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WO2019035685A1 - Batterie redox - Google Patents

Batterie redox Download PDF

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Publication number
WO2019035685A1
WO2019035685A1 PCT/KR2018/009450 KR2018009450W WO2019035685A1 WO 2019035685 A1 WO2019035685 A1 WO 2019035685A1 KR 2018009450 W KR2018009450 W KR 2018009450W WO 2019035685 A1 WO2019035685 A1 WO 2019035685A1
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WO
WIPO (PCT)
Prior art keywords
anode
electrolyte
cathode
tank
cathode electrolyte
Prior art date
Application number
PCT/KR2018/009450
Other languages
English (en)
Korean (ko)
Inventor
정현진
김대식
최원석
김태언
정진교
서동균
김진후
Original Assignee
롯데케미칼 주식회사
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 롯데케미칼 주식회사 filed Critical 롯데케미칼 주식회사
Publication of WO2019035685A1 publication Critical patent/WO2019035685A1/fr

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    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/18—Regenerative fuel cells, e.g. redox flow batteries or secondary fuel cells
    • H01M8/184—Regeneration by electrochemical means
    • H01M8/188—Regeneration by electrochemical means by recharging of redox couples containing fluids; Redox flow type batteries
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04082—Arrangements for control of reactant parameters, e.g. pressure or concentration
    • H01M8/04201—Reactant storage and supply, e.g. means for feeding, pipes
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/04—Auxiliary arrangements, e.g. for control of pressure or for circulation of fluids
    • H01M8/04276—Arrangements for managing the electrolyte stream, e.g. heat exchange
    • H—ELECTRICITY
    • H01—ELECTRIC ELEMENTS
    • H01M—PROCESSES OR MEANS, e.g. BATTERIES, FOR THE DIRECT CONVERSION OF CHEMICAL ENERGY INTO ELECTRICAL ENERGY
    • H01M8/00—Fuel cells; Manufacture thereof
    • H01M8/18—Regenerative fuel cells, e.g. redox flow batteries or secondary fuel cells
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/50—Fuel cells

Definitions

  • the present invention relates to a redox flow cell, and more particularly, to a redox flow cell in which an anode tank and a cathode tank are connected by an overflow pipe.
  • the zinc bromine redox flow cell produces electricity by the redox reaction occurring between the electrolyte and the electrode.
  • a redox flow cell is formed by repeatedly laminating a bipolar electrode and a membrane, stacking a current collecting plate and an end plate sequentially on both sides of the outermost layer, A pump for supplying an electrolyte to the stack, a pipe for storing the electrolyte, and an electrolyte tank for storing the electrolyte to be discharged after the internal reaction in the stack.
  • the electrolyte tank is composed of an anode tank containing an anode electrolyte (anolyte) containing zinc, and a cathode containing a cathode electrolyte (catholyte) containing bromine And an electrolyte tank (catholyte tank).
  • the anode electrolyte tank and the cathode electrolyte tank are connected by an overflow pipe to supply the deficient electrolyte solution to each other.
  • the overflow tube connects the anode and the upper end of the cathode electrolyte tank to each other.
  • the internal pressure is changed due to the difference in the viscosity and the specific gravity of the electrolyte, resulting in a crossover.
  • the overflow pipe regulates the level of the anode and the cathode electrolyte.
  • the overflow pipe at the upper part moves the gas and the electrolyte from the cathode electrolytic solution (both electrolytic solution) to the anode electrolytic solution (negative electrolytic solution). Movement of the gas may reduce current efficiency.
  • the overflow pipe connecting the upper ends to each other can reduce the efficiency by introducing an electrolyte having a high specific gravity and viscosity generated in the cathode electrolyte tank into the anode electrolyte tank during charging / discharging.
  • One aspect of the present invention is to provide a redox-flow battery which prevents movement of gas generated during charging / discharging and moves the electrolyte.
  • One aspect of the present invention is to provide a method of controlling a level of an anode and a cathode electrolyte by moving only a cathode electrolyte having a low specific gravity and a viscosity to an anode electrolyte tank while shutting off gas and polybrominated gas generated in the cathode electrolyte, Flow cell.
  • the redox flow cell includes an anode electrolyte inflow line and an anode electrolyte inflow line connecting the anode electrolyte tank and the stack, a cathode electrolyte inflow line connecting the cathode electrolyte tank and the stack, and a cathode electrolyte inflow line
  • An anode electrolyte overflow tube having a first lower end immersed in the anode electrolyte in the anode electrolyte tank and a first upper terminal opened in the upper portion of the cathode electrolyte tank, 2, and a second upper end opened to an upper portion of the anode electrolyte tank.
  • the first lower end of the anode electrolyte overflow pipe may be located at 1/3 or more of the height (H) of the anode electrolyte tank.
  • the second lower end of the cathode electrolyte overflow pipe may be located at a half or more of the height (H) of the cathode electrolyte tank.
  • the anode electrolyte overflow pipe and the cathode electrolyte overflow pipe may be provided in plurality.
  • the anode and the cathode electrolyte tank are connected to the anode and the cathode electrolyte overflow pipe to block the gas and the polybenzene generated in the cathode electrolyte during charging / discharging,
  • the current efficiency can be increased because only the low cathode electrolyte is moved to the anode electrolyte tank to adjust the level of the anode and the cathode electrolyte. That is, the total energy efficiency can be increased.
  • FIG. 1 is a state diagram for blocking the movement of gas generated in a cathode electrolyte of a redox flow cell according to an embodiment of the present invention.
  • FIG. 2 is a perspective view showing a stack applied to FIG.
  • FIG. 3 is a sectional view taken along the line III-III in Fig.
  • FIG. 4 is a sectional view taken along the line IV-IV in Fig.
  • FIG. 5 is a perspective view of the anode, cathode, and electrolyte solution overflow tanks in FIG. 1; FIG.
  • FIG. 6 is a view illustrating a state in which a cathode electrolyte is moved in a redox flow cell according to an embodiment of the present invention.
  • FIG. 1 is a state diagram for blocking the movement of gas generated in a cathode electrolyte of a redox flow cell according to an embodiment of the present invention.
  • the redox flow cell of one embodiment includes a stack 120 for generating current in a redox reaction, and an anode, a cathode electrolyte, and an anode (not shown) An anode for respectively storing a cathode electrolyte, and cathode electrolyte tanks 210 and 220.
  • the redox flow cell of the embodiment includes an anode that connects the anode and the cathode electrolyte tanks 210 and 220 and the stack 120 via the anode and the cathode electrolyte pumps Pa and Pc, a cathode electrolyte inflow line La1, Lc1, an anode, and a cathode electrolyte discharge line La2, Lc2.
  • the anode and the cathode electrolytic solution flow into the stack 120 through the anode and the cathode electrolytic solution inflow line La1 Lc1 according to the driving of the anode and the cathode electrolytic solution pumps Pa and Pc, respectively.
  • the anode and the cathode electrolytic solution outflow lines La2 And Lc2 are stored in the anode and cathode electrolyte tanks 210 and 220, respectively.
  • a heat exchanger (207) is provided in the anode electrolyte outflow line (La2) through which the anode electrolyte flows out.
  • the heat exchanger 207 is disposed on the side of the anode electrolyte, which is less reactive than the cathode electrolyte, and directly contacts the anode electrolyte to increase the reactivity of the anode electrolyte. That is, the efficiency of the battery is improved.
  • electrolyte crossover occurs within the stack 120 due to viscosity and specific gravity difference of the electrolyte. This may cause a difference in the level of the electrolyte solution (L1a, L1c) in the anode electrolyte tank 210 and the cathode electrolyte tank 220.
  • the heat exchanger 207 can reduce the difference in the level of the electrolytic solution (L1a, L1c).
  • the anode electrolyte tank 210 accommodates an anode electrolyte containing zinc and the cathode electrolyte tank 220 (for convenience, a two-phase electrolyte tank containing two phases of the cathode electrolyte is not shown) Containing catholyte.
  • a middle cathode electrolytic solution having a high specific gravity and a high viscosity is accommodated in the lower part
  • a light catholyte having a specific gravity and viscosity lower than that of the middle cathode electrolytic solution is accommodated in the middle
  • the upper part accommodates the gas generated during charge / discharge.
  • the redox flow cell of the embodiment of the present invention further includes an anode and cathode electrolyte overflow pipes La3 and Lc3 for connecting the anode and the cathode electrolyte tanks 210 and 220 to each other.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 are formed in such a manner that when the internal pressure of the stack 120 changes due to the difference in viscosity and specific gravity of the electrolyte during charging and discharging, And the levels (L1a, L1c) of the anode and the cathode electrolyte in the anode and cathode electrolyte tanks 210, 220 are adjusted.
  • the anode electrolyte overflow pipe La3 is arranged so that the first lower end D1 constituting the lower portion thereof is inserted into the lower portion of the anode electrolyte tank 210 and immersed in the anode electrolyte, And the first upper end U1 constituting the upper portion is opened at an upper portion of the cathode electrolyte tank 220.
  • the cathode electrolytic solution overflow pipe Lc3 is disposed such that the second lower end D2 of the cathode electrolytic solution overflow pipe Lc3 is inserted into the lower portion of the cathode electrolytic solution tank 220 and immersed in the cathode electrolytic solution, (U2) is opened at an upper portion of the anode electrolyte tank 210.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 move the anode where the first lower end D1 or the second lower end D2 is immersed and the cathode electrolytic solution to the cathode on the opposite side and the anode electrolyte tanks 220 and 210 .
  • the cathode electrolyte overflow pipe Lc3 is disposed such that the second lower end D2 is preferably immersed in the light cathode electrolyte, as in the embodiment of the present invention, Only the cathode electrolytic solution can be moved to the anode electrolyte tank 210.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 are arranged so that the first lower end D1 and the second lower end D2 are respectively immersed in the anode and the cathode electrolytic solution, Gas and polybromine are prevented from moving to the anode electrolyte tank 210.
  • the anode and cathode electrolyte overflow pipes La3 and Lc3 may be provided in three embodiments, but the present invention is not limited thereto.
  • the anode and the cathode electrolyte overflow pipe La3, and Lc3 may be provided in one, or preferably three or more, in number.
  • FIG. 2 is a perspective view showing the stack applied to FIG. 1
  • FIG. 3 is a sectional view taken along line III-III in FIG. 2
  • FIG. 4 is a sectional view taken along line IV-IV in FIG. 2 through 4
  • the stack 120 includes a membrane 10, a spacer 20, and an electrode plate 30 that are repeatedly stacked.
  • the stack 120 further includes collectors 61 and 62 and end plates 71 and 72 which are sequentially stacked at both ends in the stacking direction and supply an anode and a cathode electrolytic solution to the electrode plate 30
  • An anode electrolyte channel CHa see FIG. 3
  • a cathode electrolyte channel CHc see FIG. 4
  • the electrode plate 30 includes one side of the anode electrode 32 and the other side of the cathode electrode 31.
  • the anode and cathode electrolyte channels CHa and CHc supply the anode and the cathode electrolyte to the anode and cathode electrodes 32 and 31, respectively.
  • the end plate 71 has an anode, an anode connected to the cathode electrolyte inflow lines La1 and Lc1, and cathode electrolyte inlets H21 and H31.
  • the end plate 72 has an anode, an anode connected to the cathode electrolyte outflow lines La2 and Lc2, a cathode electrolyte outflow ports H22 and H32, and an anode, a cathode electrolyte outlets H22 and H32, To the anode and cathode electrolyte channels (CHa, CHc).
  • anode and cathode electrolyte channels CHa and CHc are connected to the anode and cathode electrolyte inlets H21 and H31 at one end in the stack 120 and to the anode and cathode electrolyte outlets H22 and H32 at the other end .
  • the stack 120 also includes bus bars B1 and B2 which are disposed inside the end plates 71 and 72 and connected to the current collecting plates 61 and 62, respectively.
  • the bus bars B1 and B2 may discharge the current generated in the stack 120 or may be connected to an external power source 206 to charge the anode and cathode electrolyte tanks 210 and 220 with current.
  • FIG. 5 is a perspective view of the anode, cathode, and electrolyte solution overflow tanks in FIG. 1; FIG. 5, the anode electrolyte overflow pipe La3 may have a first lower end D1 at least one third of the height H of the anode electrolyte tank 210 according to an embodiment of the present invention. have.
  • the cathode electrolytic solution overflow pipe Lc3 may have a second lower end D2 at least one half of the height H of the cathode electrolytic solution tank 220.
  • the height settings of the first lower end D1 and the second lower end D2 can be variously changed as needed.
  • an anode which flows into and overflows into the anode and cathode electrolyte overflow pipes La3 and Lc3 through the height setting of the first lower end D1 and the second lower end D2,
  • the amount of the anode, the anode electrolyte overflowed, and the cathode electrolyte may be limited to those with low specific gravity and low viscosity.
  • the cathode electrolytic solution tank 220 there is a stagnant middle cathode electrolytic solution having a high specific gravity and viscosity.
  • the middle cathode electrolytic solution is supplied through the cathode electrolytic solution overflow pipe Lc3 at the same internal pressure as the light cathode electrolytic solution. Movement can be disadvantageous.
  • the second lower end D2 of the cathode electrolyte overflow pipe Lc3 is equal to or larger than a half of the height H of the cathode electrolyte tank 220, ) Can be immersed in the cathode cathode electrolyte to limit the overflow of the cathode cathode electrolyte and increase the efficiency.
  • anode electrolyte overflow pipe La3 can also increase the efficiency of the level control of the anode and the cathode electrolyte through the overflow by adjusting the height of the first lower end D1 similarly to the cathode electrolyte overflow pipe Lc3 have.
  • the first lower end D1 of the anode electrolyte overflow pipe La3 is connected to the second electrode of the cathode electrolytic solution overflow pipe Lc3 And may be disposed at a lower height than the lower end D2.
  • the height settings of the first lower end and the second lower end may be variously set as needed.
  • the anode electrolyte overflow pipe La3 has a first end U1 exposed to the cathode electrolyte tank 220 and the cathode electrolyte overflow pipe Lc3 has a first end U1 exposed to the cathode electrolyte tank 220, And an upper end U2.
  • the first and second upper ends are disposed above the anode and cathode electrolyte tanks 210 and 220 so that the anode and the cathode electrolyte can be prevented from flowing into the anode and cathode electrolytic solution tanks 210 and 220.
  • the second top U2 may be located above the first top U1. Therefore, the anode and cathode electrolyte moving to the first and second ends U1 and U2 do not interfere with each other at the second and first ends U2 and U1. However, although not shown, the second top U2 may be located below the first top U1 or at the same height.
  • the cathode electrolytic solution tank 220 further includes a gas discharge line Lc4 at the upper end thereof and a gas filter GF at the gas discharge line Lc4 to generate a cathode electrolytic solution Gas is discharged. Therefore, the gas generated from the cathode electrolyte and the polybromine do not move to the anode electrolyte tank 210.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 move the anode and the cathode electrolyte to the cathode and the anode electrolyte tanks 220 and 210 by the inner pressure at the bottom of the anode and cathode electrolyte tanks 210 and 220, respectively.
  • the cathode electrolytic solution tank 220 only the light cathode electrolytic solution having a low specific gravity and viscosity is moved to the anode electrolytic solution tank 210.
  • the first lower end D1 and the second lower end D2 are disposed so as to be immersed in the anode and the cathode electrolytic solution respectively, even if gas is generated in the cathode electrolytic solution tank 220 during charging / discharging, Lc3 in the anode-electrolyte tank 210 as shown in Fig. Therefore, as compared with the case of using the electrolyte tank of the prior art, the current efficiency increases in this embodiment, thereby increasing the total energy efficiency.
  • the anode electrolyte overflow pipe La3 has a first lower end D1 at least one third of the height H of the anode electrolyte tank 210 and the cathode electrolyte overflow pipe Lc3 has a cathode (H / 3) of the cathode electrolyte tank 220 because the second lower end D2 is provided at least one half of the height H of the electrolyte tank 220, The cathode electrolyte is not moved.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 are connected to the anode and the cathode electrolyte inflow lines La1 and Lc1 and the anode and cathode electrolyte overflow pipes La3 and Lc3 in order to match the flow rates of the anode and cathode electrolyte in the anode and cathode electrolyte tanks 210 and 220, May be set to be equal to or larger than the piping area of the cathode electrolyte outflow lines (La2, Lc2). To this end, a plurality of anode and cathode electrolyte overflow pipes La3 and Lc3 may be formed.
  • the anode electrolyte tank 210 includes an anode electrolyte containing zinc, and is driven by an anode electrolyte pump Pa, And the anode electrode 32 and receives the anode electrolyte discharged via the space between the membrane 10 and the anode electrode 32.
  • the cathode electrolyte tank 220 includes a cathode electrolyte containing bromine, and is disposed between the membrane 10 of the stack 120 and the cathode electrode 31 To the cathode side.
  • the cathode electrolytic solution tank 220 circulates the cathode electrolytic solution between the membrane 10 and the cathode electrode 31 of the stack 120 by driving the cathode electrolytic solution pump Pc.
  • the cathode electrolytic solution inflow line Lc1 and the cathode electrolytic solution outflow line Lc2 connect the cathode electrolytic solution tank 220 to the stack 120 with the four-way valve 205 interposed therebetween, And an outflow operation.
  • the four-way valve 205 may also connect the cathode electrolyte outlet H32 to the cathode electrolyte inlet H31 of the stack 120 to supply the cathode electrolyte together with the cathode electrolyte inlet line Lc1 back to the stack 120 have.
  • the stack 120 may be formed by stacking a plurality of unit cells C1 and C2.
  • this embodiment illustrates a stack 120 formed by stacking two unit cells (C1, C2).
  • the stack 120 further includes a flow frame, a membrane flow frame 40 and an electrode flow frame 50.
  • the stack 120 includes two unit cells C1 and C2 and therefore has one electrode flow frame 50 at the center and two membrane flows arranged symmetrically on both sides of the electrode flow frame 50.
  • Two end plates 71 and 72 are disposed on the outer surface of the frame 40 and the outer surface of the membrane flow frame 40, respectively.
  • the membrane 10 is configured to pass ions and is coupled to the membrane flow frame 40 in the thickness direction center of the membrane flow frame 40.
  • the electrode plate 30 is joined to the electrode flow frame 50 at the center in the thickness direction of the electrode flow frame 50.
  • the end plates 71 and 72, the membrane flow frame 40, the electrode flow frame 50, the membrane flow frame 40 and the end plates 71 and 72 are disposed and the membrane 10, And the stacks of the unit cells C1 and C2 are formed by joining the membrane flow frame 40, the electrode flow frame 50 and the end plates 71 and 72 to each other with the spacers 20 interposed therebetween. 120 are formed.
  • the electrode plate 30 has an anode electrode 32 formed on one side and a cathode electrode 31 on the other side in a portion where the two unit cells C1 and C2 are connected to form two unit cells C1 and C2. To form a bipolar electrode connecting in series.
  • the membrane flow frame 40, the electrode flow frame 50 and the end plates 71 and 72 are adhered to each other to set the internal volume S between the membrane 10 and the electrode plate 30,
  • the anode and cathode electrolyte channels (CHa, CHc) are configured to supply the anode and the cathode electrolytic solution, respectively, at equal pressures and amounts on both sides of the membrane (10).
  • the anode electrolyte channel CHa connects the anode electrolyte solution inlet H21, the internal volume S and the anode electrolyte outlet H22 to the membrane 10 and the anode electrode 32 by driving the anode electrolyte pump Pa. To allow the anode electrolyte to flow out after reaction.
  • the cathode electrolyte channel CHc connects the membrane electrode 10 and the cathode electrode 31 by driving the cathode electrolyte pump Pc by connecting the cathode electrolyte inlet H31, the internal volume S and the cathode electrolyte outlet H32.
  • the cathode electrolytic solution is allowed to flow into the internal volume S set between the anode and the cathode.
  • the anode electrolyte undergoes a redox reaction on the side of the anode electrode 32 of the internal volume S to generate a current and is stored in the anode electrolyte tank 210.
  • the cathode electrolytic solution is subjected to a redox reaction on the cathode electrode 31 side of the internal volume S to generate a current and is stored in the cathode electrolytic solution tank 220.
  • the bromine contained in the cathode electrolytic solution is produced and stored in the cathode electrolyte tank 220.
  • the zinc contained in the anode electrolyte is deposited on the anode electrode 32 and stored.
  • Equation 1 a reverse reaction of Equation 1 occurs between the membrane 10 and the cathode electrode 31, and an adverse reaction of Equation 2 occurs between the membrane 10 and the anode electrode 32.
  • the current collecting plates 61 and 62 in the stack 120 collect current generated in the anode electrode 32 and the cathode electrode 31 or supply the current to the anode electrode 32 and the cathode electrode 31 from outside And are electrically connected to the outermost electrode plates 30 and 30.
  • the anode electrolyte overflow pipe La3 is connected to the inner pressure of the anode electrolyte tank 210 because the first lower end D1 is provided in 1/3 or more of the height H of the anode electrolyte tank 210 in the charge /
  • the anode electrolyte of the level L1a flows into the first lower end D1 and moves to the cathode electrolytic tank 220 of the level L1c through the first end U1. At this time, the gas and the polybromine in the anode electrolyte tank 210 are not moved to the cathode electrolyte tank 220.
  • FIG. 6 is a view illustrating a state in which a cathode electrolyte is moved in a redox flow cell according to an embodiment of the present invention.
  • the cathode electrolyte overflow pipe Lc3 is connected to the cathode electrolyte tank
  • the cathode electrolytic solution of the level L2c flows into the second lower end D2 by the internal pressure of the anode 220 and moves to the anode electrolyte tank 210 of the level L2a through the second upper end U2.
  • the gas and the polybromine in the cathode electrolyte tank 220 are not transferred to the anode electrolyte tank 210.
  • the gas inside the cathode electrolyte tank 220 is discharged through the gas discharge line Lc4 and the gas filter GF.
  • the prior art connects the anode, the cathode electrolyte overflow tube to the anode, and the cathode electrolyte tank from above.
  • the anode and the cathode electrolyte overflow pipes La3 and Lc3 are inserted into the lower portions of the anode and cathode electrolyte tanks 210 and 220 to be opened at the top of the cathode and anode electrolyte tanks 220 and 210 Structure.
  • the prior art achieved a voltage efficiency of 80.7%, a current efficiency of 88.5% and an energy efficiency of 71.4%.
  • this embodiment achieved a voltage efficiency of 80.9%, a current efficiency of 90.4%, and an energy efficiency of 73.1%. That is, as a result of the charge / discharge efficiency test under the same conditions, the current efficiency and the energy efficiency of the present embodiment were higher than those of the prior art.
  • electrode plate 31 cathode electrode
  • heat exchanger 210 anode electrolyte tank
  • C1, C2 unit cell Cha: anode electrolyte channel
  • CHc cathode electrolyte channel D1, D2: first and second bottom
  • H21 anode electrolyte inlet
  • H22 anode electrolyte outlet
  • H31 cathode electrolyte inlet
  • H32 cathode electrolyte outlet
  • L1a, L1c, L2a, L2c level La1: anode electrolyte inflow line
  • La2 anode electrolyte outflow line
  • La3 anode electrolyte overflow tube
  • Lc1 cathode electrolyte inlet line
  • Lc2 cathode electrolyte outlet line
  • Lc3 cathode electrolyte overflow tube
  • Lc4 gas discharge line
  • Pa anode electrolyte pump Pc: cathode electrolyte pump

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  • Engineering & Computer Science (AREA)
  • Manufacturing & Machinery (AREA)
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Abstract

Un aspect de la présente invention est de fournir une batterie redox permettant de bloquer le mouvement d'un gaz généré et de déplacer un électrolyte pendant la charge ou la décharge. La batterie redox selon un mode de réalisation de la présente invention comprend : un conduit d'entrée d'anolyte et un conduit de sortie d'anolyte qui relient un réservoir d'anolyte et un empilement; un conduit d'entrée de catholyte et un conduit de sortie de catholyte qui relient un réservoir de catholyte et l'empilement; un tuyau de trop-plein d'anolyte ayant une première extrémité inférieure immergée dans un anolyte à l'intérieur du réservoir d'anolyte et une première extrémité supérieure ouverte au niveau du sommet du réservoir de catholyte; et un tuyau de trop-plein de catholyte ayant une seconde extrémité inférieure immergée dans un catholyte à l'intérieur du réservoir de catholyte et une seconde extrémité supérieure ouverte au niveau du sommet du réservoir d'anolyte.
PCT/KR2018/009450 2017-08-18 2018-08-17 Batterie redox WO2019035685A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR10-2017-0104969 2017-08-18
KR1020170104969A KR20190019703A (ko) 2017-08-18 2017-08-18 레독스 흐름 전지

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE9108939U1 (de) * 1991-07-20 1991-10-31 Müller, Karl-Heinz, 56307 Dürrholz Abtrennvorrichtung
KR101511228B1 (ko) * 2013-11-28 2015-04-10 롯데케미칼 주식회사 레독스 흐름 전지
US20160006054A1 (en) * 2014-07-07 2016-01-07 Unienergy Technologies, Llc Single capacity balancing in a redox flow battery
US20160111706A1 (en) * 2013-07-10 2016-04-21 Redflow R&D Pty Ltd Flowing Electrolyte Battery and Method of Controlling a Flowing Electrolyte Battery
KR20160064545A (ko) * 2014-11-28 2016-06-08 롯데케미칼 주식회사 징크-브로민 산화환원 흐름 전지 시스템

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE9108939U1 (de) * 1991-07-20 1991-10-31 Müller, Karl-Heinz, 56307 Dürrholz Abtrennvorrichtung
US20160111706A1 (en) * 2013-07-10 2016-04-21 Redflow R&D Pty Ltd Flowing Electrolyte Battery and Method of Controlling a Flowing Electrolyte Battery
KR101511228B1 (ko) * 2013-11-28 2015-04-10 롯데케미칼 주식회사 레독스 흐름 전지
US20160006054A1 (en) * 2014-07-07 2016-01-07 Unienergy Technologies, Llc Single capacity balancing in a redox flow battery
KR20160064545A (ko) * 2014-11-28 2016-06-08 롯데케미칼 주식회사 징크-브로민 산화환원 흐름 전지 시스템

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