Existing chlor-alkali processes generally use asbestos, mercury or fluorine-containing ion-exchange membranes to separate the simultaneous chlorine production on the anode and hydrogen production on the cathode, and form sodium hydroxide in the electrolyte. Here, using the Na+ de-intercalation/intercalation of a Na0.44MnO2 electrode as a redox mediator, we decouple the chlor-alkali process into two independent steps: a H2 production step with the NaOH formation in the electrolyte and a Cl2 production step. The first step involves a cathodic H2 evolution reaction (H2O → H2) and an anodic Na+ de-intercalation reaction (Na0.44MnO2 → Na0.44−xMnO2), during which NaOH is produced in the electrolyte solution. The second step depends on a cathodic Na+ intercalation reaction (Na0.44−xMnO2 → Na0.44MnO2) and an anodic Cl2 production (Cl → Cl2). The cycle of the two steps provides a membrane-free process, which is potentially a promising direction for developing clean chlor-alkali technology.
The chlor-alkali process plays a predominant and irreplaceable role in the chemical industry because its products are used in over 50% of all industrial chemical processes1,2,3,4,5,6,7,8,9,10,11. However, the chlor-alkali industry is among the highest energy-consuming processes with pollutant emissions that have a serious effect on the environment and human life1,2,3,4, 11,12,13,14,15,16. Accordingly, it is desirable to develop a more efficient and cleaner chlor-alkali process.
Typical chlor-alkali electrolysis (i.e. brine electrolysis) consists of two half reactions: the hydrogen evolution reaction (HER) on the cathode and the chlorine evolution reaction (CER) on the anode, which is accompanied by sodium hydroxide (NaOH) formation in the electrolyte. From 1888 till now, three processes emerged in the chlor-alkali industry: the diaphragm cell, mercury cell and present membrane cell1,2,3,4, 17, 18. In a diaphragm cell, a porous asbestos mat is used to separate the anodic CER and cathodic HER, and NaOH is simultaneously formed in the cathodic compartment (Supplementary Fig. 1)1,2,3,4. In the mercury cell, the CER on the anode is coupled with the formation reaction of sodium amalgam (2Hg + 2Na+ + 2e− → 2NaHg) on the liquid mercury cathode (Supplementary Fig. 2)1,2,3,4. Then, the sodium amalgam is separated and used in the second cell to produce NaOH via the anodic reaction of Na-ion release (NaHg → Na+ + Hg + e−) and the cathodic HER (Supplementary Fig. 2)1,2,3,4. The operation of the present membrane cell is very similar to the diaphragm cell, but the difference is to use a polymer ion-exchange membrane instead of the porous asbestos mat (Supplementary Fig. 3)1,2,3,4. Because of the separated formation of Cl2 and NaOH, the mercury cell generally produces a purer product than do the diaphragm and membrane cells but with higher energy consumption because of the increased cell voltage for electrolysis (Supplementary Fig. 2)1,2,3,4.
Over the past decades, many studies have been conducted to reduce the pollution related to chlor-alkali processes. The environmental measures implemented over the past several years have successfully alleviated the issue of huge mercury emissions. In the diaphragm and membrane process, the use of asbestos or fluorine-containing materials only causes indirect emissions. Because of the limited lifetime (approximately several years) of these materials, the diaphragm and membrane process only result in moderate environmental risks. Furthermore, the membrane cell has dominated the current chlor-alkali industry. The application of oxygen-depolarised cathodes in the membrane cell also reduces the electric energy consumption in the chlor-alkali process5, 19. However, the general applications of this membrane-based chlor-alkali process remain challenging. Although this method can facilitate the separation of the products because of its chemical resistance, the expensive ion exchange membrane generally exhibits limited useful life20,21,22,23,24,25,26,27. In particular, this membrane is susceptible to contaminant ions such as Mg2+ and Ca2+ in the brine, which shorten the useful lifetime of the membranes20,21,22,23. The precipitated calcium and magnesium will decrease the efficiency and increase the power consumption. In addition, the high-pressure gases in the electrolytic cell aggravate the membrane degradation28. Accordingly, unstable sustainable energy sources such as wind and solar energy are difficult to use to directly power the membrane cell, because the gas pressures in the anode and cathode compartments must remain in balance with a stable power input. Therefore, it is highly desired to develop an environmentally friendly, high-efficiency, membrane-free chlor-alkali process. In fact, the old mercury cell can be considered as a typical membrane-free chlor-alkali technology, where the redox mediator of amalgam/sodium amalgam (Hg/NaHg) decouples the H2 (and NaOH) production and Cl2 production. Unfortunately, because of the high toxicity, the mercury-cell-based chlor-alkali technology must be stopped step by step. However, the old mercury cell gives us the inspiration that the reversible Na+-storage reaction can decouple the chlor-alkali technology. In recent years, sodium-ion batteries (SIBs) are attracting extensive attention as a promising alternative candidate to lithium-ion batteries (LIBs) because of the abundant natural reserve and low cost of sodium29,30,31,32,33,34,35. The reversible Na+ intercalation/de-intercalation of the electrode is also expected to be used as a redox mediator to decouple the chlor-alkali technology.
Here we report a membrane-free chlor-alkali electrolysis process, where the Cl2 evolution and H2/NaOH production are decoupled by the reversible Na-ion intercalation/de-intercalation reaction of the Na0.44MnO2 electrode. This decoupled strategy shows promise in developing a clean chlor-alkali technology.
Mechanism of the two-step chlor-alkali electrolysis
As shown in Fig. 1a, the electrolysis process includes a H2 (+NaOH) production step (Step 1) in a NaOH solution and a Cl2 evolution step (Step 2) in a saturated NaCl solution. Step 1 involves the anodic Na+ de-intercalation from the Na0.44MnO2 electrode (Eq. 1) and the cathodic reduction of H2O on the HER electrode to produce H2 and OH− (Eq. 2). After being washed with brine, the Na0.44−xMnO2 (i.e. desodiated Na0.44MnO2, which is formed in Step 1) is used as the cathode in Step 2 for the Cl2 evolution, where the anodic Cl2 evolution reaction on the CER electrode (Eq. 3) is coupled to the cathodic Na+ intercalation in the Na0.44−xMnO2 electrode (Eq. 4). Steps 1 and 2 can be cycled by moving the Na0.44MnO2/Na0.44−xMnO2 electrode between cell 1 for Step 1 and cell 2 for Step 2 (Fig. 1a).
Step : 2
This approach creates a chlor-alkali electrolysis process with several important advantages. First, because of the environmentally friendly nature of Na0.44MnO2, this technology is cleaner than diaphragm cells, mercury cells and even the current membrane cells. Second, this architecture can separately produce H2 (+NaOH) and Cl2 without using a membrane. Finally, the separate generation of Cl2 and H2 prevents the mixing of product gases over a range of current densities and also simplifies the gas handling, which significantly increases the operational flexibility of chlor-alkali electrolysis cells and potentially make them suitable to be driven by sustainable energy sources (such as solar or wind energy).
Na0.44MnO2 with a three-dimensional (3D) S-shaped tunnel structure was prepared via a simple solid reaction (see the experimental section) according to previous reports36,37,38,39,40. The X-ray diffraction (XRD) pattern, scanning electron microscopy (SEM) image and transmission electron microscopy (TEM) image of the prepared sample are shown in Supplementary Figs. 4 and 5. Prior to the fabrication of this chlor-alkali electrolytic cell, the intercalation/de-intercalation behaviours of the Na0.44MnO2 electrode in an alkaline electrolyte (1 M NaOH) and a brine electrolyte (saturated NaCl) were investigated using cyclic voltammetry (CV) measurements with a typical three-electrode system (Supplementary Figs. 6, 7). As shown in Supplementary Figs. 6 and 7, the prepared Na0.44MnO2 exhibits identical electrochemical profiles in both electrolytes, which indicates a possibility of the reversible cycle between the desodiation (i.e. Na+ de-intercalation) in the alkaline electrolyte and the sodiation (i.e. Na+ intercalation) in the brine electrolyte of one Na0.44MnO2 electrode. To further clarify this point, the desodiation of a Na0.44MnO2 electrode in an alkaline electrolyte and consequent sodiation of the resulting electrode in a brine electrolyte were investigated using linear sweep voltammetry (LSV) measurements with a three-electrode system at a sweep rate of 2 mV s−1 (Fig. 1b). The HER on a Pt-coated titanium mesh electrode in an NaOH solution and CER on a RuO2/IrO2-coated titanium mesh electrode in a brine electrolyte were also investigated by LSV measurements for comparison (Fig. 1b). As shown in Fig. 1b (the red line), five desodiation peaks at −0.04, 0.08, 0.28, 0.34 and 0.49 V (vs. Hg/HgO) appear in the positive sweep process (from −0.2 to 0.55 V vs. Hg/HgO) in an alkaline electrolyte, and they indicate a desodiation reaction of Na0.44MnO2 → Na0.44−xMnO2 + xNa+ + xe−. Then, the resulting Na0.44−xMnO2 electrode was put in the brine electrolyte for the LSV measurement with a negative sweep from 0.55 to −0.2 V vs. Hg/HgO. As shown in Fig. 1b (the blue line), the sodiation peaks in the brine electrolyte appear at 0.38, 0.25, 0.16, −0.08 and −0.16 V vs. Hg/HgO in the negative sweep process. The potential gap between the main peaks of desodiation in the alkaline electrolyte and those of sodiation in the brine electrolyte is ~0.11 V, which indicates a good reversibility. Furthermore, the special potential window for the Na0.44MnO2/Na0.44−xMnO2 redox couple is between the onset potentials for the HER and CER (the green and black lines in Fig. 1b, respectively). The result indicates that Na0.44MnO2 can be used as a redox mediator to decouple the conventional chlor-alkali process into two steps, according to Fig. 1a. The galvanostatic charge–discharge curve of the Na0.44MnO2 electrode at a current density of 0.1 A g−1 is shown in Supplementary Fig. 8 to clarify the specific capacity of Na0.44MnO2.
Performance of the two-step chlor-alkali electrolysis
The chlor-alkali electrolytic process in Fig. 1a was constructed with a commercial Pt-coated Ti-mesh electrode for the HER (2.5 × 4 cm2, Supplementary Fig. 9a), a commercial RuO2/IrO2-coated Ti-mesh electrode for the CER (2.5 × 4 cm2, Supplementary Fig. 9b) and an Na0.44MnO2 electrode (2.5 × 4 cm2, Supplementary Fig. 9c). According to Fig. 1a, Step 1 (NaOH/H2 production) and Step 2 (Cl2 production) were conducted in two separated cells with the alkaline electrolyte and brine electrolyte, respectively. The electrolysis of the cells was investigated by chronopotentiometry with an applied current of 100 mA and a step time of 600 s, and the corresponding chronopotentiometry curves (cell voltage vs. time) are shown in Fig. 2a. The chronopotentiometry data of the anode (anodic potential vs. time) and cathode (cathodic potential vs. time) were also investigated during the electrolysis process and are shown in Fig. 2a. In Fig. 2a, Step 1 (i.e. the NaOH/H2 production process) exhibits an average cell voltage of ~1.3 V, which arises from the difference between the average anodic potential of 0.3 V (vs. Hg/HgO) of the desodiation (Na0.44MnO2 → Na0.44−xMnO2 + xNa+ + xe−) and the cathodic potential of approximately −1.0 V (vs. Hg/HgO) of the H2O reduction (2H2O → H2 + 2OH−). Then, after the washing with NaCl solution, the resulting Na0.44−xMnO2 formed in Step 1 was moved to another cell for Step 2 (the Cl2 production process). The average cell voltage in Step 2 was ~1.07 V, which is equal to the average potential difference between the anodic CER (2Cl− + 2e− → Cl2, ~1.24 V vs. Hg/HgO) and cathodic sodiation (Na0.44−xMnO2 + xNa+ + xe− → Na0.44MnO2, ~0.17 V vs. Hg/HgO). The photo profiles of the H2 generation in Step 1 and Cl2 generation in Step 2 are shown in Fig. 2b and c, respectively, to characterise the decoupled steps. Furthermore, video evidence is shown to further clarify the separated H2 generation in Step 1 and Cl2 generation in Step 2 (see Supplementary materials, Supplementary Movies 1 and 2). The electrolysis of the cells with a longer step time of 1 h (3600 s) was investigated by chronopotentiometry at an applied current of 100 mA (Supplementary Fig. 10). The chlor-alkali electrolytic process with the decoupled H2 (+NaOH) production and Cl2 production was further characterised by the chronopotentiometry measurements at the higher applied currents of 200, 500 and 1000 mA, respectively (Supplementary Fig. 11). The corresponding video proofs for the electrolysis at 1000 mA are shown in Supplementary Movies 3 and 4. When tested at a high current of 1000 mA ( = current density of 100 mA cm−2), the overall cell voltage (average voltages on Step 1 + Step 2) is ~3.65 V. Obviously, the applied current density (100 mA cm−2) is still much lower than the typical current densities in modern membrane cells (150–700 mA cm−2)8. For this case, the electrolysis rate in the cell is limited by the Na+ intercalation/de-intercalation in the crystalline framework of solid electrode material (Na0.44MnO2). An efficient solution for this issue is to reduce the current density (mA cm−2) applied on the Na0.44MnO2 electrode, which can be achieved by increasing the area (cm2) ratio between the Na0.44MnO2 electrode and the CER (or HER) electrode. For example, a higher applied current density of 500 mA cm−2 on the CER or HER electrode has been successfully achieved using this method (Supplementary Fig. 12). The kinetics of the Na+ or Li+ intercalation/de-intercalation also controls the power performance of current rechargeable Na-ion or Li-ion batteries. Various approaches such as nanosizing and nanostructuring electrode materials have been developed to improve the power of these rechargeable batteries41, which can also be used to improve the electrolysis rate of the new chlor-alkali process. According to the design in Fig. 1a, the H2/NaOH generation (Step 1) and Cl2 generation (Step 2) are performed in two separated cells: Cell 1 and Cell 2. In theory, both steps can be conducted in a single cell with the brine electrolyte (Supplementary Fig. 13a). However, the generated NaOH is dissolved in the brine electrolyte solution, which indicates that no pure NaOH stream is produced. Furthermore, with the increase of generated NaOH in the brine solution, the oxygen evolution reaction (OER) occurs on the CER electrode (Supplementary Fig. 13b). The separated cells can efficiently prevent the undesired issues, which is one of the purposes of the design in Fig. 1a. A conceptual design of the continuous production of the decoupled process is shown in Supplementary Fig. 14, and the technology challenges are briefly analysed in the corresponding discussion. According to recent reports about decoupled water electrolysis42,43,44,45, we can assume that the decoupled chlor-alkali process can be driven by an unstable renewable energy, which may improve the cost and efficiency of electrolysers.
As a typical electrode material for sodium-ion batteries, Na0.44MnO2 exhibits the high efficiency and long cycle capability, which were demonstrated in a previous report on a Na0.44MnO2-based aqueous battery39. To further clarify this point, the cycle performance of Na0.44MnO2 was investigated using a galvanostatic charge (in the 1 M NaOH solution)/discharge (in the saturated NaCl solution) test (Supplementary Fig. 15). Obviously, the highly reversible Na+ intercalation/de-intercalation behaviour of Na0.44MnO2 facilitates the cycle of NaOH/H2 production (Step 1) and Cl2 production (Step 2). Accordingly, the cycle profile of NaOH/H2 production and Cl2 production was investigated with an applied current of 100 mA. The achieved result is shown in Fig. 3, where the new chlor-alkali electrolytic process stably produced H2 (+NaOH) and Cl2 in over 50 consecutive cycles. For practical application, it is also necessary to clarify the durability of the Na0.44MnO2 electrode and its electrochemical stability in NaOH solution with higher concentrations. Therefore, the Na+ intercalation/de-intercalation behaviour of the Na0.44MnO2 electrode in the 10 M NaOH (30 wt %) solution was investigated by CV measurement at a scan rate of 2 mV s−1 (Supplementary Fig. 16), where the achieved electrochemical profile is identical to that in 1 M NaOH. This result demonstrates the high stability of Na0.44MnO2 in high-concentration alkaline solutions. Then, the 10 M NaOH solution was used to perform Step 1 for NaOH and H2 production (Supplementary Fig. 17). The electrochemical profile of Step 1 in 10 M NaOH is identical to that in 1 M NaOH.
Gas analysis of the H2 evolution and Cl2 evolution
As shown above, the new chlor-alkali electrolytic process involves the decoupled H2 (and NaOH) production step and Cl2 production step. To further confirm this point, in situ differential electrochemical mass spectrometry (DEMS) was used to measure the H2 evolution in Step 1 and Cl2 evolution in Step 2 with a constant applied current of 100 mA. In this experiment, a quadrupole mass spectrometer with a leak inlet was connected to the chlor-alkali electrolytic cell (the cell for Step 1 or Step 2) with two tubes as the purge/carrier gas inlet and outlet (see Methods and Supplementary Fig. 18 for details). A pure Ar gas stream was used as the purge gas before the electrolysis and the carrier gas during the electrolysis process. Prior to the gas analysis, the system was purged with a pure Ar stream for 1.5 h. Then, the system was purged with a pure Ar stream for an additional hour, and an online analysis record shows that H2 (Fig. 4a) or Cl2 (Fig. 4b) reached a stable background line. As shown in Fig. 4a, c, when the H2-production step (Step 1) begins, the H2 evolution is clearly observed in the online analysis record. In parallel with the H2 production, the NaOH is produced in the electrolyte solution because of the OH− generation in the HER at the cathode (Eq. 2) and Na+ de-intercalation from the Na0.44MnO2 anode (Eq. 1). After Step 1, a rest step of 130 min was performed with a pure Ar stream to eliminate the remnant H2 in the system, and a hysteresis of H2 was observed in the online analysis record (Fig. 4a). Then, the resulting Na0.44−xMnO2 electrode that was formed in Step 1 was washed with NaCl solution to remove the surface-adsorbed NaOH. The washed Na0.44−xMnO2 electrode was moved to another cell for the Cl2 production (Step 2) and the corresponding DEMS analysis. As shown in Fig. 4b, d, the Cl2 evolution is clearly observed in the online analysis record of DEMS during Step 2. However, it should be noted that the DEMS result shown in Fig. 4b cannot demonstrate the pure Cl2 production. It is almost impossible to fully avoid the parasitic OER reaction during the CER process8. This point will be further clarified by the yield analysis for H2 and Cl2. Furthermore, the Cl2 gas, which is generated at the anode, experiences immediate hydrolysis as follows: Cl2 + H2O → HClO + HCl46. As a result, only a part of the generated Cl2 gas is recorded by DEMS, which will be later confirmed. Step 1 is performed in an alkaline electrolyte (NaOH solution). Therefore, in theory, the NaOH generated in Step 1 is not mixed with other salts. However, the Na0.44MnO2 electrode is moved between the NaOH electrolyte in Step 1 and the brine electrolyte in Step 2, which can result in the presence of OH− (or Cl−) in the brine electrolyte (or NaOH electrolyte). Therefore, additional washing is necessary to remove the surface-adsorbed OH− (when moving from Step 1 to Step 2) or Cl− (when moving from Step 2 to Step 1), which is one of the disadvantages of the new chlor-alkali electrolytic process. This disadvantage is further clarified by the continuous production design shown in the discussion about Supplementary Fig. 14.
A typical drainage method (Supplementary Fig. 19a) was used to quantify the H2 or Cl2 generation over a specific time length. In this experiment, the produced H2 gas volume (mL) was measured with an applied current of 200 mA for 500 s (Supplementary Fig. 19b). The Faradaic efficiency was calculated from the ratio between the measured and theoretical H2 gas volumes. Supplementary Table 1 summarises the H2 production data obtained from five repeated experiments, where the Faradaic efficiency of the H2 production is ~100%. With the identical measurement condition, the obtained Cl2 gas volume is lower than that of H2 gas because some Cl2 that was generated at the anode undergoes hydrolysis (Cl2 + H2O → HClO + HCl). The HClO and Cl2 in the electrolyte were determined using the iodometric titration method (see Methods)47. The total chlorine that evolved because of the electrolysis of NaCl solution was determined by adding the chlorine in gas phase to the 'available chlorine' in liquid phase. The results of five repeated experiments, which are shown in Supplementary Table 2, indicate the average Faradaic efficiency of 90.2% for the Cl2 production, which is lower than that for H2 production. Furthermore, an ion-exchange membrane was used to evaluate the H2 production and Cl2 production with repeated experiments. In these experiments, the Na0.44MnO2 electrode and HER or CER electrode were separated by the membrane (Nafion film). The corresponding data from five repeated experiments are provided in Supplementary Table 3. The Faradaic efficiency of H2 production in the membrane cell is ~100%, which is as same as that achieved without membrane. It can be detected that the calculated Faradaic efficiency (97.4%) of Cl2 production with the use of membrane is still lower than 100%, indicating the presence of the parasitic OER reaction.
In summary, the Na+ intercalation/de-intercalation reaction has been successfully used to decouple the H2 (+NaOH) and Cl2 production in the conventional chlor-alkali electrolysis technology. The separated H2 (+NaOH) and Cl2 production in different compartments facilitates the membrane-free chlor-alkali process. This technology should be cleaner than the previous chlor-alkali electrolytic process because Na0.44MnO2 is environmentally friendly. Finally, as a typical Na-storage electrode material with low cost, Na0.44MnO2 can be easily produced on a large scale when using the conventional solid-state method. This work may open the door to build a cleaner chlor-alkali electrolysis technology, where the reversible Na+ storage in the electrode plays the role of a redox mediator to decouple the H2 (+NaOH) and Cl2 production. For example, the reversible Na+ adsorption/desorption in the porous carbon electrode of electrochemical double-layered capacitors can be used to decouple the conventional chlor-alkali electrolysis (Supplementary Figs. 20, 21 and Supplementary Movies 5, 6). Furthermore, the recent chlorine technology with oxygen-depolarised cathodes5, 19 can be decoupled by the reversible Na+ storage in an Na0.44MnO4 electrode (Supplementary Fig. 22). However, in the current state, the decoupled chlor-alkali process is still some way away from practical application. The movement of the battery electrode between Steps 1 and 2 and the corresponding washing processes requires a complex automation operation and advanced industrial design. The kinetics of the battery electrode reaction is still lower than that of the HER and the CER, so the advanced electrode is required to reduce the difference in kinetics. Other issues, such as the reachable concentrations, purity of products, required amount of Na0.44MnO2, parasitic OER reaction etc, also need to be solved in future research endeavours.
Synthesis and characterisation of Na0.44MnO2
Na0.44MnO2 was prepared using a solid-state reaction method with Na2CO3 (99%) and Mn3O4 (99.95%) as the precursor mixture. In the typical synthesis, stoichiometric amounts of Na2CO3 and Mn3O4 were ground by ball milling (Fritsch, Pulverisette 5) at 300 RPM for 5 h. The final products were obtained by sintering the resulted mixture in a muffle furnace at 775 °C for 10 h. Powder X-ray diffraction (XRD) patterns were collected using an X-ray diffractometer (D8 Advance, Bruker), which was equipped with Cu-Kα in the 2θ range of 10−60°. The size and morphology of the powdered samples were observed using FE-SEM (JSM-6390, JEOL) and field emission HRTEM (JEM-2010, JEOL).
Electrode fabrication and electrochemical test
The Na0.44MnO2 electrode was prepared according to the following steps. The active materials (70 wt %) were mixed well with acetylene black (8 wt %), multi-walled carbon nanotubes (8 wt %) and polytetrafluoroethylene binder (14 wt %) in isopropanol to form a homogeneous slurry. The slurry mixtures were treated with a roll press machine to form films. The films were dried in a vacuum oven at 80 °C for 12 h to remove the remaining solvent before pressing onto a titanium grid, which served as a current collector. The electrochemical profiles of the prepared Na0.44MnO2 electrode in an alkaline electrolyte (1 M NaOH) and a brine electrolyte (saturated NaCl) were investigated using cyclic voltammogram (CV) and galvanostatic charge–discharge measurements, respectively. The desodiation (i.e. Na+ de-intercalation) of the Na0.44MnO2 electrode in an alkaline electrolyte and consequent sodiation (i.e. Na+ intercalation) of the resulting electrode in the brine electrolyte were also investigated using LSV at a sweep rate of 2 mV s−1. The onset potential of the HER on a commercial Pt-coated Ti-mesh electrode in an alkaline electrolyte (1 M NaOH) and the onset potential of the CER on a commercial RuO2/IrO2-coated Ti-mesh electrode in a brine electrolyte (saturated NaCl) were investigated using LSvs. The aforementioned experiments were performed with a typical three-electrode method, where a Pt plate and Hg/HgO (0.098 V vs. NHE) were used as the counter and reference electrodes, respectively. All electrochemical measurements were performed on a PARSTAT MC multi-channel workstation (Princeton). In these experiments, the mass loading of Na0.44MnO2 in electrode was ~7 mg cm−2.
Fabrication of the electrolytic cell
The cell was constructed with a commercial Pt-coated Ti-mesh electrode (Supplementary Fig. 9a) for the HER, a commercial RuO2/IrO2-coated Ti-mesh electrode for the CER (Supplementary Fig. 9b) and a Na0.44MnO2 electrode (Supplementary Fig. 9c; the electrode preparation is provided in the discussion of Supplementary Fig. 9c). The HER (+NaOH formation) and CER were conducted in two separated cells, which were filled with 1 M NaOH and saturated NaCl, respectively. First, the Na0.44MnO2 electrode (2.5 × 4 cm2) was fixed by a platinum electrode cramp for the electrolysis (i.e. Step 1) in the NaOH solution. After the HER, the Na0.44MnO2 electrode was washed and transferred to the NaCl solution for the electrolysis of Step 2.
Chlor-alkali electrolysis investigation
The chlor-alkali electrolysis with two decoupled steps (i.e. Step 1 in cell 1 and Step 2 in cell 2) was investigated using chronopotentiometry measurements with applied currents of 100 mA. Step 1 was performed in cell 1 with 1 M NaOH electrolyte, in which the HER electrode (that is, Pt coated Ti-mesh electrode) and Na0.44MnO2 electrode were connected to the cathode and anode, respectively, of the power source for electrolysis. The duration time of Step 1 was 600 s with an applied current of 100 mA. Then, the Na0.44−xMnO2 electrode that was formed in Step 1 in cell 1 was washed with an NaCl solution to remove the adsorbed NaOH on the surface. The washed Na0.44−xMnO2 electrode was put into cell 2 with saturated NaCl for Step 2. In Step 2, the Na0.44−xMnO2 electrode and CER electrode (i.e. the RuO2/IrO2-coated Ti-mesh electrode) were connected to the cathode and anode, respectively, of the power source for the electrolysis. The cell voltages (V vs. time) of Steps 1 and 2 were recorded to characterise the electrolysis profile. With an additional reference electrode (i.e. the Hg/HgO electrode), the chronopotentiometry data (potential vs. time) of a single electrode (the HER electrode, Na0.44MnO2/Na0.44−xMnO2 electrode or CER electrode) were recorded in Steps 1 and 2. A PARSTAT MC multi-channel workstation was used to perform the chlor-alkali electrolysis investigation. The information about gas analysis is shown in Supplementary Fig. 18 and Supplementary Table 1–3.
Data supporting the findings of this study are available within the Article and its Supplementary Information file, and from the corresponding author upon request.
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We acknowledge funding support from the Natural Science Foundation of China (21622303, 21333002), National Key Research and Development Plan (2016YFB0901500) and Shanghai Science & Technology Committee (08DZ2270500).