Evaluation of the technoeconomic feasibility of electrochemical hydrogen peroxide production for decentralized water treatment

doi:10.1007/s11783-020-1293-2

Front. Environ. Sci. Eng.

2021, Vol. 15

Issue (1) : 1 https://doi.org/10.1007/s11783-020-1293-2

RESEARCH ARTICLE

Evaluation of the technoeconomic feasibility of electrochemical hydrogen peroxide production for decentralized water treatment

Yang Li, Yixin Zhang, Guangshen Xia, Juhong Zhan, Gang Yu, Yujue Wang(

)

School of Environment, State Key Joint Laboratory of Environmental Simulation and Pollution Control, Beijing Key Laboratory for Emerging Organic Contaminants Control, Tsinghua University, Beijing 100084, China

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Abstract

• Gas diffusion electrode (GDE) is a suitable setup for practical water treatment.

• Electrochemical H₂O₂ production is an economically competitive technology.

• High current efficiency of H₂O₂ production was obtained with GDE at 5–400 mA/cm².

• GDE maintained high stability for H₂O₂ production for ~1000 h.

• Electro-generation of H₂O₂ enhances ibuprofen removal in an E-peroxone process.

This study evaluated the feasibility of electrochemical hydrogen peroxide (H₂O₂) production with gas diffusion electrode (GDE) for decentralized water treatment. Carbon black-polytetrafluoroethylene GDEs were prepared and tested in a continuous flow electrochemical cell for H₂O₂ production from oxygen reduction. Results showed that because of the effective oxygen transfer in GDEs, the electrode maintained high apparent current efficiencies (ACEs,>80%) for H₂O₂ production over a wide current density range of 5–400 mA/cm², and H₂O₂ production rates as high as ~202 mg/h/cm² could be obtained. Long-term stability test showed that the GDE maintained high ACEs (>85%) and low energy consumption (<10 kWh/kg H₂O₂) for H₂O₂ production for 42 d (~1000 h). However, the ACEs then decreased to ~70% in the following 4 days because water flooding of GDE pores considerably impeded oxygen transport at the late stage of the trial. Based on an electrode lifetime of 46 days, the overall cost for H₂O₂ production was estimated to be ~0.88 $/kg H₂O₂, including an electricity cost of 0.61 $/kg and an electrode capital cost of 0.27 $/kg. With a 9 cm² GDE and 40 mA/cm² current density, ~2–4 mg/L of H₂O₂ could be produced on site for the electro-peroxone treatment of a 1.2 m³/d groundwater flow, which considerably enhanced ibuprofen abatement compared with ozonation alone (~43%–59% vs. 7%). These findings suggest that electrochemical H₂O₂ production with GDEs holds great promise for the development of compact treatment technologies for decentralized water treatment at a household and community level.

Keywords Advanced oxidation process Electro-peroxone Gas diffusion electrode Hydrogen peroxide Oxygen reduction

Corresponding Author(s): Yujue Wang

Issue Date: 13 July 2020

Cite this article:

Yang Li,Yixin Zhang,Guangshen Xia, et al. Evaluation of the technoeconomic feasibility of electrochemical hydrogen peroxide production for decentralized water treatment[J]. Front. Environ. Sci. Eng., 2021, 15(1): 1.

URL:

https://academic.hep.com.cn/fese/EN/10.1007/s11783-020-1293-2
https://academic.hep.com.cn/fese/EN/Y2021/V15/I1/1

Tab.1 Water quality parameters of the groundwater used in this study

Fig.1 Scheme of (a) electrochemical cell with the submerged and aerated electrode (SAE) and (b) the gas diffusion electrode (GDE), and (c) the electro-peroxone system for groundwater treatment.

Fig.2 Evolution of H₂O₂ concentrations and apparent current efficiency for H₂O₂ during electrolysis with the submerged and aerated electrode (a and b) and with gas diffusion electrode (c and d). Reaction conditions: HRT= 10 min, water flow rate= 40 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 2 cm × 2 cm for the SAE and GDE, O₂ flow rates= 0.25–2 L/min for the SAE and 0.25 L/min for the GDE.

Fig.3 H₂O₂ production rates as a function of applied current density during electrolysis with the GDE cathode and with the SAE cathode (inset). Reaction conditions: HRT= 10 min, water flow rate= 40 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 2 cm × 2 cm for the SAE and GDE, O₂ flow rates= 0.25 L/min for the GDE and 2 L/min for the SAE.

Fig.4 (a) H₂O₂ concentrations and ACEs for H₂O₂ production, (b) cell voltage and energy consumption for H₂O₂ production as a function of applied current densities during electrochemical H₂O₂ production with the GDE cathode. Reaction conditions: HRT= 10 min, water flow rate= 40 mL/min, electrolyte= 0.1 M Na₂SO₄, electrode area= 3 cm × 3 cm, interelectrode distance= 2 cm.

Fig.5 (a) Potential profile in the electrochemical cell, (b) cell voltages and energy consumptions for H₂O₂ production as a function of interelectrode distance during electrochemical H₂O₂ production with the GDE cathode. Reaction conditions: HRT= 10 min, water flow rate= 40 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 3 cm × 3 cm, current density= 40 mA/cm².

Fig.6 Evolution of (a) apparent current densities and cell voltages, (b) energy consumption of H₂O₂ production as a function of solution conductivity during electrochemical H₂O₂ production with the GDE cathode. Reaction conditions: HRT= 10 min, water flow rate= 40 mL/min, electrolyte= 0.025–0.1 mol/L Na₂SO₄, electrode area= 3 cm × 3 cm, current density= 40 mA/cm²

Fig.7 Evolution of (a) H₂O₂ concentrations and ACEs for H₂O₂ production, (b) cell voltages and energy consumption for H₂O₂ production as a function of HRT during electrochemical H₂O₂ production with the GDE cathode. Reaction conditions: water flow rate= 5–40 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 3 cm × 3 cm, current density= 40 mA/cm².

Fig.8 Evolution of (a) H₂O₂ concentrations and ACEs for H₂O₂ production, (b) cell voltages and energy consumptions for H₂O₂ production during electrochemical H₂O₂ production with the GDE cathode. Reaction conditions: HRT= 20 min, water flow rate= 20 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 3 cm × 3 cm, interelectrode distance= 2 cm, current density= 40 mA/cm²

Fig.9 (a) Ibuprofen abatement efficiency, (b) E_EO of ibuprofen abatement as a function of H₂O₂ doses during ozonation and the E-peroxone treatment of the selected groundwater. Operating conditions of electrochemical cell: HRT= 20 min, water flow rate= 20 mL/min, electrolyte= 0.1 mol/L Na₂SO₄, electrode area= 3 cm × 3 cm, interelectrode distance= 2 cm, current density= 40 mA/cm². Operating conditions of ozone column: HRT= 10 min, water flow rate= 833 mL/min, flow rate of electrochemical cell effluent= 10–20 mL/min, O₃/O₂ gas flow rate= 0.25 L/min, gas phase O₃ concentration= 18.7 mg/L.

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