• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    A system for generating or storing energy on an electrochemical basis comprises at least one flow cell, each of which consists of two electrolyte cells (21, 22) of different charge flow, separated by a membrane half cells, in which half cells at least one electrode is arranged , and one tank for each of the electrolyte liquids. In order to reduce or completely eliminate the adverse effect of hydrogen formation in the cell in a simple and inexpensive manner, a common gas volume (23) connecting the tanks is provided and at least one catalyst in the tank for the positive electrolyte liquid (22) (24) for the reduction of the positive reaction partner of the redox couple in contact with the positive electrolyte liquid (22) and with the common gas volume (23).
    公开号:AT512184A4
    申请号:T69/2012
    申请日:2012-01-23
    公开日:2013-06-15
    发明作者:Adam Dr Whitehead；Martin Harrer
    申请人:Cellstrom Gmbh；
    IPC主号:
    专利说明:

    FW-3460 AT
    System for power generation or storage on electrochemical
    Base
    The invention relates to a system for generating or storing energy on electrochemical basis, comprising at least one flow cell, each consisting of two flowed through by differently charged Eiektrolytflüssigkeiten, separated by a membrane half-cells, in which half-cells each at least one electrode is arranged, and one tank for each of the Eikktrolytflüssigkeiten, and in particular a system in which the electrolyte liquid in the positive half-cell in the charged state contains tetravalent and pentavalent vanadium, sulfuric acid and optionally other additives
    Almost every electrochemical energetic electrolyte system used in practice produces a certain amount of gaseous hydrogen. For redox flow batteries, especially vanadium redox flow batteries, this poses a particular problem since hydrogen is formed electrochemically at the negative electrode according to the reaction 2H + + 2e '<- * H2 and the desired reaction, for example V3t + e '&lt; - &gt; Vz + at the negative electrode obstructed.
    The strength of hydrogen evolution at the negative electrode is considerably higher than parasitic reactions (e.g., O 2 or C O 2 formation) at the positive electrode, resulting in a state-of-charge (SOC) difference at the positive and negative electrodes, respectively. For the vanadium battery, this has the consequence that after a certain period of hydrogen formation, the negative electrolyte more V3 + than the positive electrolyte V02 + contains. This reduces the capacity of the system.
    To account for this hydrogen formation or the imbalance in the charge state for redox flow batteries have been proposed different, but structurally and control-consuming solutions. Thus, according to NH Hawk, NASA redox storage system, development project, DOE / NASA / 12726-24, NASA Lewis Research Center, Cleveland, Ohio (1984) and US 4,159,366 for an Fe-Cr redox flow Battery suggested the use of rebalance cells. These consist inter alia of a hydrogen anode and an iron cathode, which are separated by an ion exchange membrane, and which are supplied with hydrogen on the side of the gas electrode. Later, a version was developed that prefers chlorine rather than hydrogen reduction. A similar solution is also presented in US 5258241.
    JP 07211347 discloses a rebalance cell, inter alia, for vanadium redox flow batteries, in which V02 + at one electrode of a cell divided by a membrane is reduced to V02 + and at the other electrode from aqueous sulfuric acid oxygen • t ♦ * · · · * ·· ♦ * »· *« · · * «
    12--2..1 .. FW-3460AT is created. This construction has similar Nachtale as the systems described in the previous paragraph. In addition, it is necessary that a periodic filling with water to avoid dehydration of the anode half-cell is necessary and for the production of the balance energy use (electrical energy) is necessary
    Rebalance cells must also be monitored in a complex manner, because too much carried by the cell charge of the electrolyte suffers a reduction in usable capacity, since the cell then in the opposite direction gets out of balance. For lead-acid batteries, gas reformers are known and common. However, it is not intended for use with redox flow batteries with electroactive species in solution. A catalyst is used here to re-adjust the charge state of the electroactive species.
    According to the invention, therefore, while avoiding the disadvantages mentioned above, a new solution is proposed, which is characterized in that a tank connecting the common gas volume is provided, and that in the tank for the positive electrolyte liquid at least one catalyst for the reduction of the positive reaction partner of Redox pair is arranged in contact with the positive electrolyte liquid and with the common gas volume. Thus, the system according to the invention does without additional cells with circulation, is passive and even active, without having to be actively pumped or forcibly discharged. The required hydrogen is formed within the system, does not have to be supplied externally, and is used to "discharge". of the positive electrolyte used instead of the "charge &quot; of the negative electrolyte.
    Furthermore, the frequent monitoring of the charge state necessary for rebalance cells can be avoided or considerably reduced for both electrolytes, which is provided there in order to determine the charge quantity for setting the charge state into a usable range. This is very expensive and also expensive.
    According to a first embodiment of the invention, the catalyst is arranged near an inlet and / or outlet for the electrolyte liquid. This ensures a constant flow over the catalyst without expensive equipment.
    Advantageously, the catalyst is applied to a floating on the positive electrolyte liquid arrangement, preferably on a membrane spanned on a frame, whereby in a simple manner the contact of the catalyst with the positive electrolyte liquid and the common gas volume is achieved.
    Another variant provides for this purpose that the catalyst is applied to a partially immersed in the positive electrolyte liquid tissue.
    In order to allow easy access of the hydrogen-containing gas to the catalyst and at the same time the access of the positive electrolyte to the other, • · * «·· • · *« ·· *: 3-
    To permit FW-3460 AT uncoated side, the catalyst advantageously has at least one gas diffusion layer, preferably containing conductive fibers.
    A particularly proven embodiment of an arrangement according to the invention is characterized in that catalysts based on platinum and / or iridium dioxide are provided.
    Preferably, the system of the invention is provided with means for establishing or maintaining a gas flow over the catalyst, which contributes to an improvement in the catalytic reaction.
    Vorteiihafterweise means for a pressure equalization of the common gas volume from the environment are provided according to another embodiment.
    All the above features are particularly advantageous and, while achieving the effects and advantages mentioned so far, are also used in a system for generating or storing energy on an electrochemical basis, in which the electrolyte liquid in the positive half-cell in the charged state is tetravalent and pentavalent vanadium, sulfuric acid and optionally contains further additives. Thus, the electrochemical cells are used for the charge as well as the discharge of the vanadium redox flow battery instead of just the discharge as in a redox fuel cell.
    Although the subject invention is intended primarily for use with vanadium redox flow batteries, it can in principle be applied to all types of redox flow batteries with aqueous electrolytes, for example also based on iron and chromium.
    In the following description, the invention will be explained in more detail by means of embodiments and with reference to the accompanying drawings.
    The Flg. Fig. 1 is a schematic representation of the tanks of a redox flow battery with a catalyst according to the invention near the inlet of the positive electrolyte. Fig. 2 is an advantageous structural embodiment of a catalyst according to the invention, and Fig. 3 is a diagram of that of a small electrochemical Cell generated electricity with short-term use of a catalyst according to the invention.
    Fig. 1 shows the tanks of a flow cell of a redox flow battery as a preferred example of an electrochemical-based power generation or storage system. In the tanks are the differently charged electrolyte liquids, which are circulated for energy generation or energy storage in the half-cells and then wei-the back into the tanks, the negative electrolyte liquid is denoted by 21 and the positive electrolyte liquid 22.
    The tanks may be spatially separate containers, but may also, as shown in Fig. 1, as two, divided by a partition compartments in a common
    Be formed container, which adjoin compartments directly. The positive electrolyte liquid may contain, for example, in the charged state tetravalent and pentavalent vanadium, sulfuric acid and optionally further additives. Above the electrolyte liquids 21, 22, a common gas volume 23 is preferably provided above the two tanks connecting these two tanks. In the case of a common container with two compartments for the electrolyte liquids 21, 22, the common gas volume 23 is formed by the non-divided by the partition area above the compartments. Furthermore, at least one catalyst 24 for the reduction of the positive reaction partner of the redox couple in contact with the positive electrolyte liquid and the common gas volume 23 is arranged in the tank of the positive electrolyte 22. As is apparent from Fig. 1, the catalyst 24 is advantageously so arranged so that the positive electrolyte liquid 22 periodically or continuously flows over one of the surfaces thereof, which is effected here by placing near the inlet 31 for the electrolyte liquid. A placement near the outlet would be possible.
    The catalyst 24 consists of a structure of catalytically active material or of a carrier coated with this material. By its arrangement, a portion of the catalyst 24 is caused to contact with the positive electrolytic liquid 22, and another portion is in contact with the gas containing hydrogen and formed on the negative electrode. Thus, a three-phase interface between the positive electrolyte 22, the gas in the volume 23 and the catalyst 24.
    Since the volume of the electrolyte liquids 21, 22 in the tanks, and thus the level of electrolysis, typically varies by a few centimeters (due to mass transport through the ion exchange membrane between the half cells), the catalyst 24 is either partially immersed in the positive electrolyte liquid 22 or, advantageously designed to track this height variation, for example, by running as a floating body with catalytically active coating. An example of this is shown in Fig. 2, which shows a buoyant frame 11, advantageously made of PVC, PE, PP or other stable material) with a membrane 12 spanned therein and catalytically coated.
    Suitable membranes can be ion exchange membranes (such as Nation® from DuPont) or microporous species (such as microporous polyethylene separators, often used in lead-acid batteries). The catalytically active coating may be present on one or both sides and could also be applied to conductive particles (such as industrial coal) with which the membrane is then coated (as is conventional in fuel cells). * «* * * • • • • * * -5 * ♦ · •» ♦ «· • * • · · · ♦ Φ« * «FW-3460 ΑΤ
    A catalyst similar to a gas diffusion electrode and membrane carrier would be conceivable. This comprises a catalytically active layer on a water-repellent, porous and electrically conductive layer. This may also contain additional electrically conductive fibers (especially graphite fibers such as a carbon fabric) to increase the active surface area for the reduction reaction. In addition, the water-repellent, porous and electrically conductive layer allows easy Zuthff of the hydrogen-containing gas to the catalyst material from one side, while the access of the positive electrolyte liquid to the other, uncoated side is maintained.
    In the case of the vanadium redox flow battery, this causes a reduction of V02 + in the positive tank using H2 formed at the negative electrode, thereby keeping the charge state the same in both tanks (ie, the average oxidation state of the vanadium at the initial value of 3.5 should be kept).
    The device according to the invention operates passively, i. without energy input from external sources, solely by the reaction between the gaseous hydrogen and the electroactive species in the charged-state positive electrolyte 22, for example the reaction V02 + + H + + WH2 <-► VOz + + H20. Although this reaction is thermally advantageous (AG0 ~ -97 kJ mol'1), it occurs only to a negligible extent at room temperature and without the presence of a suitable catalyst.
    Of course, a plurality of catalytic devices 24 may be provided in the tank of the positive electrolyte 22 to enhance the use of the hydrogen. Further, means may be provided for effecting gas flow across the catalyst 24, either active means or those for generating and directing convection flow.
    In principle, all possible substances can be used as catalytically active substances, in particular for the hydrogen reduction reaction in an acidic environment, finely dispersed Pt, Pt-Ru, Pt-Mo, Pt-W, Pt-Co-Mo, Pt-Co. W, Pd, Pt-Cr, IrO 2, etc. are advantageous. Important is sufficient stability against dissolution in the electrolyte.
    Since the consumption of the hydrogen gas can lead to a reduction in pressure in the gas volume 23 above the tanks relative to the environment, means for pressure equalization are advantageously provided, for example for introducing inert gas from a compressed gas source. On the other hand, overpressure due to the formation of hydrogen by dissipating the gas from the volume 23 via a line with integrated flame arrester can be reduced.
    Based on the following application examples, the advantages of the arrangement according to the invention will be explained.
    Application Example 1
    FW-3460 AT
    In a test system with a cell with a compartmentalized tank and common gas volume, fully charged positive and negative electrolytes were introduced, with the nominal positive electrolyte being 0.8 M (VO ^ jSO 3.2 M H2S04) and the negative electrolyte 1.6 M VS04, 2.4 M H2SO4. The cell was maintained at a constant 1.75 V so that the electrolytes were kept fully charged, continuously measuring the holding current.
    Hydrogen gas was pumped into the common gas volume above the tank until its concentration reached 90%, after which the tank was isolated and sealed. By means of a gas sensor, which operates in the absence of oxygen, the hydrogen concentration was measured continuously. The system was operated with a catalyst placed alone in the gas volume which was not in contact with the electrolyte, the holding current being measured constant at about 40 mA.
    Subsequently, a Ti02-coated Ti lattice was partially immersed in the electrolyte, so that about half of the lattice was in the positive electrolyte and the other half in the overlying gas volume. After about five minutes, an increase in current through the cell could be detected in response to a reduction in the positive electrolyte. After 39 minutes, the catalytic lattice was removed. The power remained above the baseline for a few minutes until the positive electrolyte was fully charged again. Then again a current of 40 mA turned on.
    Thus, the effectiveness of the catalyst for the reduction of the positive electrolyte by oxidation of hydrogen in the gas volume was detectable.
    Application Example 2:
    The above test was repeated with a graphite felt of 20 cm 2 area and 5 mm thickness wound around the lower immersed part of the IrO 2 coated Ti grid. The catalyst assembly remained submerged for 36 minutes, then was removed and then the excess charge was measured.
    The results were as follows:
    Charge [mAh] Immersion Time [h] Equivalent Rebalance Current [mA] Ir02-Ti 11.5 0.63 18 Ir02-Ti + Graphite Felt 104.8 0.6 175
    These numbers show that the additional area of the felt was beneficial for the reductant of V02 +. This is to be expected when the reaction rate is limited by the vanadium reduction rather than by the hydrogen oxidation (which occurs on the platinum).
    The IrO 2 on Ti catalyst (and also Pt on Ti) and the catalyst with IrO 2 on Ti in conjunction with the graphite had little effect on the recombination of the hydrogen with the positive electrolyte.
    However, a membrane assembly for a fuel cell was found to be effective in which a catalytic Pt-Ir coating was applied to a membrane. With this membrane in the gas cavity (not in contact with the electrolyte), a current of 3 mA flowed through the cell. After contacting the catalyst with the electrolyte (it floated on the electrolyte, in good contact with both the electrolyte and the hydrogen-containing gas), the current increased to about 27 mA. After removal of the catalyst from the electrolyte, the stream slowly fell back until all of the V (IV) was reoxidized. Figure 3 illustrates a current-time plot for this similar experiment at 83% concentration of hydrogen and partial immersion of a membrane-supported catalyst material between the time marks at 2000 and 13000 seconds.
    The average current Icatalytic exceeding the base current was relatively independent of the hydrogen content in the gas volume, as shown in the following table:
    Average H2 concentration Ikata lytic [mA] 83% 24 28% 21 8% 23
    The area of the membrane-supported catalyst was 5.0 cm 2 and the experiment was carried out at room temperature.
    权利要求:
    Claims (9)
    [1]
    • ♦ *: β- FW-3460 ΑΤ Claims; 1. A system for energy generation or storage on an electrochemical basis, comprising at least one flow cell, each consisting of two of differently charged Elektrolytflüssigkerten (21, 22) through which a membrane separated half-cells, in which half-cells each at least one electrode is arranged, and in each case a tank for each of the electrolyte liquids, characterized in that a common gas volume (23) connecting the tanks is provided, and that in the tank for the positive electrolyte liquid (22) at least one catalyst (24) for the reduction of positive reaction partner of the redox couple in contact with the positive electrolyte liquid (22) and with the common gas volume (23) is arranged.
    [2]
    2. System according to claim 1, characterized in that the catalyst (24) near an inlet (31) and / or outlet for the electrolyte liquid (22) is arranged.
    [3]
    3. System according to claim 1 or 2, characterized in that the catalyst (24) is applied to a on the positive electrolyte liquid (22) floating arrangement, preferably on a clamped on a frame (11) membrane (12).
    [4]
    4. System according to claim 1 or 2, characterized in that the catalyst (24) is applied to a partially immersed in the positive electrolyte fluid (22) tissue.
    [5]
    5. System according to one of claims 1 to 4, characterized in that the catalyst (24) has at least one gas diffusion layer, preferably containing conductive fibers.
    [6]
    6. System according to one of claims 1 to 5, characterized in that catalysts (24) are provided based on platinum and / or iridium dioxide.
    [7]
    7. System according to one of claims 1 to 6, characterized in that means for generating or maintaining a gas flow over the Katalsator (24) are provided. ** · »·« ** · »« * · «« * * · · · * I * 4 «I I · · · · · · ·

    FW-3460 AT
    [8]
    8. System according to any one of claims 1 to 7, characterized in that means are provided for pressure equalization of the common gas volume (23) relative to the environment.
    [9]
    9. System for energy generation or storage on an electrochemical basis, comprising at least one flow cell, each consisting of two of differently charged electrolyte liquids (21, 22), separated by a membrane half-cells, wherein the electrolyte liquid in the positive half-line in the charged state contains four- and pentavalent vanadium, sulfuric acid and optionally further additives, wherein in each half lines at least one electrode is arranged, and in each case a tank for each of the electrolyte liquids (21, 22), characterized in that the system according to one of Claims 1 to 8 is formed.
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    同族专利:
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    JP2015504233A|2015-02-05|
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    AT512184B1|2013-06-15|
    EP2807695A1|2014-12-03|
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    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    JP2003173812A|2001-12-04|2003-06-20|Sumitomo Electric Ind Ltd|Capacity drop detection method of redox flow battery|
    US20100092843A1|2008-10-10|2010-04-15|Deeya Energy Technologies, Inc.|Venturi pumping system in a hydrogen gas circulation of a flow battery|
    EP2339682A1|2009-10-29|2011-06-29|Beijing Prudent Century Technology Co. Ltd.|Redox flow battery and method for continually operating the redox flow battery for a long time|
    US4159366A|1978-06-09|1979-06-26|The United States Of America As Represented By The Administrator Of The National Aeronautics And Space Administration|Electrochemical cell for rebalancing redox flow system|
    CA1202071A|1982-12-01|1986-03-18|Patrick G. Grimes|Method and apparatus for maintaining the ph in zinc-bromine battery systems|
    JPS61211960A|1985-03-15|1986-09-20|Mitsui Eng & Shipbuild Co Ltd|Secondary cell|
    DE3843312A1|1988-12-22|1990-06-28|Siemens Ag|Rebalance cell for a Cr/Fe redox ion storage device|
    JP2528100Y2|1991-04-26|1997-03-05|住友電気工業株式会社|Electrolyte flow battery|
    EP0729648B1|1993-11-17|2003-04-02|Pinnacle VRB|Stabilised electrolyte solutions, methods of preparation thereof and redox cells and batteries containing stabilised electrolyte solutions|
    JP3315508B2|1994-01-07|2002-08-19|住友電気工業株式会社|Electrolyte flow battery with electrolyte readjustment device|
    JP3283825B2|1998-06-25|2002-05-20|住友電気工業株式会社|Redox flow battery and method for manufacturing the same|
    JP3897544B2|2001-06-07|2007-03-28|住友電気工業株式会社|Redox flow battery electrolyte and redox flow battery|
    JP2006147374A|2004-11-19|2006-06-08|Kansai Electric Power Co Inc:The|Method of operating vanadium redox flow battery system|
    US7517608B2|2007-03-09|2009-04-14|Vrb Power Systems Inc.|Inherently safe redox flow battery storage system|
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    US8916281B2|2011-03-29|2014-12-23|Enervault Corporation|Rebalancing electrolytes in redox flow battery systems|
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    法律状态:
    2014-09-15| PC| Change of the owner|Owner name: CELLSTROM GMBH, AT Effective date: 20140723 |
    2016-11-15| PC| Change of the owner|Owner name: GILDEMEISTER ENERGY STORAGE GMBH, AT Effective date: 20161005 |
    2018-09-15| MM01| Lapse because of not paying annual fees|Effective date: 20180123 |
    2018-12-15| PC| Change of the owner|Owner name: ENEROX GMBH, AT Effective date: 20181018 |
    优先权:
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    PCT/EP2012/076324| WO2013110421A1|2012-01-23|2012-12-20|System for generating and/or storing energy on an electrochemical basis|
    EP12808815.0A| EP2807695B1|2012-01-23|2012-12-20|System for generating and/or storing energy on an electrochemical basis|
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    AU2013200868A| AU2013200868B2|2012-01-23|2012-12-20|System for energy generation or storage on an electrochemical basis|
    US13/814,865| US9225031B2|2012-01-23|2012-12-20|System for energy generation or storage on an electrochemical basis|
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