Integrated and Superaerophilic Ni-O-C Electrode enables Fast and Stable Electrochemical H2O2 Production for Electro-Fenton-like Process

Fast and stable production of hydrogen peroxide (H 2 O 2 ) through electrochemical pathways is crucial for wastewater treatment applications. With this objective, herein we report an integrated and superaerophilic electrode composed of atomically dispersed Ni-O-C sites enriched carbon nanosheets (IS-NiOC electrode) for electrochemical oxygen reduction to produce H 2 O 2 . Both experimental and theoretical results have proven that atomically dispersed Ni-O-C sites enable a low overpotential (260 mV at 0.1 mA cm − 2 ) and high selectivity (> 90% at 0.0 ~ 0.5 V vs. RHE) in neutral electrolyte. Compared with a commercial gas-diffusion electrode, the IS-NiOC electrode offers stronger anity to oxygen bubbles and more robust three-phase contact points, resulting in high current density (~ 106 mA cm − 2 at 0.25 V vs. RHE) and superior stability (~ 200 h). These merits allow the application of the IS-NiOC electrode in an electro-Fenton-like process, which enables fast degradation of representative organic pollutants in both steady state and ow state.


Introduction
Hydrogen peroxide (H 2 O 2 ) is an environmentally friendly and highly e cient oxidant with a wide range of applications in elds of wastewater puri cation, medical treatment and industrial synthesis [1][2][3][4] . At present, over 99% of H 2 O 2 is produced by anthraquinone oxidation process; however, this process requires complex and large-scale infrastructure, generates a substantial volume of waste chemicals, and induces potential hazards in transport or store of the high concentration products [5][6][7][8][9] . For these reasons, an alternative route for small-scale on-site generation is urged to exploit. Direct electrochemical synthesis of H 2 O 2 by oxygen reduction reaction via a two-electron pathway (2e ORR) has gained a satisfactory solution to address the issues associated with the anthraquinone process due to its low resource consumption, convenience, and green initiative 8,10−14 . In practice, 2e ORR has already been successfully applied in electro-Fenton(EF)/electro-Fenton-like(EF-like) reactions [15][16][17] , which belong to economical advanced oxidation processes [18][19][20] for hazardous organic pollutants degradation.
In order to achieve fast and stable H 2 O 2 generation by an electrochemical method, catalytic electrodes with high current density at a low overpotential, high selectivity and excellent stability are desperately needed 2,21−24 . Previous studies have already identi ed various active catalysts, including noble metals and their alloys [25][26][27][28] , active carbonaceous materials 11,29−32 and transition metal-doped carbon materials [33][34][35][36] . In contrast to tremendous progress in seeking for active catalysts, there are very limited efforts devoted to investigate advanced electrode architectures, which is equally important and nonnegligible as e cient electrode architectures can simultaneous accelerate electron and reactant transport rate. [37][38][39][40][41][42] The general strategy to solve this problem is employing a Te on-treated carbon ber paper (TCFP) as the substrate to increase three-phase contact point (TPCP) by constructing gas-diffusion layer, as shown in Fig. 1a. However, the in-situ generated H 2 O 2 on an electrode surface would easily oxidize the carbon-based catalysts/substrates, and eventually destroy the gas diffusion channels and operation stability. Direct construction of active materials into micro-/nanostructures on conductive substrates to form integrated electrodes may reinforce the gas diffusion channels to against the destruction. 38,39,43,44 As schemed in Fig. 1b, we hypothesize that the integrated and superaerophilic electrode establishes a dense and thick gas diffusion layer that can mitigate the H 2 O 2 corrosion process.
Following this line, herein we demonstrated a nickel-incorporated oxidized carbon nanosheets arrays on carbon-ber paper (CFP) for electrochemical H 2 O 2 production. The nickel-incorporated oxygen-doped carbon catalyst (NiOC) exfoliated from CFP exhibited an outstanding intrinsic activity with an onset potential of ~ 0.5V vs. RHE and high selectivity (> 82%) over a wide potential range of 0.0 ~ 0.5V vs. RHE in neutral electrolyte. Proper surface modi cation of the NiOC electrode surface achieved strong a nity to gas bubbles, resulting in the fabrication of an integrated and superaerophilic NiOC electrode (IS-NiOC electrode) with robust and enriched TPCPs. Combining the advantages of the catalyst and surface property, the IS-NiOC electrode exhibited large current density (> 100 mA·cm − 2 ) at 0.25V vs. RHE and remarkable selectivity (> 90% at 0.0 ~ 0.5 V vs. RHE). More importantly, compared with a traditional electrode made by a drop-casting method (D-NiOC electrode, < 10 h stability), the IS-NiOC electrode possessed superior operation stability (~ 200 h) for electrochemical air reduction to produce H 2 O 2 . We also demonstrated the application of the IS-NiOC electrode in an EF-like process, which realized fast degradation of representative organic pollutants.

Results
Synthesis and characterizations of the IS-NiOC electrode. The IS-NiOC electrode was synthesized by a multi-step process, as schemed in Supplementary Fig. 1a. Firstly a conventional solvothermal method was employed to synthesis Ni(OH) 2 nanosheet (average size and thickness of ~ 1 µm and ~ 50 nm, respectively) arrays on CFP, as shown in Supplementary Fig. 1b. Afterwards, the Ni(OH) 2 nanosheet arrays were in situ transformed to NiOC catalyst (Fig. 1c, XRD can be seen in Supplementary Fig. 1c) with hierarchical and porous architecture by carbonizing polyoxyethylene (PEO) at a high temperature. Further, the NiOC electrode was modi ed by a speci c concentration of uorine-based polymers to achieve a superaerophilic surface. To demonstrate the structural advantage, the exfoliated NiOC catalyst was dropcasted on TCFP (D-NiOC electrode) as the contrast electrode. It was revealed that, once an individual air bubble (~ 50 µL) touched the electrode surface, about ~ 3.8s was needed for the bubble to spread out on D-NiOC electrode ( Fig. 1g and Supplementary Movie 1) while the required time shrunk to ~ 0.8 s for the IS-NiOC electrode ( Fig. 1e and Supplementary Movie 2), clearly demonstrating a much stronger a nity of the IS-NiOC electrode towards air bubbles. This phenomenon was attributed to the superaerophilic layer under neutral electrolyte (1 M Na 2 SO 4 ), which could build up a numerous of sturdy air pockets for coalescing with bubbles.
Transmission electron microscopy (TEM, Fig. 2a) revealed that the nal product was mainly composed of stubby carbon nanotubes, and high-resolution TEM image ( Supplementary Fig. 2) illustrated that Ni nanoparticle (lattice spacing: 0.208 nm) was encapsulated in the multilayered carbon shell (lattice spacing: 0.367 nm) and located at the tip area of stubby nanotubes. It should be noted that the Ni nanoparticles cannot be washed out even using strong acids. The atomic dispersion of Ni sites on NiOC was con rmed by aberration-corrected high-angle annular dark eld scanning transmission electron microscopy (HAADF-STEM, Fig. 2b) where the bright dots corresponding to Ni single-atom sites (marked by white circles, size of the bright spots if ca. 0.2 nm) were homogenously distributed throughout the entire sample. Elemental mappings results further con rmed the homogeneous distribution of Ni, O and C species across the tubular structure (Fig. 2c) despite the presence of inevitable Ni nanoparticles.
Closer inspection on the electronic structure promotes the deep understanding of structure-activity relationship. X-ray photoelectron spectroscopy (XPS) was rstly performed, and the results ( Supplementary Fig. 3a) further proved the presence of Ni, O and C elements in NiOC electrode. The existence of uorine (F) (Supplementary Fig. 3b) in IS-NiOC electrode con rmed the successful modi cation by polytetra uoroethylene (PTFE). The deconvoluted spectrum of nickel 2p (Fig. 2d) illustrated the coexistence of metallic and oxidation state nickel [45][46][47] , and the deconvoluted spectrum of RHE) at 0.01mA·cm − 2 and achieved selectivity of > 82.8% at a wide potential range of 0-0.50V (vs. RHE) in neutral media. Analogously, the O-C catalyst exhibited a similar selectivity at a narrower potential range (0 ~ 0.33 V vs. RHE), but a strong distinction occurred on the overpotential (Δ = 0.17 V). In addition, a faster ORR kinetics was found on the NiOC catalyst than that of O-C catalyst, as re ected in Tafel slopes (118.2 mV dec − 1 for NiOC and 161.0 mV dec − 1 for O-C, Supplementary Fig. 6). In view of the former XPS and XANES analysis, we thus drew a conclusion that such a huge ORR performance disparity was attributed to the presence of atomically-dispersed nickel in catalyst. Moreover, the NiOC catalyst was superior to those of reported carbon-based catalysts (O-CNTs 11 , Fe-CNT 33 , g-N-CNTs 51 , summarized in Table S1) and represented an outstanding activity and selectivity of the catalyst for 2e ORR in neutral media.
To understand the intrinsic high activity of NiOC system, DFT calculations were performed. For the 2e ORR, there are two reaction steps 52 : where the asterisk (*) represents the active site. As shown in Fig The superaerophilic property of an electrode has already been demonstrated effective in accelerating the gas diffusion process, thereby greatly enhancing the current increasing rate in diffusion region 39 . In this case, a fast-current increase rate as well as a large current density was observed in the IS-NiOC electrode by virtue of the advantages of catalyst and architecture. To evaluate the performance under high current density, a steady state ORR test was performed in with continuous oxygen bubbling by using H-Cell (as shown in Supplementary Fig. 7). The D-NiOC electrode with weaker a nity to gas bubbles was also tested for comparison. The typical ORR polarization curves with IR-correction of D-NiOC electrode and IS-NiOC electrode in neutral media were shown in Fig. 3d. The IS-NiOC electrode displayed an ultrahigh ORR performance with a rapid and stable current increase (~75 mA·cm -2 per 100 mV) and a large current density (~122 mA·cm -2 at 0.2 V vs. RHE, with IR correction). On the contrary, the D-NiOC electrode exhibited a limited current density (37.9 mA·cm -2 at 0.2 V vs. RHE, with IR correction) and slower current increasing rate (~17.6 mA·cm -2 per 100 mV). This phenomenon was attributed to lack of hierarchical architecture on D-NiOC electrode (as shown in Supplementary Fig. 8a), which weakened the interaction with gas bubbles. Moreover, bene ting from the superaerophilic nanostructure, the unique surface of IS-NiOC electrode could guarantee an unobstructed channel for gas reactants by constructing the robust TPCP and thick gas transfer channel.
Tafel analysis (Fig. 3e) illustrated that the IS-NiOC electrode provided a wider potential and current range (Δ= 0.1347 V, 0-15.46 mA cm -2 ) than that of D-NiOC electrode (Δ= 0.071 V, 0-8.55 mA cm -2 ) for linear portion of the curve, indicating that the gas diffusion process on IS-NiOC electrode was much faster than that of D-NiOC electrode. For the IS-NiOC electrode, the corresponding selectivity and production rate of H 2 O 2 under different potential (without IR-correction) in neutral medias were shown in Fig. 3f, where a high H 2 O 2 selectivity of 90.4% and H 2 O 2 production rate of 59.3 mg·cm -2 h -1 at 0 V vs RHE were observed.
This performance enhancement was also applicable in alkaline electrolyte (1 M KOH), where the IS-NiOC electrode exhibited a large current density (~250 mA·cm -2 at 0.3 V vs. RHE, without IR correction) and splendid H 2 O 2 selectivity (~95%), as shown in Supplementary Fig. 9. The IS-NiOC electrode can also reduce the oxygen in air with relatively lower concentration to form H 2 O 2 in a neutral system, where the working electrode was oated horizontally on the surface of the electrolyte (as shown in Supplementary  Fig. 10). The up-side surface can absorb air as the reactants and simultaneously release the liquid products from the down-side surface. For the IS-NiOC electrode, the 2e ORR current density in air atmosphere decreased to ~20% of that in oxygen atmosphere (Fig. 3g), which was consistent with the changing of oxygen concentration. In addition, the performance of IS-NiOC electrode and D-NiOC electrode in air got a similar tendency with those in oxygen atmosphere, as shown in Fig. 3h and 3i. The Tafel plots ( Supplementary Fig. 11) indicated that, compared with the ORR potential of IS-NiOC electrode in pure oxygen, a negative potential shift (55mV) was observed for the same electrode in air. This potential shift was very close to the theoretical value of 46 mV (based on Nernst Equation, more details can be found in Supporting Information). The Tafel slopes of IS-NiOC electrode were 93.4 mV·dec -1 and 92.3 mV·dec -1 in air and pure oxygen, respectively, indicating that the decrease of oxygen concentration did not affect the ORR kinetics signi cantly.
It was found that the ORR performance of the IS-NiOC electrode was highly dependent on the PTFEmodi cation parameters, as shown in Fig. 3j. A very limited current density (1 mA cm -2 at 0V) was observed on the electrode without PTFE-modi cation, mainly because of the weak oxygen bubble adhesion capability ( Supplementary Fig.12). The IS-NiOC electrode soaked in a diluted PTFE concentration (0.05 wt%) cannot afford a strong oxygen bubble adhesion, whereas increasing the concentration would impede the electron transport. These two metrics should be simultaneous optimized for achieving a superior current density. After intensive experimental efforts, an optimal PTFE concentration came to 0.1 wt%. More noteworthy, a signi cantly prolonged 2e ORR stability was observed on IS-NiOC electrode when performing air reduction in neutral system. Under the same test condition, the IS-NiOC electrode (modi ed by 0.1 wt% PTFE) could continuously produce H 2 O 2 (~25 mA·cm -2 ) for over 200 h (navy plots in Fig. 3k), while the promising initial current density was only maintained for a few hours (<10 h) for D-NiOC electrode with the same mass loading (dark red plots in Fig. 3k). It is worth mentioning that, the H 2 O 2 selectivity was kept at a stable value (~90%) during all the processes for both IS-NiOC and D-NiOC electrodes, indicating that the decay of the D-NiOC electrode was not caused by catalysts degradation. In a deeper analysis, it is revealed that both the IS-NiOC electrode and D-NiOC electrode suffered from the surface corrosion from the H 2 O 2 production since the surface liquid contact angles (LCAs, Supplementary Fig. 13) got a variable decrease after a period of running. The signi cant difference is attributed to the robust TPCP of IS-NiOC electrode which could alleviate the corrosion to a great extent. To validate this assumption, an IS-NiOC electrode with a thinner gas lm (soaked in 0.1 wt% PTFE for shorter time, ~8 min) was subject to a stability running. As expected, the latter one showed a slightly worse stability (red plots in Supplementary Fig. 14). Based on the above information, we believe that the robust gas diffusion layer plays a vital role in stability enhancement. The surface properties of IS-NiOC electrode and D-NiOC electrode before and after long-term reaction were thus characterized in detail. The air diffusion side for both IS-NiOC and D-NiOC electrodes is still intact after long-term testing, indicating that oxygen can be continuously diffused into the electrode. However, as for the water diffusion side, the IS-NiOC and D-NiOC electrodes show a considerable difference in the a nity to water.
As shown in Supplementary Fig. 13, a signi cant decrease on LCA (from 150.8° to 53.9°) was found for the D-NiOC electrode after long-term testing, while a slight decrease (from 154.2° to 119.5°) was observed in the LCAs of the IS-NiOC electrode. Considering the ORR reaction only occurred at TPCP, the fast-current density degradation was directly caused by TPCP vanishment.
EF-like performance of IS-NiOC electrode. Electrochemical advanced oxidation processes (EAOPs) have attracted substantial attention owing to the environmental versatility, high e ciency and safety 54 . Among all the EAOPs, the EF process is most popular, in which the oxidant (H 2 O 2 ) is formed in-situ from oxygen at the cathode surface in acidic solutions. However, generation of large values of iron-containing sludge and limited operating pH range (an optimal run is performed at pH ~3) of EF process urges the development of EF-like process which can be operated in a completely heterogeneous and neutral system. 55,56 Besides stable and fast H 2 O 2 generation, a desirable electrode should also possess the capability to activate H 2 O 2 to degrade organic pollutants (i.e. Fenton-like process) [57][58][59] . It is reported that H 2 O 2 can be activated to reactive oxygen species (ROS) along with the valence state change of Ni in Nibased catalysts 60 . In this case, we thus evaluated the Fenton-like performance of NiOC catalyst in neutral system and observed that NiOC catalyst exhibited a more effective degradability compared with that of O-C catalyst under the same experiment conditions (Supplementary Fig. 15). Thus, combining the advantages of rapid H 2 O 2 production and Fenton-like activity in neutral system, the IS-NiOC electrode is supposed to show a high EF-like performance.
To evaluate the EF-like performance, a steady-state three-electrode system enabling on-site H 2 O 2 production and in-situ organic (Indigo) degradation was constructed, as shown in Fig. 4a. A Na on membrane was adapted to separate the cathode and anode reaction, which could avoid the oxidation of generated H 2 O 2 on the anode surface. The IS-NiOC electrode was employed as the cathode to reduce oxygen to H 2 O 2 , which was further converted to ROS assisted with NiOC catalyst. As shown in Fig. 4b and   4c, the IS-NiOC electrode took 60, 40 and 24 minutes to complete degrade Indigo (50 ppm in 15 ml) under the current densities of 10, 20, and 50 mA cm -2 , respectively. In order to simulate the industrial pollutants degradation process, a two-electrode device (without any membrane) with an electrolyte circulating system was constructed, as schemed in Figure 4d and Supplementary Fig. 16. The IS-NiOC electrode was employed as the cathode and the dimensionally-stable boron-doped diamond (BDD) electrode was used as the anode. The employment of BDD electrode enables accelerated organics degradation process as it is well-known to produce strong oxidant (hydroxyl radical, ·OH) through the discharge of water at high oxidation potentials. The oxygen gas owed over the anode surface to provide reactant gas, and 50 mL electrolyte containing representative organic pollutant (50 ppm bisphenol A in 0.05 M Na 2 SO 4 ) owed through the channel. As shown in Fig. 4e, both the BPA and total organic carbon (TOC) removal rate increased under an operation current of 40 mA (the operation voltage is almost constant at ~3.3 V). After 8 hours reaction, the BPA and TOC removal rate reached ~95% and ~ 62%, respectively. Overall, the results demonstrated the great application potential of IS-NiOC electrode in EF-like process for wastewater treatment.

Discussion
In conclusion, we have successfully fabricated an integrated and superaerophilic electrode with a hierarchical architecture of NiOC catalyst for fast and stable H 2 O 2 electrochemical generation in neutral media. The NiOC catalyst was demonstrated effective in selective production of H 2 O 2 from electrochemical oxygen reduction, and the superaerophilic surface property further accelerated both oxygen diffusion and electron transport rates, thereby greatly improving the 2e ORR current density and stability. We also demonstrated the application of IS-NiOC electrode in EF-like process, which realized effective degradation of representative organic pollutants. The concept and principles in this work should be applicable for designing electrochemical H 2 O 2 production electrodes in the future.

Method
Synthesis of IS-NiOC electrode: The IS-NiOC was fabricated by a three-step method. Firstly, Ni(OH) 2 nanosheets were constructed on microporous carbon ber paper (CFP, fuel cell store) by solvothermal method. In a typical procedure, Ni(NO 3 ) 2 ·6H 2 O (1 mmol) and CO(NH 2 ) 2 (10 mmol) were dissolved in 36 mL of methanol to form a clear solution by continuous stirring. CFP which was pre-treated by oxygen plasma and the as-obtained solution were transferred to a 40 mL Te on-lined stainless-steel autoclave. Then, the autoclave was kept at 120℃ for 12 hours, and then allowed to cool down to room temperature naturally. Thus, the Ni(OH) 2 nanosheet arrays on CFP were obtained and subsequently rinsed with distilled water and ethanol each for 5 min with the assistance of ultrasonication, and dried at 80℃ for 2 hours. Secondly, the Ni(OH) 2 @CFP nanosheet arrays was propped on a porcelain boat which was lled with polyoxyethylene (PEO, Mv~10,000) powder and the porcelain boat was put into the tube furnace with an Ar gas ow (40 sccm). The tube furnace was heated up to 900 ℃ in 90 min and was held at that temperature for 3 hours to carbonize the PEO and grow carbon materials in-situ on the CFP. The distance between the CFP and the PEO powder was kept between 0.5 and 1 cm, and the PEO amount was kept between 0.5 and 2 g. Lastly, the as-prepared NiOC electrode was soaked in PTFE (0.1 wt%) for 10 min, and then heated at 350 ℃ for 30 min in air atmosphere. The mass loading of the catalyst was measured as ~3mg cm -2 .
Synthesis of D-NiOC electrode: The same mass loading (~3mg·cm -2 ) of the NiOC catalyst was fabricated by the drop-casting method. Speci cally, the NiOC catalyst was dispersed in ethanol solution with a concentration of 1 mg mL -1 . Then the solution with NiOC was loaded on PTFE modi ed CFP by dropcasting.
Synthesis of O-C catalysts: 1g active carbon and 1g PEO was put into the tube furnace after mixing up, the tube furnace was heated up to 900℃ in 90 min and held for 3 hours under Ar atmosphere.
Characterizations: The structural information of sample was characterized using eld-emission SEM (Zeiss SUPRA 55) operating at 20 kV and high-resolution TEM system (JEOL 2100) operating at 200 kV. XPS spectrum was carried out by using a model of ESCALAB 250. X-ray powder diffraction patterns were recorded on an XRD (Rigaku D/max 2500) at scan rate of 10° min -1 . The aberration-corrected HAADF-STEM measurements were taken on a JEM-ARM200F instruments at 200 keV. X-ray absorption spectroscopy (XAS) was conducted at the Shanghai Synchrotron Radiation Facility (SSRF).
Surface Characterizations to Oxygen Bubbles: This study characterized the wetting ability of the electrodes by measuring the contact angles of a Na 2 SO 4 solution using Optical contact angle and Surface/interfacial tension measuring system (OSA 60G, LAUDA Scienti c, Germany). For these experiments, 50 μL of the electrolyte were dropped on the electrode surface, and the LCA was measured in ambient air at room temperature. The air-bubble CA with the volume of ~50 μL was measured by the captive-bubble method.
Electrochemical RRDE Characterizations: For the preparation of the catalytic electrodes, the NiOC catalysts were dispersed in ethanol to achieve a catalyst concentration of ~5 mg·mL -1 with 5 wt% Na on solution. After sonication for 60 min, 10 μL of the catalyst ink was drop-dried onto a glassy carbon disc (area: 0.247 cm 2 , PINE). The electrochemical tests were performed in a computer-controlled CHI working station (Shanghai CHENHUA) with a three-electrode cell at room temperature. The glass carbon electrode loaded with catalyst was used as the working electrode. A graphite rod and a Ag/AgCl were used as the counter and reference electrode, respectively. 0.1 M phosphate buffered saline was chosen as the electrolyte. The ORR activity and selectivity were investigated by polarization curves and rotating ring-disk electrode measured in oxygen-saturated electrolyte at a scan rate of 10 mV·s -1 . where I R is the ring current, I D is the disk current, N is the collection e ciency (experimental calibration (~0.35) in Supporting Information (Supplementary Fig. 5)).
Practical Electrochemical Characterizations: To avoid the negative effect of Ohm resistance, an open system was employed to measure the current density (as shown in Supplementary Fig. 7). Practical ORR selectivity was performed in a two-compartment cell with Na on 117 membrane as separator. Both the cathode compartment and the anode compartment were lled with the same electrolyte (20 mLof 1 M Na 2 SO 4 or 1 M KOH). The electrolyte in anode compartment was saturated by oxygen gas, and 1 cm 2 electrode (IS-NiOC electrode, or D-NiOC electrode) was soaked in electrolyte as the working electrode. A Ag/AgCl or Hg/HgO electrode was employed as the reference electrode for neutral and alkaline systems, respectively. A graphite rod was placed in the cathode compartment as the counter electrode. To evaluate the H 2 O 2 selectivity, the electrode was operated for several minutes under a constant potential, then the electrolyte was collected to quantify the H 2 O 2 concentration. Theoretically, 1 C of electric quantity will produce 8.82 ppm H 2 O 2 (equation (2)) under this condition (20 mL electrolyte).
Electrochemical Air Reduction Characterizations: The electrochemical air reduction was performed by using the home-made device (as shown in Supplementary Fig. 10). A graphite rod and a Ag/AgCl were used as the counter and reference electrode, respectively. A owing 1 M Na 2 SO 4 solution was employed as the electrolyte. The selectivity was performed by calibrating the collected electrolyte.
Fenton-like degradation: A 50 mL of 10 mg/L RhB solution and 10 mg catalyst were transferred into the conical ask, as shown in Supplementary Fig. 15. The conical ask was kept under soni cation until the catalyst homogeneous dispersion. Then, the conical ask was xed on shaker and keep shaking for 12 hours to complete adsorption. 3 mL of 30 wt% H 2 O 2 was put into the solution. To analysis the concentration of the organic, 1 mL degradation solution was extraction, and 1 mL of 0.5 M Na 2 SO 3 was injected to stop the oxidizing of the remaining H 2 O 2 . After the centrifugation, the concentration was quanti ed by the UV-vis.
Steady State of electro Fenton-like degradation: An H-Cell was employed as the reaction device, and Na on 117 membrane as the separator. Both the cathode compartment and the anode compartment were lled with the same electrolyte (20 mL of 0.05 M Na 2 SO 4 and 50 ppm Indigo). The electrolyte in anode compartment was saturated by oxygen gas, and 1 cm 2 of IS-NiOC electrode was soaked in electrolyte as the working electrode. A Ag/AgCl was employed as the reference electrode and a graphite rod was placed in the cathode compartment as the counter electrode. The reaction current was set as 10, 20 and 50 mA, to collect the degrade tendency, 0.5 mL of the reaction solution was extracted and mixed with 0.5 mL Na 2 SO 3 . The concentration of Indigo was ensured by the UV-vis.
Flow State of electro Fenton-like degradation: The two-electrode and ow-state device was home-made, see details in Supplementary Fig. 16. The IS-NiOC electrode was employed as the cathode and the BDD electrode was employed as the anode (reaction on BDD electrode was as eq (3)). The working area for anode was 2*2 cm 2 , and the distance between cathode and anode was 2 mm. The oxygen gas owed in and out over the surface of the anode, and the electrolyte was pumped through the channel from the cathode by the peristaltic pump.

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