageous single electrochemical process for the effective treatment of a complex water matrix.

Employing electro-peroxone process for degradation of Acid Red 88 in aqueous environment by Central Composite Design: A new kinetic study and energy consumption

The Azo dyes are primarily employed in textile industries to produce high amounts of colored organic and inorganic wastewater. Therefore, their treatments are critical. In this research, the removal and mineralization of Acid red 88 (AR88), as a widely used mono Azo dye, was inspected by the Electro-peroxone(E-peroxone) method. It is a coupling of electrochemically produced H₂O₂ and ozone that can produce robust hydroxyl radicals. The Central Composite Design (CCD) was applied to explore the influence of operational variables on the removal of AR88 as a response. The optimal conditions predicted by the CCD were as the following; Applied current at 0.7 A, pH at 7.35, O₃ Flowrate at 1.03 L min^-1 and the concentration of AR88 at 527.29 mg. L^-1. The Pareto chart showed that the concentration of AR88 has a significant influence on the response. At the predicted optimal conditions, the actual and predicted AR 88 removal were 95.4 and 92.96%, respectively. The removal of COD after 45 min was 70% representing the excessive efficiency of E-peroxone in mineralization of AR88. The E-peroxone follows the pseudo-first-order kinetics (k_{obs-E-peroxone} = 6.56 × 10^-2 min^-1), which was more remarkable than the single ozonation, and electrolysis. The calculated specific energy consumption (SEC) in the E-peroxone was 40.14 kWh/Kg AR 18 removal, which was lower than the individual ozonation, and electrolysis methods. The operative production of H₂O₂ from O₂ at the cathode is the critical factor in the high removal of AR88 in this process.