A BATTERY SYSTEM

Abstract

The present invention relates to batteries and more particularly to battery systems. More particularly, the present invention relates to metal-air based battery systems. In an aspect of the present invention, there is provided a battery system, the system comprising (a) a cell comprising a metal anode and a cathode current collector, the metal anode and the cathode current collector separated by a separator; (d) a gas diffusion tank; and (e) an electrolyte between the cathode current collector and the gas diffusion tank, the electrolyte comprising redox molecules.

Claims

1. A battery system, the system comprising: (a) a cell comprising a metal anode and a cathode current collector, the metal anode and the cathode current collector separated by a separator; (b) a gas diffusion tank; and (c) an electrolyte between the cathode current collector and the gas diffusion tank, the electrolyte comprising redox molecules.

2. The system according to claim 1, wherein the redox molecules may be any molecule selected from the group comprising: a quinone derivative, an aromatic amine derivatives, a phenazine derivatives, a phenothiazine derivatives and quinoxaline.

3. The system according to claim 1, wherein the concentration of the redox molecules in the electrolyte is about 5 mM to 5M.

4. The system according to claim 1, wherein the separator selectively allows the passage of metal ions only.

5. The system according to claim 1, wherein the separator is any one selected from the group comprising: a lithiated Nafion or its composite membrane, and a lithium ion conductive ceramic membrane.

6. The system according to claim 1, wherein the metal in the metal anode is any metal selected from the group comprising: lithium, potassium, calcium, aluminium, zinc and magnesium.

7. The system according to claim 6, wherein the lithium metal electrode is a vinylene carbonate pre-treated lithium foil.

8. The system according to claim 7, wherein the lithium metal electrode further comprises a PVDF-Nafion composite membrane.

9. The system according to claim 1, wherein the cathode current collector comprises a porous conducting matrix.

10. The system according to claim 9, wherein the porous substrate is carbon felt.

11. The system according to claim 1, further comprising a pump to pump the electrolyte fluid between the cathode current collector and the tank.

12. The system according to claim 11, wherein the pump is a peristaltic pump.

13. The system according to claim 1, wherein the gas in the gas diffusion tank is oxygen and the pressure of oxygen in the gas diffusion tank is 1 atmosphere.

Description

[0019] In order that the present invention may be fully understood and readily put into practical effect, there shall now be described by way of non-limitative examples only preferred embodiments of the present invention, the description being with reference to the accompanying illustrative figures.

[0020] In the Figures:

[0021] FIG. 1. (a) and (b) show a battery system according to an embodiment of the present invention.

[0022] FIG. 2. (a) Cyclic voltammograms of EV and Lil in TEGDME. The scan rate is 0.10 V/s. The redox potential of Li.sub.2O.sub.2 is indicated for reference. (b) Discharge/charge curves of a RFLOB in the first 3 cycles. The current density is 0.05 mA/cm.sup.2. (c) The discharge curve of a RFLOB primary cell showing the high utilization ratio of lithium anode in the presence of 10 mM EV.sup.2+. The current density is 0.125 mA/cm.sup.2. (d) Discharge/charge curves and Coulombic efficiency of a RFLOB employing a PVDF-Nafion membrane at different cycle numbers. The current density is 0.125 mA/cm.sup.2. The electrolyte was 1.0 M LiTFSI in TEGDME containing 10 mM EV.sup.2+/10 mM I.sup.−, with a volume of 8 ml in (b), (c), and 4 ml in (d).

[0023] FIG. 3. X-ray photoemission spectroscopy (XPS) measurement of Li 1s and O 1s spectra and the corresponding peak deconvolutions. The upper and lower panels display those of the discharged and charged species in the GDT tank, respectively.

[0024] FIG. 4. (a-b) Field emission scanning electron microscopy (FESEM) images showing the morphology evolution of Ni foam after discharging (a) and re-charging (b) in the GDT tank. The insets illustrate the formation and decomposition of Li.sub.2O.sub.2 on the surface of Ni foam. (c-d) Transmission electron microscopy (TEM) and high-resolution TEM images showing the agglomerated nanoparticles (c) of Li.sub.2O.sub.2 and the lattice fringes (d).

[0025] FIG. S1. CV curves of 5 mM EV (a) and 5 mM Lil (b) in 1 M LiTFSI-TEGDME electrolyte at various scan rates (0.2, 0.1, 0.05, 0.02, 0.01 V/s). (c) Charge/discharge curves of 5 mM EV and 5 mM Lil in static cells with PVDF-Nafion membrane. The current density is 0.05 mA/cm.sup.2.

[0026] FIG. S2. Electron density difference maps associated with the interactions in Li.sub.2O.sub.2/I.sub.2 (a) and Li.sub.2O.sub.2/I.sub.3− system (b). Isovalues: |0.0012 a.u.|. I.sub.2 and I.sub.3 .sup.− are adsorbed on the (0001) surface of Li.sub.2O.sub.2 in parallel adsorption geometry. The blue and yellow zones correspond to electron density deduction and enhancement regions, respectively.

[0027] FIG. S3. Charge and discharge curves of RFLOB in the absence of redox mediators in the electrolyte. The current density was 0.05 mA/cm.sup.2.

[0028] FIG. S4. XRD pattern of the discharging products deposited on Ni foam in the GDT tank.

[0029] Diffraction peaks from Li.sub.2O.sub.2 are clearly identified (JCPDS File No. 01-074-0115) besides those from Ni foam.

[0030] FIG. S5. SEM photos show the morphology of pristine nickel foam before (a) and after (b) fully discharging the cell as indicated in FIG. 2c.

[0031] In the present invention, we demonstrate a novel design of redox flow Li-oxygen batteries. Resorting to the reversible redox targeting reactions, the formation and decomposition of Li.sub.2O.sub.2 could be reversibly achieved without using noble catalysts in a tank separated from the electrode, which could greatly alleviate the pore clogging effect of the insoluble Li.sub.2O.sub.2 and significantly lower the cost. With this novel working principle, lithium metal could be readily replaced by other metals such as aluminium, zinc, magnesium, etc., if proper electrolytes and redox molecules are employed, so that redox flow metal-air batteries could be built. Lithium is used here in a non-limiting example.

[0032] With reference to FIG. 1, there is provided a power generation redox flow metal-air battery system having a cell or cell stack 1 having a metal anode 2, a cathode current collector 3 and a separator membrane 4. The cathode current collector may be a porous current collector and the cathodic compartment may be filled with an electrolyte containing redox molecules. The separator membrane can prevent the crossover of redox molecules and allow lithium ions to pass through. The cell stack 1 constitutes a lithium metal anode and carbon felt cathode (2 cm×2 cm), separated by a membrane. A gas diffusion tank (GDT) is connected to the cathodic compartment through a pump. During discharge process, oxygen flows into the tank and is reduced to form Li.sub.2O.sub.2 while electrolyte fluid containing redox mediators and Li.sup.+ circulates between GDT and cell. During the discharging process, lithium metal in the anodic compartment is oxidized to Li.sup.+. Meanwhile, oxidized redox molecule 1 (RM.sup.1.sub.ox) in the cathodic compartment will be reduced on the porous current collector 3 to RM.sup.1.sub.red. The latter will then flow into the gas diffusion tank 9 with the help of pump 7. In embodiment, the gas diffusion tank 9 is an oxygen (O.sub.2) diffusion tank. In the tank 9, RM.sup.1.sub.red will further reduce O.sub.2 to O.sub.2.sup.− which will react with Li.sup.+ to form Li.sub.2O.sub.2. In the above process, RM.sup.1.sub.red will be oxidized to RM.sup.1.sub.ox, which will then flow back to the cell component and start a new cycle. The above process will continue until lithium metal is used up.

[0033] During the charging process, Li.sup.+ is plated in the anodic compartment. Meanwhile, reduced redox molecule 2 (RM.sup.2.sub.red) will be oxidized on the porous current collector 3 to RM.sup.2.sub.ox. The latter will then flow into the O.sub.2 diffusion tank 9 with the help of pump 7. In the O.sub.2 diffusion tank 9, RM.sup.2.sub.ox will further oxidize Li.sub.2O.sub.2 to form Li.sup.+ and O.sub.2. During this process, RM.sup.2.sub.ox is reduced back to RM.sup.2.sub.red, which will then flow back to the cell component and start a new cycle. The charge process will go on until all Li.sub.2O.sub.2 are used up.

[0034] The porous matrix 10 in the O.sub.2 diffusion tank 9 is used to improve the chemical reaction sites in the tank. The power supply or load 5 is used to provide electricity during charging process and consume electricity during discharging process.

[0035] The present invention will be described in detail and the corresponding electrochemical and chemical reactions are shown below in the example below.

EXAMPLE

Materials and Methods

[0036] 1. Materials

[0037] Tetraethyleneglycol dimethylether (TEGDME, 99%, Sigma-Aldrich) and lithium bis(trifluoromethane)sulfonimide (LiTFSI, Sigma-Aldrich) were used as solvent and lithium salt for electrolyte preparation. Ethyl viologen diperchlorate (EV, 98%, Sigma-Aldrich) and Lil (99%, Sigma-Aldrich) were employed as redox mediators for oxygen reduction and evolution reactions, respectively. Vinylene carbonate (VC, 97%, Sigma-Aldrich) was used to passivate Li metal and promote the formation of solid electrolyte interface (SEI) film on lithium surface. Prior to use, all the above chemicals were stored in an argon-filled glove box without exposure to air.

[0038] 2. RFLOB Cell Assembly

[0039] Lithium foil was pretreated by immersing in 1 M LiTFSI-TEGDME electrolyte containing 5 vol. % VC for 24 h and used as anode. Carbon felt was used as cathode current collector. The electrochemical cell was fabricated by sandwiching the lithium foil and carbon felt in a cell stack made of stainless steel, in which the two electrodes are separated by a Celgard 2300 separator. The size of the electrode is 2 cm×2 cm. The gas diffusion tank (GDT) is made of a glass vial loaded with nickel foam to construct gas diffusion layers and provide deposition site for Li.sub.2O.sub.2. Alternatively, the porous matrix in the tank can be any high surface materials having good chemcial stability toward O2 and redox electrolytes, such as glass fibre, plastics, etc. 8 ml electrolyte consisting of 10 mM Lil and 10 mM EV in 1 M LiTFSI-TEGDME was prepared and transferred into the GDT tank. The GDT tank has an inlet and an outlet for the electrolyte fluid and oxygen, respectively, and is connected with the electrochemical cell. Electrolyte fluid is circulated between the cell and tank by a peristaltic pump. The cell used for cycling test was fabricated with PVDF-Nafion membrane in place of Celgard separator. To speed up the testing, 4 ml electrolyte consisting of 10 mM Lil and 10 mM EV in 1 M LiTFSI-TEGDME was used. The preparation and evaluation of the PVDF-Nafion membrane will be reported elsewhere since it is beyond the scope of this study.

[0040] 3. Electrochemical Measurements

[0041] Cyclic voltammograms of the two redox molecules were measured with a three-electrode system at different scan rates (0.01, 0.02, 0.05, 0.1, 0.2 V/s). Lithium metal was used as counter and reference electrodes, and a Pt disk was used as the working electrode. The battery was tested at galvanostatic mode at different current densities. All the above electrochemical measurements were performed on an Autolab electrochemical workstation (Metrohm Autolab, PGSTAT302N).

[0042] 4. Characterizations

[0043] Field emission scanning electron microscopy (FESEM) images were obtained on a Zeiss Supra 40 field-effect scanning electron microscope. Prior to the FESEM measurement, the Ni foam was taken out of the GDT tank and washed by acetonitrile for three times before drying in a vacuum oven at 80° C. for 24 h. High-resolution transmission electron microscopy (HRTEM) images were recorded with JEOL 3010F. The Ni foam sample was washed in acetonitrile for three times and sonicated for 20 min. The suspension was collected and dropped onto copper mesh for TEM measurement. The X-ray photoelectron spectroscopy (XPS) analysis was conducted on a Kratos Analytical Axis Ultra DLD Spectrometer. All the samples were protected by argon during the preparation and transfer processes. Powder X-ray diffraction (XRD) pattern was measured by a powder diffractometer (Bruker D8 Advanced Diffractometer System) with Cu Kα (1.5418 Å) source. The samples were sealed by Kapton film in the glove box with argon and then transferred outside to take XRD measurement.

[0044] 5. Computation Method

[0045] A two-dimensional slab model was adopted to simulate the stable Li.sub.2O.sub.2 (0 0 0 1) surface. First-principles calculations were performed by using the plane-wave technique implemented in Vienna ab initio simulation package (VASP). The generalized gradient approximation with the Perdew-Burke-Ernzerhof functional has been employed to describe the exchange-correction potential in all calculations. Projector-augmented wave potentials were employed to describe the electron-ion interaction and a cutoff energy is set to 400 eV.

[0046] In general, one should note that these two molecules would not chemically react with each other upon operation. During discharging, both of the molecules will subsequently be reduced to I.sup.31 and EV.sup.+ in the cell. Similarly during charging, both of molecules will subsequently be oxidized to EV.sup.2+ and I.sub.2. So it is unlikely that both I.sub.2 and EV.sup.+ co-exist in the catholyte causing reaction between the two.

[0047] As a preliminary proof-of-concept study, we do not attempt to study the influences of the flow rate and other operation parameters on the overall device performance before the following factors are optimized: firstly, the PVDF—Nafion membrane is resistive, which makes up a big IR drop. Secondly, the sluggish reaction between I.sub.2 and Li.sub.2O.sub.2 and those of I.sup.− on the electrode account for a major loss of overpotential during charging. As a result, the discharging/charging current density is relatively low.

[0048] 6. Discussion

[0049] In the present application, we demonstrate a new implementable solution—rechargeable redox flow Li—O.sub.2 battery (RFLOB) to tackle the critical issues confronted by non-aqueous Li—O.sub.2 batteries. As illustrated in FIG. 1, the RFLOB has a gas diffusion tank (GDT) connected to the electrochemical cell stack. Electrolyte fluid is circulated between the tank and cell by a peristaltic pump, in which for the first time we concurrently introduced two different redox mediators to catalyze the O.sub.2 reduction and evolution reactions during discharging and charging processes, respectively. As a result, the use of conventional electrocatalysts on the cathode has been completely avoided. The GDT tank is filled with porous material allowing the easy access of redox fluid and O.sub.2, in which the O.sub.2 pressure is kept constant through a gas inlet and outlet. During discharging process, redox mediator RM.sub.1 is reduced at cathode and flows into the GDT tank where it is oxidized by O.sub.2 in the presence of Li.sup.+:

RM.sub.1.sup.ox+e.sup.−.fwdarw.RM.sub.1.sup.red(electrochemical reaction on cathode)  (1)

Li.sup.++RM.sub.1.sup.red+O.sub.2.fwdarw.Li.sub.2O.sub.2+RM.sub.1.sup.ox (chemical reaction GDT)  (2)

[0050] In this process, Li.sub.2O.sub.2 is formed and deposited in the porous matrix of the GDT tank. The regenerated RM.sub.1 then flows back to the cell for a second round of reactions. During charging process, another redox mediator RM.sub.2 is oxidized at cathode and flows into the GDT tank where it is reduced by Li.sub.2O.sub.2 releasing O.sub.2.

Rm.sub.2.sup.red.fwdarw.RM.sub.2.sup.ox+e.sup.−(electrochemical reaction on cathode)  (3)

Li.sub.2O.sub.2+RM.sub.2.sup.ox.fwdarw.Li.sup.++RM.sub.2.sup.red+O.sub.2 (chemical reaction in GDT)  (4)

[0051] As the formation of Li.sub.2O.sub.2 occurs in the tank, surface passivation and pore clogging of the cathode are essentially avoided. In theory, the capacity of the cell would just be limited by the size of GDT tank should sufficient Li metal be used in the anodic compartment. In addition, as the redox mediators generally have fast reaction kinetics, low-cost carbon felt could be used as the cathodic current collector even without electrocatalyst, which is however indispensible in conventional Li—O.sub.2 batteries. As such, a “catalyst-free” Li—O.sub.2 battery could be developed, which is distinct from the conventional Li—O.sub.2 cells.

[0052] The redox potential of Li.sub.2O.sub.2 in aprotic solvent is ˜2.96 V vs. Li/Li.sup.+. Considering the redox potentials of ethyl viologen (EV) and iodide, which are ˜2.65 V for EV.sup.+/EV.sup.2+ and ˜3.10/3.70 V for I.sub.−/I.sub.3.sup.31/I.sub.2 (FIG. 2a), just straddle that of Li.sub.2O.sub.2, these two redox species were identified as the mediators for oxygen reduction and evolution reactions in RFLOB, respectively. The potential difference between the mediators and Li.sub.2O.sub.2 provides the necessary thermodynamic driving force for the formation and decomposition of Li.sub.2O.sub.2 via redox targeting reactions, of which the lower potential of EV.sup.+ enables the reduction of O.sub.2 forming Li.sub.2O.sub.2 during discharge process (reaction 2), while the relatively positive potential of triiodide or iodine facilitates the oxidation Li.sub.2O.sub.2 during charge process (reaction 4). Both redox mediators have been tested in static cells and showed good reversibility (FIG. S1).

[0053] In an embodiment, the RFLOB was fabricated with a GDT tank filled with 8 ml redox electrolyte consisting of 10 mM EV.sup.2+/10 mM and 1.0 M lithium bis(trifluoromethane) sulfonimide (LiTFSI) in tetraethyleneglycol dimethylether (TEGDME). The O.sub.2 pressure in the tank was kept at 1 atmosphere. Vinylene carbonate pretreated lithium foil was used as anode in the electrochemical cell to preclude the reaction with redox mediators, since the Celgard® separator is unable to block the crossover of the redox mediators. The cell was discharged and charged in galvanostatic mode and the voltage profiles are shown in FIG. 2b. In the first discharging process, only a single voltage plateau at ˜2.70 V was observed, which matches the reduction of EV.sup.2+. However, noting the theoretical discharge capacity of EV.sup.2+ to EV.sup.+ is only ˜2 mAh, the much-extended capacity (here the cell capacity was controlled at 6 mAh) implies the reduction of O.sub.2 by EV.sup.+ in the GDT tank, forming EV.sup.2+ and Li.sub.2O.sub.2 as revealed later. The regenerated EV.sup.2+ then flows back to the cell and starts a second round of reduction meanwhile electricity is generated. In theory, the above discharge process could carry on until Li metal in the anode is used up and reaches the theoretical specific energy of the cell. For instance, in a non-constrained discharge process close to 80% lithium was converted into Li.sub.2O.sub.2 with relatively low overpotential loss in the presence of 10 mM EV.sup.2+ (FIG. 2c), which paves a way of making low-cost and extremely high-energy density Li—O.sub.2 primary cells.

[0054] During the charging process, two voltage steps appeared at ˜3.55 and 3.75 V (FIG. 2b). The oxidation of EV.sup.+ was not observed since most of EV.sup.+ have been oxidized to EV.sup.2+ by the surplus O.sub.2 in the tank. Hence the cell voltage shoots directly up to that for the oxidation of I.sup.− to I.sub.3.sup.− upon charging, at which there seemed very limited reaction between I.sub.3.sup.− and Li.sub.2O.sub.2 since the capacity extension at this voltage is rather small. Thereafter the voltage rises steadily until it reaches the second voltage plateau. Brown color was built up gradually in the electrolyte, indicating more and more polyiodide was produced. The high voltage plateau corresponds to the further oxidation of I.sub.3.sup.− to higher order polyiodides and eventually to iodine. The extended capacity at the high voltage indicates the reaction between iodine and Li.sub.2O.sub.2 was efficient which resulted in the oxidation of the latter and releasing O.sub.2.

[0055] The charge transfer process between Li.sub.2O.sub.2 and I.sub.2 is corroborated by theoretical calculations. FIG. S3 shows the electron density difference maps of I.sub.3.sup.− and I.sub.2 on Li.sub.2O.sub.2 (0001) surface in parallel adsorption geometry, where the blue and yellow zones correspond to electron density deduction and enhancement regions, respectively. Apparently there is a tendency of electron transfer from Li.sub.2O.sub.2 to both I.sub.3.sup.− and I.sub.2. The charge transfer is quantified by the Bader charge calculation to be 0.49 e.sup.− for Li.sub.2O.sub.2/I.sub.2, relative to that for Li.sub.2O.sub.2/I.sub.3.sup.−, indicating much more effective electron transfer in the former as compared to the latter.

[0056] In the subsequent discharging process, a short voltage plateau appeared at ˜3.30 V, attributed to the reduction of triiodide or iodine in the electrolyte. After that, the cell voltage kept stable at ˜2.70 V, exhibiting good reversibility of EV. In order to rule out the capacity from the direct reduction of dissolved O.sub.2 on the cathode, the cell was also tested in the absence of both redox mediators (FIG. S2). It is obvious that given the extremely low capacity, the reaction of dissolved O.sub.2 on the cathode has negligible contribution to the overall cell capacity. In general, one should note that these two molecules would not chemically react with each other upon operation. During discharging, both of the molecules will subsequently be reduced to I.sup.− and EV.sup.+ in the cell. Similarly during charging, both of molecules will subsequently be oxidized to EV.sup.2+ and I.sub.2. So it is unlikely that both I.sub.2 and EV.sup.+ co-exist in the catholyte causing reaction between the two.

[0057] The above results are very encouraging that, since the deposition of Li.sub.2O.sub.2 mainly occurs in the GDT tank, which intrinsically obviates the passivation and pore clogging of cathode in the cell, very stable voltage profiles with relatively low overpotentials were achieved in the first three cycles, even in the absence of catalysts. To prove the formation and decomposition of Li.sub.2O.sub.2 in the GDT tank, X-ray photoelectron spectroscopy (XPS) was employed to investigate the chemical states of Li and O for species formed in the tank at the end of discharge and charge. The signal associated with Li—F bond (56.6 eV) presents in all the samples (FIG. 3), presumably from the remained LiTFSI. The peak of Li—O—O—Li (55.0 eV) is clearly seen in the Li 1s spectra after discharging while nearly disappeared after charging. The existence of Li.sub.2O.sub.2 is further corroborated by O 1s spectra, where two large peaks assigned to the O1s (532.3 eV) from LiTFSI and Li—O—O—Li (531.2 eV) in Li.sub.2O.sub.2 are evidently observed. The latter then vanished after charging, in agreement with the Li 1s spectra. In order to confirm the formation of Li.sub.2O.sub.2 on Ni foam in the GDT tank, XRD measurement was carried out with the sample after full discharging. As the diffraction pattern shown in FIG. S4, the characteristic peaks of Li.sub.2O.sub.2 such as (101), (100) are clearly seen. These peaks are relatively broad in width in contrast to those from the Ni substrate, indicating the nanocrystalline nature of the formed Li.sub.2O.sub.2. In addition, some minor peaks, which may be assigned to LiOH and Li.sub.2CO.sub.3 phases, are also visible. These by-products may plausibly be introduced during sample transfer and/or XRD measurement, which were conducted in air. The XPS and XRD results were further substantiated by scanning and transmission electron microscopic measurements.

[0058] As the SEM images shown in FIG. 4, after discharging the smooth surface of pristine Ni foam (FIG. S5a) was covered by a layer of agglomerated particles (FIG. 4a), ENREF 38 which nearly disappeared with only little residual left after charging (FIG. 4b). This is consistent with the XPS measurement should the particles be Li.sub.2O.sub.2. The cell in FIG. 2c was also examined after full discharging, in which we expect much more product would be formed in the GDT tank. As revealed in FIG. S5b, not surprisingly, a much thicker layer of particulate precipitate was observed on the Ni foam. The particles are in round shape and 10-20 nm in diameter (FIG. 4c), which are crystalline in nature as revealed by the high resolution TEM. The lattice fringes of (101) and (100) crystal planes of Li.sub.2O.sub.2 are clearly identified (FIG. 4d), with d-spacing of 0.25 nm and 0.27 nm, respectively. This unambiguously confirms the formation of Li.sub.2O.sub.2 upon discharging.

[0059] The above results have convincingly validated the working principle of RFLOB. In order to assess the viability of the cell for long-term cycling, despite that it has yet been optimized and there are a few other critical issues to be addressed (such as the poor cyclability of lithium anode), we tested the cycling performance of the above RFLOB cell at a controlled discharging capacity (Li.sub.2O.sub.2 to redox molecules ratio is 1:1). A PVDF-Nafion composite membrane was employed to protect the lithium anode from being attacked by the redox mediators and dissolved O.sub.2 upon repeated striping and plating in long cycling process. As the voltage profiles shown in FIG. 2d, relatively large overpotential was observed due to the large IR drop across the membrane. Interestingly, with increasing cycle number, the overpotential of the cell decreased gradually, largely a result of the reduced resistance of the membrane over cycling. There isn't deterioration of charging capacity in the first 30 cycles. Instead, due to improved conductivity of the membrane, the charging capacity was even enhanced with the Columbic efficiency reaching nearly 100% after 10th cycle (FIG. 2d).

[0060] As a preliminary proof-of-concept study, we do not attempt to study the influences of flow rate and other operation parameters on the overall device performance before the following factors are optimized: Firstly, the PVDF-Nafion membrane is resistive, which makes up a big IR drop. Secondly, the sluggish reaction between I.sub.2 and Li.sub.2O.sub.2 and those of I.sup.− on the electrode account for a major loss of overpotential during charging. As a result, the discharging/charging current density is relatively low.

[0061] The above results provide compelling evidence and concertedly validate the functionality of RFLOB. That is, with the assistance of redox mediators, the discharging product Li.sub.2O.sub.2 could be remotely formed in the GDT tank and reversibly oxidized in the charging process without depositing onto the cathode inside the cell. Such decoupled reactions of Li.sub.2O.sub.2 provide great flexibility to circumvent the issues confronted by the conventional Li—O.sub.2 batteries. The surface passivation and pore clogging of the cathode resulted from Li.sub.2O.sub.2 precipitations, which is inevitable in conventional cells, are essentially avoided under the new operation mode. While the overpotential persists during the charging process, the intolerably large voltage hysteresis could in theory be mitigated by using suitable redox mediators even in the absence of electrocatalysts, which on the other hand is expected to also improve the cycling stability of the cell. In addition, the capacity of the cathode could be expanded by simply enlarging the size of GDT tank, which is however constrained by the pore volume of cathode and catalysts deposited on it in the conventional Li—O.sub.2 batteries. Moreover, as the reaction of O.sub.2 in GDT is far apart from the electrodes, the tolerance of the cell towards air would be enhanced as well.

[0062] While promising, to develop RFLOB into a viable device for advanced large-scale energy storage, the large voltage hysteresis would have to be further reduced. In the present study, the stagnant reaction between triiodide and Li.sub.2O.sub.2 and resistive Li.sup.+-conducting membrane represent the main causes of the large overpotential during charging process. Faster redox mediators with matched potential to the oxidation of Li.sub.2O.sub.2 are desired to expedite the reactions. In addition, optimization of the three-phase interface in the GDT tank to facilitate the reactions of O.sub.2 and Li.sup.+, and more effectively utilize the volume to accommodate Li.sub.2O.sub.2 is also required. Highly porous low-weight materials with good affinity to the deposition of Li.sub.2O.sub.2 and superior chemical resistance would be the ideal option. We are currently pursuing the above aspects to develop RFLOB into a low-cost and durable alternative to the Li—O.sub.2 batteries for large-scale energy storage applications.

[0063] In comparison with current metal-oxygen batteries, the present invention greatly alleviates the use of noble catalysts, dramatically lower the overpotential or polarization, and pore clogging of the cathode is avoided which leads to a lower cost, higher energy efficiency and improved capacity.

[0064] Whilst there has been described in the foregoing description preferred embodiments of the present invention, it will be understood by those skilled in the technology concerned that many variations or modifications in details of design or construction may be made without departing from the present invention.