Patent Grant
8785023
This invention generally relates to energy storage technologies, and more particularly to redox flow battery energy storage systems and applications.
Many renewable energy technologies, while economically viable and environmentally beneficial, suffer from the disadvantage of periodic and unpredictable power generation. To enable such renewable energy technologies to expand, large scale energy storage systems are required. Additionally, many conventional electric generation technologies, such as coal and nuclear power plants, as well as promising alternative energy generation technologies, such as fuel cells, function best when operated at constant power, and thus can benefit from energy storage systems that can deliver peak power when needed and store energy during off-peak hours.
Reduction/oxidation (redox) flow batteries of the various embodiments offer one large-capacity energy storage solution. Redox flow batteries are electrochemical energy storage systems which store electrical energy in chemical reactants dissolved in liquids. Thus, the energy storage capacity of a flow battery is theoretically limited only by tank size. An efficient and cost-effective redox flow battery system of the various embodiments would provide a needed addition to electrical grid systems.
A redox flow battery storage system of the various embodiments store electrical energy in electrolyte species. The redox flow battery storage system includes at least one redox flow battery stack assembly including a number of layers with each layer including multiple independent cells in a cascade orientation along the reactant flow path. The cells of the redox flow battery stack assembly may configured to increase electrical storage efficiency with the state-of-charge of reactants expected in each cell. Reactants may be heated to increase battery efficiency, with waste heat from energy sources or uses of energy from the battery or system providing the thermal energy to heat the reactants. By adjusting the size of tanks for storing the reactants and adding redox flow battery stack assemblies, the storage system can be sized to support multi-megawatt implementations suitable for use with power grid applications. Thermal integration with energy generating systems, such as fuel cell, wind and solar systems, further maximizes total energy efficiency. The redox flow battery system of the various embodiments can also be scaled down to smaller applications, such as a gravity feed system suitable for small and remote site applications.
Redox flow battery stack assemblies of the various embodiments comprise a plurality of electrochemical cells arranged in hydraulic series to form a cascade arrangement. In some embodiments, such cascade arrangements comprise cells configured for a portion of a state-of-charge gradient that the cell is expected to experience.
The accompanying drawings, which are incorporated herein and constitute part of this specification, illustrate exemplary embodiments of the invention, and, together with the general description given above and the detailed description given below, serve to explain features of the invention.
The various embodiments will be described in detail with reference to the accompanying drawings. Wherever possible, the same reference numbers will be used throughout the drawings to refer to the same or like parts. References made to particular examples and implementations are for illustrative purposes, and are not intended to limit the scope of the invention or the claims.
As used herein, the terms “about” or “approximately” for any numerical values or ranges indicates a suitable temperature or dimensional tolerance that allows the part or collection of components to function for its intended purpose as described herein.
The term “engineered cascade flow battery” is used herein to refer generally to a cascade flow battery in which cells, stages and/or arrays within the battery are configured in terms of materials, design shapes and sizes, reactant flow, and/or other design variables based on an expected condition of reactants (e.g., the state of charge of electrolytes) so as to increase the battery's performance (e.g., energy storage efficiency, power generation efficiency, reduced electrolyte breakdown, reduced hydrogen generation, or other performance) over that achievable in a cascade flow battery in which all cells, stages and/or arrays along the reactant flow path are substantially the same as one another. References to “optimized” or “optimum” are merely intended to indicate design parameters which may be controlled or varied in an engineered cascade flow battery in order to improve performance and to distinguish the embodiments from designs in which there is no configuration based on expected local properties of reactants. Use of these terms is not intended to imply or require that the any cells, stages and/or arrays or components thereof are designed for the best possible or theoretical performance.
As used herein the phrase “state of charge” and its abbreviation “SOC” refer to the chemical species composition of at least one liquid electrolyte. In particular, state of charge and SOC refer to the proportion of reactants in the electrolyte that have been converted (e.g. oxidized or reduced) to a “charged” state from a “discharged” state. For example, in a redox flow battery based on an Fe/Cr redox couple, the state of charge of the catholyte (positive electrolyte) may be defined as the percent of total Fe which has been oxidized from the Fe2+ state to the Fe3+ state, and the state of charge of the anolyte (negative electrolyte) may be defined as the percent of total Cr which has been reduced from the Cr3+ state to the Cr2+ state. In some embodiments, the state of charge of the two electrolytes may be changed or measured independent of one another. Thus, the terms “state of charge” and “SOC” may refer to the chemical composition of only one or of both electrolytes in an all-liquid redox flow battery system. The skilled artisan will also recognize that the state of charge of one or both electrolytes can be changed by processes other than electrochemical processes (e.g., by adding quantities of one or more reactant species).
The embodiments provide an energy storage system based upon a reduction/oxidation (redox) flow battery system that is suitable for storing and delivering electric energy under a wide variety of conditions. Electric energy stored by the redox flow battery system can be produced from a wide variety of electric generation or conversion methods, including hydroelectric, natural gas, coal, gasoline, diesel or other liquid petroleum fuel, nuclear, wave power, tidal power, solar, thermal energy, wind, etc. The redox flow battery systems of the various embodiments are also capable of delivering stored energy to a wide variety of loads, including a distributed electrical grid, a data center, an irrigation pump, a cellular telephone station, another energy storage system, a vehicle, a vehicle charging system, a building, or any other electrical load.
Flow batteries are electrochemical energy storage systems in which electrochemical reactants are dissolved in liquid electrolytes (sometimes referred to herein collectively as “reactant” or “reactants”), which are pumped through reaction cells (referred to herein as “cells”) where energy is either added to or extracted from the battery. In applications where megawatts of electrical energy must be stored and discharged, a redox flow battery system can be expanded to the required energy storage capacity by increasing tank sizes and expanded to produce the required output power by adding electrochemical cells or cell blocks (i.e., groups of multiple cells which are sometimes referred to herein as “cell arrays”).
A system diagram of an embodiment of a redox flow battery energy storage system is illustrated in
Referring to
The conductive surfaces 22, 24 are coupled to conductors 42, 43 which complete a circuit through either an electrical power source 45 (for charging) or an electrical power load 46 (for discharge), which may be selected in single stack embodiments via an electrical switch 44. The cathode electrolyte (“catholyte) and anode electrolyte (“anolyte”) are stored in electrolyte tanks 26, 28, and are pumped by pumps 30, 32 to provide the input flows 34, 36 to the redox flow battery stack assembly 10, with battery output flows 38, 40 returning to the electrolyte tanks 26, 28. The redox flow battery stack assembly 10 is designed for reduce cost by keeping the complexity and part count of the stack to a minimum. The redox flow battery stack assembly 10 is further designed to minimize shunt current losses and maximizing reactant utilization.
The redox flow battery stack assembly 10 is configured to include an array of independent battery cells, assembly frames as shown in
Some types of flow battery electrolytes operate more efficiently (i.e., retaining and discharging electrical power with lower losses) when the fluids are heated to an optimum temperature. To take advantage of this characteristic, the redox flow battery cell layer assembly 48 may be configured with tubes 60, 62, 64, 66 or channels through which a heating fluid can be circulated. Circulating a heating fluid around and/or within the battery stack assembly can keep the electrolytes at a controlled temperature. By including heating fluid tubes 60, 62, 64, 66 before and after each battery cell, the operating temperature of each cell can be controlled individually so as to enable each cell to operate at a preferred or optimum temperature corresponding to the state of charge of electrolytes within the cell. The heating fluid tubes are optional because in an embodiment the electrolytes may be preheated within the tanks 26, 28, such as via a heat exchanger circulating a heating fluid so that the electrolytes enter the cell layers 48 at a sufficient temperature for charging or discharging operations. As described more fully below, the heating fluid may draw thermal energy from waste heat generated by either the source of the charging power 45 (e.g., from a generator cooling system) or the load 46 (e.g., from an equipment cooling system).
A conceptual build of a single cell of a cell section within the cell layer 48 of a flow battery stack is illustrated in
The anolyte and catholyte reactants are separated by a planar membrane separator 12 which is suspended between the two planar structural members 80, 82 by frame members 84, 86, 88, 90. It should be noted that the frame members 84, 86, 88, 90 maybe in the form of two exterior frames as illustrated in
At the reactant inlet of each battery cell 50, manifold holes 92, 94 may be provided to direct the incoming electrolyte flows into the reaction area of the cell 50. In an embodiment, the manifolds may include flow directing structures to cause proper mixing of the electrolytes as they enter each reaction cell 50. Such flow directing structures may be configured to adjust or control the reactant flow in each cell 50 within the redox flow battery stack assembly 10 based upon the expected state of charge and other fluid properties within each cell.
The planar structural members 80, 82, as well as separator frame members 84, 86, 88, 90 may include passages through which heat exchanger fluid pipes 60, 62 can pass. Positioning optional heat exchanger fluid pipes 60 within the cell input manifolds 92, 94 enables heat from the thermal fluid within the pipes to raise the temperature of the reactant flows before the reactants enter the cell chamber. Similarly, positioning heat exchanger pipes 62 within the cell output manifolds 96, 98 enables the thermal fluid to extract heat from the electrolytes after the reactants leave a final cell 56, thereby conserving thermal energy and enabling the electrolytes to be returned to storage tanks at a cooler temperature. In a preferred embodiment the thermal fluid is heated to a temperature of about 40 to 65° C. for Fe/Cr reactants.
A redox flow battery stack assembly 10 may be formed by stacking layers 48 in series to form a battery stack. In this battery stack assembly the conductive surfaces 22, 24 provide the electrical connectivity between cells in each stack cell layer as described below with reference to
The planar structural members 80, 82 which form the bipolar frame may be electrically conductive throughout their area, or may be made in such a way that only the conductive surfaces 22, 24 immediately adjacent to the electrochemically active portion of the cell 50 are electrically conductive, as illustrated in
To form each cell layer 48 as illustrated in
In the redox flow battery system of the various embodiments the cells can be replaceable and recyclable. Since the materials of construction are primarily plastics (e.g., polypropylene or polyethylene), carbon fiber felts, and carbon fiber electrodes, the cells contain no heavy metals or toxins that could pose an environmental impact. Further, the reactants, such as Fe/Cr, are no more toxic or dangerous than battery acid. Thus, the redox flow battery system of the various embodiments are ideal for providing the energy storage capacity required for renewable energy systems in a distributed fashion close to the population and load centers.
As explained more fully below with reference to
A variety of reactants and catalysts may be used in the redox flow battery system. A preferred embodiment set of electrolyte reactants is based upon the iron and chromium reactions illustrated in
An undesirable non-faradic electron transfer reaction can occur between Fe3+ and Cr2+ if these ions come into proximity to one another. Therefore, to maintain a high level of coulombic efficiency, electrolyte cross-mixing within a Fe/Cr redox flow battery stack should be minimized. One way to minimize electrolyte cross-mixing is to use a highly selective membrane separator 12 such as Nafion®-117 ion-exchange membrane (DuPont, USA). A disadvantage of highly-selective membrane separators is that they have low ionic conductivity which results in lower voltage efficiency within the redox flow battery stack. Additionally, ion-exchange membranes are expensive, with a price in the neighborhood of $500/m2. Since the DC energy storage efficiency of a redox flow battery is the product of coulombic and voltage efficiencies, an optimization tradeoff exists.
A particular embodiment of the Fe/Cr system is what is known as the mixed reactant system where FeCl2 (Fe2+) is added to the anolyte and CrCl3 (Cr3+) is added to the catholyte, as described in U.S. Pat. No. 4,543,302, the entire contents of which are incorporated herein by reference. An advantage of the mixed reactant system is that the discharged anolyte and discharged catholyte are identical. Furthermore, when the total concentration of Fe in the anolyte is the same as the catholyte, and the total concentration of Cr in the catholyte is the same as the anolyte, the concentration gradients across the membrane separators 12 are eliminated. In this way the driving force for cross-mixing between anolyte and catholyte is reduced. When the driving force for cross-mixing is reduced less selective membrane separators may be used, thereby providing lower ionic resistance and lower system costs. Examples of less-selective membrane separators include microporous membrane separators manufactured by Celgard LLC, and membrane separators made by Daramic LLC, both of which cost in the neighborhood of $5 to 10/m2. By optimizing the cell characteristics for the reactant state of charge and completing the charge or discharge in one pass, the embodiments described herein provide suitably high efficiency in a redox flow battery stack comprised of materials that are approximately two orders of magnitude lower cost than in conventional redox flow battery designs.
In both the unmixed and mixed reactant embodiments, the reactants are dissolved in HCl, which is typically about 1-3 M concentration. The electrocatalyst, which may be a combination of Pb, Bi and Au or ZrC, is provided at the negative electrode to improve the rate of reaction of recharging when Cr3+ in the anolyte is reduced to Cr2+, thereby reducing or eliminating hydrogen evolution. Hydrogen evolution is undesirable as it unbalances the anolyte from the catholyte and is a competing reaction to Cr3+ reduction leading to a reduction in coulombic efficiency.
The cell, cell layer and redox flow battery stack designs described herein can be used with other reactant combinations that include reactants dissolved in an electrolyte. One example is a stack containing the vanadium reactants V(II)/V(III) or V2+/V3+ at the negative electrode (anolyte) and V(IV)/V(V) or V4+/V5+ at the positive electrode (catholyte). The anolyte and catholyte reactants in such a system are dissolved in sulfuric acid. This type of battery is often called the all-vanadium battery because both the anolyte and catholyte contain vanadium species. Other combinations of reactants in a flow battery that can utilize the embodiment cell and stack designs include Sn (anolyte)/Fe (catholyte), Mn (anolyte)/Fe (catholyte), V (anolyte)/Ce (catholyte), V (anolyte)/Br2 (catholyte), Fe (anolyte)/Br2 (catholyte), and S (anolyte)/Br2 (catholyte). In each of these example chemistries, the reactants are present as dissolved ionic species in the electrolytes, which permits the use of battery cell and stack designs in which electrolyte flow through a plurality of battery cells series along the flow path (i.e., cascade flow), with the cells and having different physical properties along the flow path (cell size, type of membrane or separator, type and amount of catalyst). A further example of a workable redox flow battery chemistry and system is provided in U.S. Pat. No. 6,475,661, the entire contents of which are incorporated herein by reference.
A number of cell chambers are formed in each bipolar frame in a redox flow battery stack array.
Due to the variation in reactant ion concentrations as the reactants flow through the various cells in each layer, the amounts of catalytic coating may be varied to match the state of charge condition in each of the respective cells. Additionally, the catalytic coating formations applied to the porous electrodes 18, 20 may be varied in formulation (e.g., varying amounts of zirconia or bismuth compounds) to better match the state of charge condition in each cell. For example, typically the cell with the lower reactant concentrations will require a higher catalyst loading on the porous electrodes to achieve optimum performance.
The various embodiments include a unique redox flow battery stack configuration that includes multiple independent cells within a flow path as illustrated in
As illustrated in design trend line 116, other design parameters—illustrated as Group B parameters—may be increased from one end of a cell layer 48 to the other to configure the battery design so that the values increase from reactant inlet to outlet from the cell layer in discharge mode and decrease from reactant inlet to outlet from the cell layer in charging mode. As illustrated in
For example, as described above, the discharge catalyst loading and discharge catalyst activity (both Group B design parameters) may be increased in each cell along the flow path of redox flow battery stack assembly 10 from inlet to outlet in the discharge mode and decreased in each cell along the flow path of redox flow battery stack assembly 10 from inlet to outlet in the charge mode to compensate for decreasing reactant concentrations, as indicated by the design trend line 116.
Similarly, the charge catalyst loading and charge catalyst activity (both Group A design parameters) may be decreased in each cell along the flow path of redox flow battery stack assembly 10 from inlet to outlet in the discharge mode and increased in each cell along the flow path of redox flow battery stack assembly 10 from inlet to outlet in the charge mode to compensate for decreasing reactant concentrations, as indicated by the design trend line 112. The specific catalyst loading and catalysts activity implemented within each cell along the flow path can be determined using the design trend line 116 with respect to discharging, trend line 112 with respect to charging, and the number of cells in the path.
Using the design trend lines 112, 116 illustrated in
Similarly, the various embodiments may control the temperature of reactants as they flow through the redox flow battery stack depending upon whether the stack is charging or discharging.
In a similar manner, the various embodiments improve electrochemical performance by configuring the redox flow battery stack assembly 10 so that the reactant mass transport rate varies from cell to cell along the flow path.
In a similar manner, embodiment redox flow battery cells may be configured with different membrane separator 12 materials along the reactant flow path.
Thus, in an embodiment redox flow battery stack assembly 10 may include cells at one end of the flow path having membrane separators 12 made from a material with high membrane selectivity at the cost of greater ohmic losses, while cells at the other end of the flow path will have membrane separators 12 made from a material with lower ohmic losses. This design approach works because the driving force for cross mixing is greatly diminished due to the low concentrations of spontaneously-reacting active species at the outlet end in the discharge mode and at the inlet end in the charge mode. In the case of an Fe/Cr redox flow battery (
As mentioned above, the particular design configuration of each cell within a particular redox flow battery stack assembly 10 may be determined by applying the design trend lines illustrated in
By varying the design configurations of independent cells along the reactant flow path through the redox flow battery cell layer 48 and stack assembly 10 the various embodiments are able to achieve significant charging/discharging performance improvements over conventional redox flow battery designs. This performance improvement is illustrated in
By forming the conducting regions (e.g., conductive surfaces 22, 24) only on the active areas of the bipolar frame as illustrated in
Instead of assembling cells within a unibody frame for each cell layer, each cell may be assembled within cell frames 52a-56c in an embodiment illustrated in
As mentioned above, one source of losses in a redox flow battery is due to mixing or leakage of reactants along the edges of the membrane separator 12. As illustrated in
As mentioned above, the performance of a redox flow battery stack assembly 10 can be enhanced by heating the reactants to optimum temperatures at various stages within the battery flow path. Various embodiments accomplish such heating by using waste heat or alternative energy heat sources, thereby enhancing electrical performance while reducing parasitic losses. The various embodiments have a number of useful applications in energy generation applications as well as industrial applications which use electrical power and generate waste heat (e.g., heat sinks from air-conditioning and equipment cooling systems). As discussed in the embodiments below, alternative energy sources such as wind turbines and solar panels require cooling to enhance performance and prevent mechanical breakdown. Larger energy storage systems using the Fe/Cr redox flow battery technology can be thermally integrated with wind turbine farms and photovoltaic solar farms as illustrated in
Integrating a wind turbine system with a redox flow battery system provides a renewable power generation system which can operate more efficiently and economically than a wind turbine farm that does not have energy storage capacity. Such a system can store power whenever the wind is blowing, and meet the power demands of the electrical power grid regardless of the current wind conditions. This enables a wind turbine/redox flow battery system to meet utility contractual obligations to provide consistent power to the electrical power grid, thereby avoiding economic penalties for failing to supply contracted power levels during times of little or no wind. Additionally, the system allows electrical power to be supplied to the power grid during periods of peak demand, enabling the system owner to sell electrical power at the most favorable rates regardless of when peak winds occur.
An embodiment energy generation and storage system combining a wind turbine farm 170 with a redox flow battery is illustrated in
Similar to the wind turbine/redox flow battery system described above with reference to
A solar energy conversion system, such as a photovoltaic (PV) array, concentrating photovoltaic (CPV) array, a solar thermal energy power plant, or a solar hot water system, can be thermally and electrically integrated with the redox flow battery system to provide a more economical and efficient renewable energy generation system 180, 190 as illustrated in
Thermally integrating a solar thermal energy collection system with a redox flow battery system can be accomplished in at least two configurations. In a first configuration illustrated in
In a third configuration illustrated in
Thermally integrating a solar collector or solar energy conversion system with a redox flow battery system can use either pump circulation as illustrated in
The thermosiphon solar heating system operates in closed loop configuration for both embodiments illustrated in
The table in
Thermal integration of a redox flow battery system with conventional power generation systems, such as nuclear and coal-fired power plants, can provide significant energy and economic efficiencies since such systems generate a large amount of low grade waste heat. As described above, thermally integrating the redox flow battery system with sources of waste heat improves the battery operating efficiency without the expense or parasitic losses of electrical or fossil fuel heaters. Electrically integrating a redox flow battery energy storage system with conventional power generation systems also provides significant economic advantages since the battery system can enable base-loaded power plants to accommodate grid support (ancillary services) or peak power demands without varying their output. As is well known, nuclear and coal-fired power plants operate most efficiently and economically when run at constant power levels. Peak power demands can be met by charging the redox flow battery energy storage system during periods of reduced demand (e.g., off-peak hours in the late evening) and then augmenting the electrical output of the power plant with electricity drawn from the battery system during periods of peak power demand. Such a combined power plant/energy storage system can be economically advantageous since electrical power can be generated in the most economical manner (i.e., at constant output 24 hours per day) but sold at times of peak demand when electricity prices are greatest. Further economic benefits can be obtained by adding a redox flow battery energy storage system to an established conventional power plant to meet growing demands for peak power without building additional power plants. The sizing flexibility of redox flow battery systems, in which energy storage capacity can be increased simply by increasing the size or number of reactant storage tanks, means the economic advantages of adding a flow battery storage system to a conventional power plant can be obtained without having to invest in a system sized for future demands.
Geothermal energy can also be used to heat the reactant storage tanks. This approach could provide a stable system with a large amount of thermal inertia. Low grade geothermal energy can be used to provide heat to the redox flow battery stack assembly 10 or to the reactant storage tanks. In this embodiment heat is obtained from geothermal energy deep within the Earth which can be conveyed by a thermal fluid around the reactant storage tanks and/or through a heat exchanger before and after the battery stack.
The redox flow battery storage system does not necessarily need to be placed in close proximity to the power generation system. For example, if there is a low cost source of waste heat from an industrial process or a solar array (PV or CPV) used to a building, it may be economically and efficiently advantageous to locate a redox flow battery within or near the building in which the process is accomplished or the solar array located. In this manner, the waste heat from the industrial process or on-site power or thermal energy generation can be used to enhance the battery efficiency, while the energy storage capacity of the battery is used to meet peak power demands or enable purchasing electrical power during off-peak hours when electricity rates are lower. Thus, if the industrial process uses large amounts of electricity, thermally and electrically integrating the process with a redox flow battery system can meet the process's demand for electrical power while electricity is purchased to charge the battery system during off-peak hours when electricity rates are lower. This type of implementation may reduce cooling costs for the industrial process over periods when the electricity rates are high, thus providing further cost savings.
All the previously mentioned low grade heat sources can also be applied to heating the reactant tanks instead of or in addition to heating the redox flow battery stack assembly 10. Heating the reactant tanks enables the system to respond very quickly to load changes without any thermal management problems because the reactant fluid is constantly maintained at the operating temperature ready to be utilized in the flow battery. Costs and complexities of heating and insulating the reactant storage tanks may be offset by the cost advantages of simplifying the redox flow battery stack design because this approach eliminates the need for heat exchanger elements within the battery stack assembly. Further, combining these alternative embodiments, such as heating storage tanks and providing heat exchangers within the stack may provide the optimum design approach for providing clean, low cost and reliable heat to the redox flow battery.
Four additional example system embodiments of the redox flow battery system for use in battery energy storage systems (BESS) are illustrated in
In a first example embodiment illustrated in
Electrical power is generated from the chemical energy stored in the electrolytes in a second (discharging) redox flow battery stack 212. Electrolyte from the storage tanks 214, 216 is directed to the second redox flow battery stack 212 via inlet flows 218, 220. Within the second redox flow battery stack 212, electricity is generated by converting Fe+3 ions to the Fe+2 state and Cr+2 ions to the Cr+3 state (see
Reactants flowing out of the second redox flow battery stack 212 (outflows 222, 224) may be pumped into the first redox flow battery stack 210 for recharging, thereby providing a single charging and discharging loop. Since the electricity provided to the DC load 206 is generated from electrolytes in the second redox flow battery stack 212, the output current is completely isolated from the electrical sources of charging power, enabling the output power to reliably follow the DC load without power spikes or power drops. This arrangement ensures power variations from the grid, on-site renewable energy generators, or on-site distributed generators do not disrupt power to the DC load 206. Conversely, the power fluctuations associated with a large and widely varying load, such as an electric vehicle charging station or industrial batch process (e.g., a mixer), remain isolated from the utility grid 202 and other energy sources. This is beneficial to utilities as it reduces stress on the grid and also is beneficial to charge station owners as it circumvents large power demand charges. The unique characteristics of the redox flow battery system also enables DC□DC conversion to be accomplished with high overall system efficiency by a suitable choice of the number of cells connected in series within each stack to achieve V1 in the charge stack and V2 in the discharge stack. Also, the facility owner can choose when to charge the system so as to select the lowest cost electricity in order to maximize gross profit margins.
As described above, electrical efficiencies of the first and second redox flow battery stacks 210, 212 can be enhanced by heating the reactants to an elevated temperature, such as about 40 to 65° C., using on-site waste heat from equipment or facility cooling systems or geothermal heating systems 236. As described above, a heating fluid from waste heat recovery systems, solar hot water system, or geothermal heating systems 236 may be provided to a heat exchanger within the redox flow battery stacks 210, 212 (as illustrated in flow 238) and/or to heat the reactant storage tanks 214, 216 (as illustrated in flow 240).
The embodiment illustrated in
A particularly attractive application for the Fe/Cr redox flow battery system 200 embodiment illustrated in
As described above with reference to
In a second example embodiment illustrated in
The vehicle charging station 250 embodiment illustrated in
Similar to the embodiment described above with reference to
Similar to the embodiments described above with reference to
In a fourth example embodiment illustrated in
In this embodiment, the chemical fuel, such as hydrogen or natural gas, may be provided from a fuel source 356 via a fuel pipe 354 to the fuel cell 352. For example, the fuel cell/redox flow battery system 350 may be located at or near a source of natural gas, such as in an oil field, so that natural gas extracted from the ground can be provided to the fuel cell. The fuel cell 352 converts the fuel into electricity and effluents (e.g., water and carbon dioxide). Electricity output from the fuel cell 352 is provided to the first redox flow battery stack 210 where the power is used to charge the electrolytes stored in the electrolyte storage tanks 214, 216. As described above, electrical energy stored in the electrolyte species is converted into electricity in the second redox flow battery stack 212. Electricity output 234 from the second redox flow battery stack 212 can be provided to an inverter 358 which converts the DC current generated by the battery into AC current compatible with the utility grid 202 or industrial facility 359. The inverter 358 may be a solid-state electrical DC□AC inverter or a motor-generator as are well-known in the art. In this embodiment, flow of the electrolyte through the second redox battery stack 212 can be controlled by adjusting the speed of the pumps 226, 228 so as to generate electricity to meet the demands of the grid 202. When demand from the utility grid 202 or industrial facility 359 exceeds the steady-state output of the fuel cell 252, stored energy in the electrolyte is used to meet the additional demand. When demand from the utility grid 202 is less than the steady-state output of the fuel cell 252, the excess energy is stored in the electrolyte. Thus, the system 350 can follow the peak demands of the utility grid 202 or industrial facility 359 without having to operate the fuel cell 352 in an inefficient or potentially damaging manner. In a similar but alternative manner, the system 350 can be used as an on-site distributed generator to follow the peak demands of a co-located industrial facility load 359. The base load demand of an industrial facility 359 can be satisfied by the utility grid 202 or an independent stand alone fuel cell system 352.
Similar to the embodiments described above with reference to
In a further embodiment illustrated in
Since the goal of the embodiment illustrated in
Additionally, since the goal of the embodiment illustrated in
Operation of the gravity-driven redox flow battery system 400 is illustrated in
As illustrated in
As illustrated in
The advantage of eliminating pumps from the flow battery system in the embodiment illustrated in
The control valves 418, 420, 422, 424 are the only moving mechanical components apart from the rotation mechanism. The system can be operated flexibly by switching between charge and discharge mode at any time. For example, once the system has discharged through one cycle it may be advantageous to discharge a second time by rotating the system through 180° to flow reactants back into the proper tanks for discharging without applying power to the battery stack 410, and then rotating the system another 180° to restart the discharge process. Doing so will generate more electrical power stored in the reactants, although the power output will be lower than the first discharge cycle. Likewise the system can be charged through a number of cycles in a similar process. Also the system can switch from charge to discharge mode without the need to rotate the tanks if needed, although the efficiency of the system will be reduced.
The simplicity of design and operation of the embodiment described above with reference to FIGS. 14 and 15A-15C, as well as the safety of the Fe/Cr electrolyte reactants, makes the embodiment system ideal for small power storage applications. For example, this embodiment may be ideally suited for use in remote power applications, such as remote towns and villages beyond the reach of a utility grid that use solar photovoltaic arrays and/or wind turbine generators for electricity. Adding a redox flow battery system similar to this embodiment would allow remote towns and villages to be supplied with electrical power at night, for example. Similarly, one or two systems according to this embodiment may be used in remote electric vehicle charging stations using utility grid power or local renewable energy sources to charge the system when no cars need to be charged, and rotating the storage system to provide electrical power for recharging an electric vehicle when required.
It is also possible to size this embodiment system to fit inside standard sized shipping containers. Because these systems are fully sealed and self contained they can be safely operated inside the shipping container, enabling the systems to be packaged for rapid deployment. For transportation purposes the electrolyte may be transported as a salt, e.g., a ferric chloride, which may be stored in the tanks. This can significantly reduce the weight of the system for transportation. Then once the system is in place, water can be added to reach the required concentrations for operation. In this manner, systems such as the embodiment described above with reference to
FIGS. 14 and 15A-15C show the battery stack 410 fully integrated with the tanks 404, 406, 414, 416, and fixed plumbing within the support structure 402. However, in another embodiment the tanks 404, 406, 414, 416 may be separated from the battery stack 410 so that the tanks may be rotated to achieve the desired gravity feed through the battery stack 410 which remains stationary. This alternative embodiment may be more flexible in terms of the ability to easily add more tank/storage capacity. This alternative embodiment will require flexible piping or include fluid couples that accommodate rotation without leaking.
As mentioned above, the various embodiments utilize independent cells with different configurations along the reactant flow path to increase overall electrical performance.
Further representative stack design parameters and performance characteristics for a three-cell configuration are listed in Table 1 below. All values are approximate.
The various system embodiments may employ a variety of electrolyte storage tank configurations as described below. In a simple embodiment, a single tank may be used to store each electrolyte as illustrated in
In a second approach, charged and discharged electrolytes can be stored separately in system embodiments illustrated in
In a further embodiment illustrated in
The tank separator 502, 506 inhibits mixing of the charged electrolyte 504, 514 that is fed to the redox flow battery stack assembly 10 with the discharged electrolyte 506, 516 which flows back into the electrolyte tanks 26, 28. This prevents dilution of the charged electrolytes and keeps the charged electrolyte concentrations at a constant level through out the discharging cycle, thereby maintaining the battery cell potentials constant. If mixing were to occur the electrolyte concentrations in the electrolyte tanks 26, 28 would be reduced over time as more and more discharged electrolyte 506, 516 is returned to the tanks.
While
The tank separator embodiments include two forms of movable tank separator designs; a tank separator with flow passages which can be opened to enable electrolyte to flow through the separator, and a tank separator with no flow passages. Operation of these two embodiment configurations are illustrated below with reference to
In a first embodiment illustrated in
During a charge or discharge cycle, initial (either charged or discharged) electrolyte 504 is drawn from the tank 26 from below the tank separator 502 and passed through the redox flow battery stack assembly 10 while electrolyte exiting the battery 506 is pumped into the tank 26 on top of the tank separator 502. This is illustrated in
Since the tank separator 502 is buoyant, opening the louvers 503 (or other valve structures) enables the tank separator 502 to begin floating towards the top of the tank. This is illustrated in
When the tank separator 502 reaches the top of the electrolyte 506 as illustrated in
Closing or opening the valve structures of the tank separator 502 can be controlled via an external drive which may be coupled magnetically to the valve mechanism, such as louvers 503. In this manner no wires or other connections are required between an outside controller or power supply and the separator. In a redox flow battery system the electrolyte flows through a completely closed system to avoid contact with air. This makes it difficult to perform maintenance on the valve mechanisms inside the electrolyte tank 26 for long periods. Therefore, an external control mechanism using magnetism as a coupling mechanism, for example, may have advantages for controlling the tank separator 502 inside the electrolyte tank 26.
Alternatively, the valve mechanisms or louvers 503 may be controlled by mechanical mechanisms activated by the position of the tank separator 502 within the tank 26. For example, the valve mechanisms, such as louver 503 may be configured to shut when the structure surfaces, such as a buoyant lever that latches the louvers closed when it rises above the fluid surface, and may be configured to open upon a portion of the structure contacting the bottom of the tank, such as a latch release mechanism.
In an alternative embodiment the tank separator 602 may be vertically oriented and configured to traverse the length of a horizontally disposed electrolyte tank 600 as illustrated in
To begin discharging the battery, the direction of the electrolytes flowing through the redox flow battery stack assembly 10 are reversed as shown in
At any time the flow through the redox flow battery stack assembly 10 can be reversed in order to switch from charging to discharging, or discharging to charging. Thus, as illustrated in
In the embodiment illustrated in
The seal between the tank separator 502, 602 and the electrolyte tank 26, 600 does not need to exceptionally leak proof because a small amount of leakage around the edges will have very little impact on the overall system efficiency if the tank volume is sufficiently large. Also some leakage, while undesirable, does not pose any threat to the flow battery system other than slightly reducing its overall efficiency.
Since the tank separator moves due to electrolyte being extracted from the tank when it is in one state-of-charge and reinjected when it is in the opposite state-of-charge, the position of the tank separator can function as a state-of-charge indicator. By incorporating a passive or active signaling device, such as a RFID chip or a large piece of metal, the position of the tank separator and hence the system state-of-charge, can be determined by a position sensitive reader of the signal from the RFID chip or induced magnetic field of the metal piece. Multiple RFID chips or metal pieces can be used to increase signal strength and/or provide redundancy.
The horizontal or vertical tank embodiments described in
As mention above, the electrolytes stored within the tanks 214, 218 in
Other design approaches may be used to keep charged and discharged electrolytes separate. In a first alternative approach, a bladder can be provided inside each tank for each electrolyte. The bladder could be sealed to the tank and be sized appropriately to accommodate the full volume of charged and discharged electrolytes. Discharged electrolyte may be pumped into the bladder portion of the tank, with the bladder preventing the discharged electrolyte from mixing with the charged electrolyte in the remainder of the tank. The use of an in-tank bladder is similar to the movable partition embodiment described above with reference to
In a second alternative approach, a series of tanks is used for each electrolyte that in aggregate have a larger volume than the volume of electrolyte. The tanks for an electrolyte are coupled to the redox flow battery stack assembly such that the discharged and charged electrolytes are distributed among the tanks during each half cycle of the battery system. This “N+1” configuration obviates the need for a movable partition or sealed part with the tradeoff of additional plumbing, valves, and control complexity.
Other alternative designs may leverage the fact that in the discharged state the two electrolytes in the Fe/Cr mixed reactant system have identical chemical compositions. Thus, for a system that is designed to operate over a state-of-charge range that goes to full discharge (i.e., zero state-of-charge), a three tank system may be used where a first tank holds charged anolyte, a second tank holds charged catholyte, and a third, larger tank, holds the combined discharged electrolytes. In a further alternative design, one tank may be sized to hold at minimum the volumes of both the anolyte and catholyte. In a further approach, the one tank may include two partitions inside which move from the middle of the tank to the two ends. In this alternative, charged anolyte is pumped into/out of one end of the tank while charged catholyte is pumped into/out of the other end of the tank, and discharged anolyte and catholytes are pumped into/out of the middle of tank. As discharged electrolyte fills the inner section, its expanding volume pushes the partitions towards each end, compensating for the decreasing volume of the charge electrolytes. In a further alternative, bladders may be used instead of partitions to create the three separate volumes within a single tank.
All tanks in the redox flow battery system embodiments described above (except for those illustrated in
Containerizing the electrolyte tanks described above may enable them to be more easily deployed than tanks that are constructed onsite or require custom foundations that must be built onsite. Also packaging the stacks, redox flow battery control system, and the power conditioning system inside standard shipping containers can create an entire system configuration that is easily shipped by rail and/or tractor trailer and deployed with relatively minimal onsite work. Thus, containerized redox flow battery systems can provide turn-key power energy storage systems that need only be connected to a utility grid or other source of electric power. A system design in which the containers housing the redox flow battery stacks, control system, and power conditioning system are placed above containers housing the electrolyte storage tanks yields an energy storage system that can be readily transported and set-up at the destination, and that facilitates control over electrolyte flows and full or partial draining of the stacks when the battery system is idle for short or extended periods of time.
In a further embodiment, the redox flow battery stack assembly may be configured so that the battery can perform charging and discharging operations with reactants flowing in a single direction. In one configuration, electrolyte tanks 26, 28 that allow mixing of charge and discharge electrolytes, such as shown in
Alternative embodiments of redox flow battery systems will now be described with reference to
As used herein, the term “cell” or “electrochemical cell” carries its ordinary meaning, and refers, without limitation to a discrete arrangement of structural and chemical elements configured to allow an electrochemical reaction to occur. In some embodiments, two or more cells may be combined in a single structure to form a cell block. A cell block can include any number of cells in any configuration. In some embodiments, a cell block will include a common unitary housing, while in other embodiments, a cell block can include a plurality of individual cells, each having its own separate enclosure while being logically combined in a block. A plurality of cell blocks can be combined to form a stack assembly. A stack assembly can include a plurality of cell blocks connected to one another in any electrical and hydraulic configuration to form a battery pack that can be charged and/or discharged as a single unit.
In some embodiments, the backing plates 1066, 1068 are electrically conductive throughout their entire area. For example, such entirely conductive plates can be made of carbon or any other suitable electrically conductive material. In alternative embodiments, the backing plates 1066, 1068 can be configured in a multi-layer or composite material construction in which only the surfaces immediately adjacent to and in physical contact with porous electrodes 1014, 1016 are electrically conductive. In the latter embodiments, the portions of the backing plate 1066, 1068 surrounding the conductive surfaces may be electrically insulating. In further embodiments, the backing plates 1066, 1068 may include a multiple layer construction including an electrically conductive layer made of a substantially electrically conductive material, and an outer structural layer made of a material that is not necessarily electrically conductive but which provides mechanical and structural support. In some embodiments, the size, material, or other properties of the backing plates 1066, 1068 of each cell 1010 may be configured based on a cascade-stage position of the cell and/or the expected state of charge of electrolyte reactants flowing through the cell which may depend upon the position of the cell within the cascade. Such optimizations are discussed in further detail below.
In some embodiments, inlet and outlet ports 1072, 1074 are formed as channels in the backing plates 1066, 1068. In alternative embodiments, inlet and outlet ports 1072, 1074 are formed as channels in the membrane support plates 1060, 1062. In still further embodiments, the inlet and outlet ports 1072, 1074 include separate and independent structures. The inlet and outlet ports 1072, 1074 are typically constructed with small cross sectional areas to minimize shunt currents. In some embodiments, the inlet and/or outlet ports 1072, 1074 may include flow directing structures to cause proper mixing of the electrolytes as they enter and/or exit each electrode space 1014, 1016. In some embodiments, the cross-sectional dimensions, length, tortuosity or other aspects of the inlet 1072 and/or outlet 1074 ports may be configured based on a cascade-stage position of the cell and/or the expected state of charge of electrolyte reactants flowing through the cell. Such optimizations are discussed in further detail below.
In some embodiments, the porous electrodes 1018, 1020 may be made from carbon fiber or graphite felt materials. Such materials are commonly available, and are typically used in thermal insulation, air or other gas filters and other applications. Carbon felt materials generally include an open mesh of carbon fibers. Other porous, electrically conductive materials can also be used as porous electrodes in a flow battery. The porous electrode may be configured with properties, such as overall thickness, fiber size, fiber density, porosity, average pore size, tortuosity, and other properties, based on a cascade-stage position of the cell and/or the expected state of charge of electrolyte reactants flowing through the cell so as to improve or optimize the electrical efficiency of the cell and/or the entire flow battery system. Such optimizations are discussed in further detail below.
In some embodiments, materials may be bonded or plated onto one or both porous electrodes 1018, 1020 in order to modify the rate at which electrochemical reactions occur at that electrode. For example, such materials may include electro-catalysts selected to increase a rate at which reactions occur. Alternatively, such reaction rate modifying materials may be reaction suppressants which are selected to reduce the rate at which select reactions occur. The porous electrode may be configured with catalyst and/or suppressant materials, thicknesses and other catalyst and/or suppressant parameters (such as loading and activity) based on a cascade-stage position of the cell and/or the expected state of charge of electrolyte reactants flowing through the cell so as to improve or optimize the electrical efficiency of the cell and/or the entire flow battery system. Such optimizations are discussed in further detail below.
In some embodiments, the porous electrodes 1018, 1020 may be bonded, welded or otherwise physically and electrically joined to their respective backing plate 1066, 1068. In alternative embodiments, the porous electrodes may be formed integrally with at least a portion of the backing plate 1066, 1068.
The separator membrane 1012 may be made of any material capable of allowing ions to pass through while limiting the migration of other particles from one side to the other. Several separator membrane materials are known in the art. Separator membranes may also be selected or configured to improve cell characteristics based on a cascade-stage position of the cell and/or the expected state of charge of electrolyte reactants flowing through the cell. Such optimizations are discussed in further detail below.
Within some embodiments of a single redox flow battery, individual cells or groups of cells may use different separator materials than other cells in the battery. For example, the membrane separator 1012 may be made from different materials in different cells so as to exhibit varying diffusion selectivity and ionic resistance. These and other properties of membrane separators can be configured based on an expected state of charge within a cascade stage. Optimization of separator materials and material properties based on a cascade-stage position of a cell and/or the expected state of charge of electrolyte reactants flowing through the cell is discussed in more detail below.
One source of losses in a redox flow battery is due to mixing or leakage of reactants along the edges of the membrane separator 1012. Such losses may be eliminated by sealing the membrane separator material edges. Such edge sealing may be accomplished by fusing the material by heating it to an elevated temperature while compressing it, such as with an iron or vise, such as described above with reference to
Electrolytes used in redox flow batteries are typically substantially caustic, i.e., significantly acidic or basic aqueous solutions. Therefore, any flow battery components directly contacting the liquid electrolyte are preferably made of or coated with materials that will not significantly dissolve or degrade in contact with the electrolyte. Additionally, it is desirable to prevent the dissolution of additional metals into the electrolytes, since such additional metals can act as impurities, which can significantly negatively affect flow battery performance.
From left-to-right the common elements of the example cell block 1200 include an outer structural support plate 1206, four electrolyte inlet/outlet ports 1208, a fitting plate 1210, and an electric terminal plate 1212. A first electrochemical cell 1010a includes a first conductive bipolar plate 1214, a first positive half-cell 1201 including a first positive-side gasket 1216, a first positive porous electrode 1218, and a first catholyte flow channel layer 1220. A first separator assembly 1222 includes a separator membrane 112a sandwiched between first 1124a and second 1224b window frames. To the right of the first separator assembly 1222 may be a first negative half-cell 1203 including a first anolyte flow channel layer 1230, a first negative porous electrode 1232 and a first negative-side gasket 1234. A second bipolar plate 1236 may enclose the negative half-cell and be shared with the second cell 1010b which lies to the right of the second bipolar plate 1236. The second and subsequent cells may include all of the same elements as the first cell 1010a, with bipolar plates being shared by adjacent cells. The outer common elements 1204 may also be repeated at the right side of the stack. These include a second terminal plate 1212, a second fitting plate 1210, a second group of inlet/outlet ports 1208 and a second outer structural support plate 1206. All elements of the cell block 1200 may include fluid pass-through holes 1246 through which electrolyte will flow.
This simple layered design allows additional cells to be added with minimal effort. Thus, while the illustrations of
The structural support plates 1206 generally provide structural rigidity to the cell block 1200, and may therefore be made from a substantially rigid material. Since the support plates 1206 are not in direct contact with the caustic electrolytes, they can be made from low-cost, high-strength materials such a steel or aluminum. In alternative embodiments, the support plates can be made of titanium or other more costly metals. In further alternative embodiments, the support plates 1206 can be made of high-strength polymers, such as polycarbonate or some forms of HDPE. The support plates 1206 are preferably of a sufficient thickness and strength that they provide the desired degree of rigidity at the center of the plate to counteract internal pressures, but sufficiently thin to fit within desired physical dimension and weight requirements. In some embodiments, the support plate 1206 may be coated or painted with a non-reactive and non-conductive coating.
The fitting plate 1210 may provide electrical insulation (if needed) and a hydraulic seal between the support plate 1206 and the conductive terminal plate 1212. The fitting plate may also provide a surface against which the fluid inlet and outlet ports 1208 will seal once the cell block 1200 is assembled. As such, the fitting plate 1210 is preferably made of an electrically insulating material that is also impervious to the caustic electrolytes. Thus, in some embodiments, the fitting plate may be made of polypropylene, polyethylene, high density polyethylene, polyvinyl chloride, or another suitable material. The fitting plate is typically between about 0.25 inches and about 1.0 inch thick. In some embodiments, the thickness of the fitting plate 1210 may be selected based on characteristics of a seal with the inlet/outlet ports. In some embodiments, the inlet/outlet ports may solvent welded to the fitting plate 1210.
In some embodiments, the fitting plates 1210 and/or the support plates 1206 may include feet 1240 projecting beyond the outer boundaries of other cell block elements, thereby providing a support stand for the cell block 1200. In alternative embodiments, the illustrated feet 1240 may be replaced by larger and/or differently shaped projections configured for attaching the cell block 1200 to other support structures as needed.
The terminal plate 1212 may include terminal tabs 1242 providing an electrical connection point for electrically joining the cell block 1200 to a charge/discharge circuit, other cell blocks, measurement/monitoring equipment, or any other electric circuit. Electrical connections may be made with simple clamps or alligator clips. Alternatively, more permanent electrical connections may be made by bolting or otherwise joining electrical contacts through holes in the tabs 1242. The terminal plate 1212 may physically contact an outer bipolar plate 1214 to capture and conduct electric current from the cells through the outer bipolar plate 1214. Therefore, the terminal plate 1212 is preferably made of a highly electrically conductive material. In the illustrated embodiment, the terminal plate 1212 is insulated from the caustic electrolytes by the outer bipolar plate 1214. Thus, in the illustrated embodiment, the terminal plate 1212 may be made of copper, aluminum, or other relatively inexpensive, electrically conductive materials. In some embodiments, the terminal plate 1212 may be omitted by providing a conductive surface on the fitting plate 1210.
In some embodiments, a rubber, silicone or other non-reactive, compressible plastic ring gasket 1244 is positioned within electrolyte-pass-through holes 1246 in the terminal plate 1212. The ring gasket 1244 may be sized such that its outer diameter fits within the inner diameter of a pass-through hole 1246 in the terminal plate 1212. A corresponding pass-through hole 1246 in the bipolar plate 1214 may be sized such that its internal diameter is substantially the same as an internal diameter of the ring gasket 1244. Thus, in an assembled state, the ring gasket may be compressed between an inlet/outlet port 1208 and the outer surface of the outer bipolar plate 1214. The ring gasket seals the electrolyte passageway, preventing electrolyte from contacting the terminal plate 1212.
In some embodiments, a washer 1245 may be provided which fits inside the inner diameter of a pass-through hole 1246 in the bipolar plate 1214 and seals against a portion of the ring gasket 1244 to protect an internal edge surface of the bipolar plate from the caustic electrolytes. In some embodiments, the washer 1245, which may be made of any suitable plastic material, may be bonded to or integrally formed with the flow channel layer 1220 and/or 1230. In alternative embodiments, an edge surface of the bipolar plate may be treated and/or sealed to resist electrolyte absorption or degradation.
In some embodiments, the first bipolar plate 1214 may be a solid carbon plate. The purpose of the bipolar plate is to collect electric current from the porous electrode and electrolyte which directly contacts the bipolar plate 1214 in the assembled cell block 1200. Thus, the bipolar plate 1214 may be made of a highly electrically conductive material impervious to the caustic environment of the electrolytes. A bipolar plate thickness is preferably selected by balancing a desired conductivity with the mechanical strength of the plate. A thinner plate is better for electrical conductivity, but some degree of mechanical strength may be needed. In some embodiments bipolar plates may have a thickness of 0.5 mm or less, depending on the mechanical strength needed. Plates with a greater thickness, e.g., up to 1 mm or more, may also be used.
In alternative embodiments, the terminal plate 1212 may be integrally formed with the outer bipolar plate 1214, such as by providing electrical connection points directly on the bipolar plate 1214. Alternatively, electrical connection tabs of copper, aluminum or another suitable metal may be welded, soldered, mechanically joined or otherwise attached to portions of the outer bipolar plate 1214.
In the cell block of
The gasket 1216 may have a thickness sized to be substantially equal to a thickness of the flow channel layer 1220 in an assembled state. In some embodiments, the gasket 1216 may be sized to be slightly thicker than the flow channel layer 1220 such that the thickness of the gasket 1216 can be reduced under the clamping pressure. For example, in one embodiment, a flow channel layer has a thickness of about 0.118 inch and a gasket 1216 has a thickness of about 0.125 inch. The gasket 1216 may be made of any suitable material capable of being compressed and sealing against the bipolar plate 1214 and the separator window frame 1222. For example, the gasket 1216 may be made of rubber, silicone, ethylene propylene diene monomer (EPDM) rubber, or any other suitable material.
The porous electrodes 1218, 1232 are preferably sized to fit exactly within their respective electrode space. In some embodiments, the porous electrodes 1218, 1232 may be sized to be slightly compressed when the cell block is assembled. In alternative embodiments, the porous electrodes 1218, 1232 may be sized to have substantially zero clearance within the electrode space. For example, in one embodiment, the thickness of the electrode space may be equal to the thickness of the flow channel layer 1220. In some embodiments, this electrode space thickness is about 3 mm (0.118 in.) and the thickness of the porous electrode is nominally about 5 mm. In alternative embodiments, the positive and/or negative electrode spaces may be sized and/or configured to include flow channels configured to decrease an internal pressure within the electrode space without substantially reducing reaction efficiency.
The porous electrodes and corresponding electrode spaces may be configured with a variety of combinations of aspect ratio (i.e., length/width), volume and total surface area. Electric power generated by a flow battery reaction cell is proportional to the active area of the electrodes and separator membrane. In some embodiments, the electrodes may be sized with an aspect ratio of about 1:1 (i.e., square), 1:2, 2:1, or any other ratio as desired. The separator membrane will typically have an aspect ratio and dimensions corresponding to the electrodes. In some embodiments, the electrodes and/or separator membranes may have a shape other than rectangular.
The flow channel layer 1220 includes an inlet 1250 in fluid communication with a fluid pass-through hole 1246. Flow channels 1254 join the pass-through holes 1246 of the flow channel layer 1220 with the electrode space 1256 in the interior of the flow channel layer 1220. In some embodiments, inlets and/or outlets in the flow channel layer 1220 may include pressure-reducing deltas shaped like a river delta, in order to facilitate smooth flow of electrolyte into and/or out of the electrode space. In some embodiments, the flow channel 1254 includes a cutout extending entirely through the flow channel layer 1220. In alternative embodiments, the flow channel 1254 includes a trench in only one side of the flow channel layer 1220. In still further embodiments, the flow channel 1254 includes a trench on both sides of the flow channel layer with a strip of material in between.
The flow channel layer 1220 may be made of a plastic material such as polyethylene, polypropylene, polyvinyl chloride or any other material capable of withstanding the caustic environment of the electrolytes.
The separator window 1222 includes a top layer 1224a a membrane separator 1012a, and a bottom layer 1224b. In the illustrated embodiment, the top layer 1224a and the bottom layer 1224b may be substantially identical to one another. In alternative embodiments, the top layer 1224a and bottom layer 1224b may be minor images of one another. In some embodiments, the separator membrane 1012a may be secured between the top 1224a and bottom 1224b window layers by compression alone. In alternative embodiments, the separator membrane 1012a may be secured between the top 1224a and bottom 1224b window layers by an adhesive, a solvent, heat bonding, welding, or any other method or procedure.
As can be seen in
As will be clear to those skilled in the art, the second bipolar plate 1236 collects a negative electric charge on its left surface and a positive electric charge on its right surface (in this example). In this way, all cells in a flow battery cell block 1200 of this design may be joined in electrical series with one another. Any number of additional cells may be added by repeating the positive half-cell 1201, separator window 1222, and negative half-cell 1203 elements described above.
In some embodiments, the layered components of the cell block 1200 may be clamped together with bolts 1260 extending through bolt holes in each element. The size, number and arrangement of bolt holes may be varied as needed for a particular set of design requirements. In the illustrated embodiment, a cell block includes 14 bolt holes around the periphery of the each element. This provides adequate clamping pressure to ensure tight seals at all fluid junctions within the cell block.
For the purpose of the present example, the top-left inlet/outlet port 1208 in the first (i.e., left) structural support plate 1206 will be described as a catholyte inlet port. Continuing with this example, operation of a cell block embodiment illustrated in
As catholyte is pumped into the inlet port 1208, the catholyte may pass through the ring gasket 1244 without contacting the first terminal plate 1212. Catholyte then may pass through the corresponding pass-through holes 1246 in the first bipolar plate 1214 and the first positive flow channel layer 1220. Once sufficient downstream pressure builds up, catholyte will flow through the inlet channel of the flow channel layer 1220 and into the positive electrolyte space occupied by the positive porous electrode 1218. After flowing through the electrode 1218, the catholyte may exit the positive electrode space through the outlet channel in the flow channel layer 1220 and then through the lower-right pass-through hole 1246. The catholyte may then bypass the negative electrode space by passing through the lower-right pass-through holes 1246 in the negative-side gasket 1216 and the second bipolar plate 1214. Catholyte may then enter the positive electrode space of the second cell via the bottom-right pass-through hole.
Under normal operation, the ports exactly opposite the active ports will be closed, such as by valves or caps. For example, if port A is used as the catholyte inlet port, port E will be closed, thereby forcing electrolyte through the cells and out of the cell block through port H. If it is desirable to bypass the entire cell block (using the same example), port E can be opened while optionally closing port H. Electrolyte will thereby be directed through the top-left fluid bypass holes in every cell block element. With port E open, this bypass operation is likely to occur in substantially the same way even without closing port H, since an incompressible electrolyte will tend to follow a path of least resistance to flow. Thus, depending on the desired configuration and mode of operation, any of the eight ports may be an inlet or an outlet for either anolyte or catholyte.
The inlet/outlet ports 1208 may be hydraulically connected to tanks, pumps and/or other cells in any configuration as needed to form a complete flow battery stack assembly. For example, by joining a plurality of cell blocks 1200 in hydraulic series, such that outlet ports of a first cell block are joined to inlet ports of a second cell block (via inter-stage components, in some embodiments), a multi-stage cascade can be assembled. In such a system, each cell block makes up a cascade stage with a plurality of cells. In some embodiments, components of a single block/stage may be configured according to the expected state-of-charge of electrolytes at that point in the cascade as discussed herein.
Embodiments of redox flow battery systems described herein advantageously include cells or cell blocks in engineered cascade arrangements as shown, for example, in
For example, the system of
In an engineered cascade arrangement, the configurations of the cells at each stage may be configured for the expected state-of-charge condition of the electrolytes at that stage or in those cells. Therefore, physical and chemical characteristics of the cell or cells in the first stage 1052 may be configured so as to provide conditions for an efficient electrochemical reaction with the expected state of charge of the electrolytes ranging from the first state (e.g., about 90% SOC) to the second state (e.g., about 70% SOC), and the cell or cells of the second stage 1054 may be configured so as to provide conditions for an efficient electrochemical reaction from the second state (e.g., about 70% SOC) to the third state (e.g., about 50% SOC), and so on.
The number of cascade stages and the number of cells per stage are additional design variables which may be any desired value. Cascade redox flow batteries according to the embodiments herein may include any number of cascade stages, and any number of electrochemical cells in each stage. In some embodiments, engineered cascade redox flow batteries will have between two and ten stages, with each stage having one to about 20 cells.
In the embodiment of
This engineered cascade flow battery arrangement provides several advantages, including limiting shunt currents and improving overall reactant utilization. The engineered cascade flow battery also improves reactant utilization compared to that of a non-cascade redox flow battery. Improving reactant utilization helps to improve the roundtrip DC efficiency of the redox flow battery and reduces or eliminates the need to re-circulate electrolytes multiple times through a stack assembly. Recirculation may be disadvantageous because it may involve more pumping power per kW of stored energy capacity, which increases parasitic losses. Engineered cascade redox flow battery systems also have greater overall electrical storage performance than is possible with a cascade arrangement in which cells at all stages are not configured based on the expected state-of-charge gradient.
Several physical, structural, chemical and other characteristics and properties of the components in the electrochemical cells may be varied when configuring cells based on the cell's position in the cascade or the expected condition (e.g., SOC) of reactants in the cell, which may depend upon the cell's position in the cascade as well as expected or design operating conditions of the cascade flow battery system. For example, any of the following properties may be varied in configuring cells based on their position in the cascade or expected reactant conditions: catalyst loadings; reaction suppressant loadings; catalyst materials; reaction suppressant materials; catalyst activities; reaction suppressant activities; electrode thicknesses; electrode material types; electrode tortuosities; chamber volumes; flow channel dimensions; flow channel shapes; membrane separator porosities; average pore size of membrane separators; separator thicknesses; separator tortuosities; and separator selectivities. These and other parameters may be adjusted to accommodate the variations in reactant concentration (and state-of-charge) expected in each cell according to its position in the flow path of a cascade flow battery. These parameters may be varied individually or collectively (i.e., two or more of the parameters may be adjusted to the match the cell's expected reactant conditions). Other factors that may be considered in selecting and optimizing cell parameters include optimizing coulombic and voltage efficiencies for operation over a range of current densities.
Blocks of electrochemical cells may be arranged in cascades in any suitable physical, hydraulic and/or electrical arrangement meeting a desired set of design parameters.
In engineered cascade embodiments, the design parameters of each one of the first cells 52a, 52b, 52c may be configured according to the expected state-of-charge of the electrolytes in those cells, and thus may be different from the design parameters of each second cell 54a, 54b, 54c and each third cell 54a, 54b, 54c within the cell layers 48a, 48b, 48c.
As illustrated in design trend line 1116, for other design parameters—illustrated as Group B parameters—the performance of cells may be improved in a discharge mode by quantitatively increasing the parameter from a lower value in the first stage (i.e., closest to the stack assembly inlet) to a higher value at the nth stage (i.e., closest to the stack assembly outlet). For the same Group B parameters the performance of cells may be improved in a charge mode by quantitatively decreasing the parameter from a higher value in the first stage (i.e., closest to the stack assembly inlet) to a lower value at the nth stage (i.e., closest to the stack assembly outlet). In some embodiments, stages between the first and nth stage will have properties generally between the properties of the first stage and properties of the nth stage. Such intermediate stages will generally have Group B properties falling along the trend line 1116.
In some flow battery systems, the reaction rate of the anolyte charge reaction may be more limited than other reactions. In such embodiments, it may be advantageous to configure each cell design parameters based on the design curve 1112 shown in
In some embodiments of an engineered cascade flow battery stack assembly, cells may be configured with design parameters selected for the average electrolyte concentration (i.e., state-of-charge condition) expected within each cascade stage, which may provide a stair step approximation of the design trend lines illustrated in
The Group B design parameters that may be varied to configure battery cell designs according to design trend line 1116 include: ionic conductivity; separator average pore size configuring cells for separator diffusion rate configuring cells for electrode surface area configuring cells for discharge catalyst/suppressant loading; discharge catalyst/suppressant activity; temperature (when optimizing discharging); chamber volume (when optimizing discharging); and mass transport rate (when optimizing discharging).
In some embodiments, only one or two parameters may be adjusted in configuring cells for each cascade stage position. In alternative embodiments, as many as all of the parameters described herein may be adjusted in configuring cells for each cascade stage position. In some embodiments, configuration design choices may be made on a cost-savings basis, by selecting higher-cost elements for stages with particularly high and/or low state-of-charge conditions, while using less-costly elements for stages with state-of-charge conditions closer to 50%. Thus, cells may be configured based on their location in the cascade or expected reactant state to achieve performance that is less than some possible or theoretical optimum in order to meet a variety of design, cost and performance objectives.
Embodiments of further representative engineered cascade stack assembly design parameters and performance characteristics for a three-stage engineered cascade configuration are listed in Table 2 below. Ranges of the state-of-charge of reactants at each stage are provided for reference, although alternative embodiments may utilize different state-of-charge ranges.
Materials used for porous electrodes in a redox flow battery system typically include porous carbon felt materials. Carbon felts are generally available for use in a variety of applications, including thermal insulation. Carbon felts made for insulation are available at relatively low costs, but are not necessarily sufficiently uniform in their porosity or average pore size. Carbon felts with controlled designed characteristics may be obtained by custom manufacturing processes, but such custom materials will typically be more costly. For example, it may be desirable to use a carbon felt with a relatively high porosity (i.e., a larger ratio of open volume to solid volume) in order to increase a volumetric flow rate of electrolyte through the felt. It may be more desirable to control reactions at relatively high and low states-of-charge than at state-of-charge conditions closer to 50%. Therefore, in some embodiments, higher cost, optimally designed carbon felts may be used in cascade stages with high and/or low state-of-charge conditions, while using less costly felts in stages with expected state-of-charge conditions closer to 50%.
Chamber volume refers to the interior volume of the cell housing, including the space occupied by the combination of any bonding layer between the bipolar plate and negative electrode, the negative electrode, the membrane separator, the positive electrode, and any bonding layer between the positive electrode and the bipolar plate. In some embodiments, configuring the volume of the cell chamber based on position or expected reactant state may entail increasing the volume of the positive or negative electrode side to offset the volume occupied by any gases formed during operation. In an Fe/Cr flow battery system, hydrogen is typically generated at the negative electrode during a discharge reaction, particularly at high state-of-charge. Thus, in some embodiments, a cascade flow battery system utilizing an Fe/Cr chemistry can be configured with a larger negative electrode chamber volume in cells within stages with higher expected state-of-charge conditions relative to other stages in the cascade.
In some embodiments, electrochemical cells may be configured for their cascade-stage position (or expected reactant state) by varying factors affecting the reactant mass transport rate through the cell. The reactant mass transport rate is defined as the mass flow rate of electrochemical reactants passing through and contacting a porous electrode within a cell. The effective reactant mass transport rate through a cell can be varied by increasing or decreasing the physical volume of the cell chamber. For example, decreasing the cell volume will effectively increase the volumetric flow rate of electrolyte within the cell, which will tend to induce more turbulent flow through the porous electrode. Increased turbulence will tend to increase the rate that reactants come into contact with electrode surface, thereby increasing the mass transport rate.
Alternatively, the mass transport rate of a cascade stack assembly can be varied by providing stages with cells having a more restricted flow area closer to one end of the flow path and a more open and less constricted flow area at the other end. In such embodiments, the reactant mass transport rate increases in each stage along the reactant flow path when operated in the charge mode, and decreases in each stage along the reactant flow path when operated in the discharging mode. In some embodiments, the dimensions of a single cell may be varied along its length, such that a cell inlet has a smaller volume than a cell outlet (for example). In alternative embodiments, cells at a first end of a flow path may have uniform, but smaller volume than cells at a second end of a flow path.
The mass transport rate of a cell can also be varied by selecting porous electrodes with materials, shapes or other properties that increase or decrease turbulence within the cells. For example, porous electrode materials with increased tortuosity will tend to exhibit increased electrolyte turbulence and increased mass transport. Overall electrode surface area may also be varied, such as by varying a diameter of graphite fibers making up a porous electrode felt. Increasing electrode surface area will tend to increase mass transport rates.
Thus, in some embodiments where it is desirable to configure a cascade flow battery stack assembly to improve its charge reaction, the cells may be configured so that the reactant mass transport rate decreases in each cell along the flow path from inlet to outlet in the discharge mode, but increases in each cell along the flow path from the inlet to the outlet while in the charging mode. Alternatively, in embodiments for which it is desirable to configure a cascade flow battery stack assembly for a discharge reaction, the cells may be configured such that the reactant mass transport rate increases in each cell along the flow path from inlet to outlet in the discharge mode, and decreases in each cell along the flow path from the inlet to the outlet while in the charging mode.
Electrode residence time is related to the volumetric flow rate of electrolytes through a flow battery cell. An increased volumetric flow rate will result in a decreased electrode residence time, and vice versa. In some embodiments, it may be desirable to express electrode residence time as an optimization parameter for configuring cells. A higher electrode residence time is generally preferred for higher expected reactant concentrations (i.e., higher SOC), in order to allow more time for electrolytes to react within the cell. A lower electrode residence time is preferred for lower reactant concentrations in order to reduce the possibility for parasitic reactions.
Catalysts may be plated, bonded, adhered or otherwise attached to a surface of an electrode in order to increase a rate at which a desired electrochemical reaction occurs. Similarly, reaction suppressants may be applied to an electrode to selectively suppress or reduce the rate at which certain undesirable reactions occur within a cell. The degree of loading and activity of such catalysts or reaction suppressants may be configured based on an expected state-of-charge condition of reactants in a cell and/or the location of the cell within a cascade stage.
In some embodiments, the discharge catalyst loading and discharge catalyst activity (both Group B design parameters) may be configured based on a cell's position in a cascade expected state-of-charge condition of reactants in the cell. Catalyst loading is defined as the quantity of a catalyst that is plated, bonded, coated or otherwise provided on an electrode surface.
Catalyst activity is a measure of the degree of catalysis, or chemical reaction encouragement of a particular catalyst. Catalyst activity can be expressed as the ratio of the rate at which a chemical reaction occurs with the catalyst to the rate at which the same reaction occurs without the catalyst. Similarly, reaction suppressant activity refers to the degree to which a material discourages a particular chemical reaction, and can be expressed in the same terms as catalyst activity. For a given catalyst or suppressant material and a given chemical reaction, catalyst or suppressant activity can be modified by varying factors affecting the rate at which the catalyst or suppressant material come into contact with active species within an electrolyte. Such factors may include surface treatments, crystal size or structure, particle size, etc.
Thus, as used herein discharge catalyst (or suppressant) activity refers to the reaction modifying strength of catalysts (or suppressants) which encourage a discharge reaction (or discourage side-reactions during discharging) within electrochemical cells of a redox flow battery. Similarly, discharge catalyst loading refers to the quantity of a catalyst (or suppressant) covering a surface of the electrode, where the catalyst (or suppressant) encourages a discharge reaction (or discourages side-reactions during discharging) within electrochemical cells of a redox flow battery.
In some embodiments, the discharge catalyst (or suppressant) loading and discharge catalyst (or suppressant) activity may be increased in each cell along the flow path of redox flow battery stack assembly from inlet to outlet in the discharge mode and decreased in each cell along the flow path of redox flow battery stack assembly from inlet to outlet in the charge mode to compensate for decreasing reactant concentrations, as indicated by the design trend line 1116.
Similarly, in some embodiments the charge catalyst (or suppressant) loading and charge catalyst (or suppressant) activity (both Group A design parameters) may be configured based on a cell's position in a cascade. Thus, as used herein charge catalyst (or suppressant) activity refers to the reaction modifying strength of catalysts (or suppressants) which encourage a charging reaction (or discourage side-reactions during charging) within electrochemical cells of a redox flow battery. Similarly, charge catalyst loading refers to the quantity of a catalyst (or suppressant) covering a surface of the electrode, where the catalyst (or suppressant) encourages a charge reaction (or discourages side-reactions during charging) within electrochemical cells of a redox flow battery.
Thus, in some embodiments, the charge catalyst (or suppressant) loading and charge catalyst (or suppressant) activity may be decreased in each cell along the flow path of a redox flow battery stack assembly from inlet to outlet in the discharge mode and increased in each cell along the flow path of redox flow battery stack assembly from inlet to outlet in the charge mode to compensate for decreasing reactant concentrations, as indicated by the design trend line 1112. The specific catalyst (or suppressant) loading and activity implemented within each stage in the cascade can be determined using the number of stages in the cascade, the design trend line 1116 with respect to discharging, and trend line 1112 with respect to charging.
Electrical efficiency of the redox flow battery system may be enhanced by heating the reactants to an elevated temperature, such as about 40° to 65° C., using on-site waste heat from equipment or facility cooling systems, geothermal heating systems, solar hot water systems, electrical resistance heaters or any other suitable heat source. In some embodiments, a heating fluid may be heated by such a heat source and pumped through a heat exchanger to heat the electrolytes. Alternatively, heaters or heat exchangers may be incorporated directly into stack assemblies, tank enclosures and/or inter-stage components.
In some embodiments, the temperature of electrolytes may be controlled as the electrolytes flow through the cascade redox flow battery stack assembly.
The design curve to employ for a given redox flow battery stack assembly may be based on whether a greater improvement in battery efficiency is achieved by configuring the design to improve performance of the discharge reactions or the charge reactions. For example, in an Fe/Cr system, the anolyte charge reaction has the most limited reaction rates, so design trend line 1112 would be selected for the temperature profile design parameter. Thus, for a cascade flow battery stack assembly configured for a charge reaction according to trend line 1112, electrolytes will be heated to a higher temperature for reaction in stages closer to the inlet, and allowed to cool (or actively cooled) for reactions in stages closer to the outlet during a discharge mode. For the same system in a charging mode, electrolytes may be progressively heated along the cascade such that reactants are at a lower temperature in stages closest to an inlet and electrolyte temperatures are higher in stages closer to the outlet.
In a similar manner, embodiment redox flow battery cells may be configured with different membrane separator materials along the cascade flow path. Design curve 1112 shown in
Membrane selectivity is defined as the inverse of the reactant transport rate through the separator, and in some embodiments can be expressed in units of μg Fe/hr-cm/M or cm2/second. In other words, a separator has a “higher” selectivity when it allows a smaller quantity of reactant ions to pass through the membrane. A separator membrane's selectivity typically correlates positively with the membrane's area specific resistance (e.g., measured in ohm-cm2), and correlates negatively (inversely) with diffusion rate and ionic conductivity.
A number of physical characteristics of a separator membrane material are also strongly correlated with selectivity. For example, both a smaller average pore size and a higher pore tortuosity correlate with higher separator selectivities.
In the discharge mode, cells near the inlet to the cascade redox flow battery stack assembly will experience electrolyte with a high state-of-charge and a high concentration of reactants (e.g., Cr 2+ and Fe 3+). Consequently, transport of the reactants through the membrane separator will result in mixing of reactants with concomitant greater losses of stored energy than is the case in stages near the cascade outlet where the reactant concentrations are diminished. Therefore, flow batteries with engineered cascade stack assemblies achieve greater electrical charge/discharge efficiency by selecting separator membranes that limit the migration of reactants through the membrane separator to a greater degree in stages at which higher reactant concentrations are expected (e.g., near the battery inlet during a discharging operation). On the other hand, membrane separator materials that have high membrane selectivity typically also exhibit high ohmic losses (i.e., electrical resistance, which is the inverse of ionic conductivity through the membrane) that increases energy losses through the battery. Thus, it is generally desirable to use a separator membrane that has a selectivity which is high enough, but no higher than needed for a particular set of reactant concentrations. These countervailing properties result in the design curve 1112 shown in
The selectivity and electrical resistance of separator membranes may be partially affected and/or described by other physical properties of separator membrane materials, such as membrane average pore size and membrane tortuosity. A membrane's average pore size is a measure of the average size (e.g., in microns) of passageways through the membrane. The average pore size of a membrane tends to be inversely correlated with the membrane's selectivity and electrical resistance. Membrane tortuosity is a measure of the complexity of flow paths through the membrane. A high degree of tortuosity represents a complex flow path with many twists and turns, and tends to be correlated with a higher degree of membrane selectivity.
Another variable affecting membrane selectivity is the membrane's thickness. A thicker membrane layer will also have a higher selectivity, and will result in lower cross-mixing of reactants. In some embodiments, two layers of a separator material may be stacked together to effectively double the selectivity of a single layer. Similarly, a single-layer separator material may be selected based in part on its thickness in order to achieve a desired selectivity.
Thus, in one embodiment, a redox flow battery stack assembly may include cells at one end of the flow path having membrane separators made from a material with high membrane selectivity at the cost of greater ohmic losses, while cells at the other end of the flow path may have membrane separators made from a material with lower selectivities and thereby lower ohmic losses. This design approach may be beneficial partly because the driving force for cross mixing is greatly diminished due to the low concentrations of spontaneously-reacting active species at the outlet end in the discharge mode and at the inlet end in the charge mode. In the case of an Fe/Cr redox flow battery (
In configuring cells based on position or expected reactant state by varying parameters discussed above, the cascade redox flow battery stack assembly may be configured so that reactants flow in one direction for charging and in the other direction for discharging. Additionally, any of the above configuration approaches may be applied to flow battery system designs including two or more separate redox flow battery stack assemblies where at least one stack assembly is configured for charging and at least one other stack assembly is configured for discharging.
A multi-stage cascade redox flow battery may be configured for charging, discharging, or both. In some embodiments, flow battery stack assemblies may be arranged in a bi-directional flow arrangement. In a bi-directional assembly, the electrolytes are directed through the redox flow battery stack assembly in one direction in the charging mode and in the opposite direction in the discharging mode. In such embodiments, one end of the flow battery flow path (or cascade series) will always be the low state-of-charge end, and the opposite end will always be the high state-of-charge end.
In other embodiments, a first stack assembly may be provided for charging and a second, separate stack assembly may be provided for discharging. In such embodiments, electrolytes only flow in one direction through a stack assembly.
In further embodiments, electrolyte reactants may be directed through a single stack assembly in a single direction for both charging and discharging. A single-direction flow battery system allows for relatively fast (e.g., millisecond range) switching between charging and discharging modes simply by electrically disconnecting the redox flow battery from the charging power source and connecting it to the load, or vice versa, such as with an electrical switch. In some embodiments, the charging power source may include the electrical grid.
In such single-direction embodiments (in either single-stack or multi-stack systems), the state-of-charge gradient across the cascade stages will reverse direction when the battery is switched from a charging to a discharging mode. During a charging operation, electrolytes entering an inlet to a single-direction stack assembly will be at a relatively low state-of-charge condition, such that the electrolytes can be converted to a higher state-of-charge condition as they pass through the flow battery stack assembly and charged. When the electrolytes exit the stack assembly during a charge operation, they will be at a higher state-of-charge condition. During a discharge operation, the opposite is true: electrolytes will be at a relatively high state-of-charge condition at the inlet to the single-direction stack assembly and at a relatively low state-of-charge condition at the outlet.
In the case of both single-directional and bi-directional flow stack assemblies, the cells of the cascade stages may be configured as a compromise between charging and discharging. For example, the stage or stages toward the center of the cascade series may be configured for a relatively higher state-of-charge condition than the stages on the outer ends of the cascade series as shown for example in
In some embodiments, as illustrated for example in
Similarly,
Hydraulically, electrolyte flows in series from one cascade stage to the next. Between stages, flow batteries may be constructed to include a nearly infinite variety of flow paths, sensors, devices, etc. For example, in some embodiments, electrolyte exiting a first cell in a first stage can flow directly into a first cell of a second stage without mixing with electrolyte from any other source. Such embodiments are referred to herein as “direct cascade” systems. In other embodiments, electrolyte exiting a first cell of a first stage can be mixed with electrolyte exiting a second cell of the first stage or electrolyte from other sources before being directed into one or more cells of a second stage.
While the above description refers to a cascade flow battery stack assembly in a linear orientation, the skilled artisan will recognize that such a system may be arranged in any physical orientation while maintaining a plurality of stages in hydraulic series.
In the embodiment illustrated in
In the illustrated embodiment, shunt breakers 1358 advantageously isolate pairs of direct cascades (which may include more than three stages as needed), thereby limiting shunt currents through the stack assembly 1350. For example, in the illustrated embodiment, electrolyte may be simultaneously directed through two three-stage cascades before being directed to the outflow channel. Placing shunt breakers in both the in-flow and out-flow channels will reduce shunt currents. In alternative embodiments, each single direct cascade section may be isolated by shunt breakers. In further alternative embodiments, direct cascades may be combined into groups of three or more and isolated from other sections of the stack assembly by shunt breakers.
In some embodiments, common inlet and outlet flow channels may be sized to minimize shunt currents while allowing consistent flow rates through the direct cascade sections. The flow channels directing electrolyte through the cells of the direct cascade sections may also be configured to limit shunt currents within a direct-cascade section or blocks of direct cascades.
In some embodiments, each stage of the cascade stack may be configured according to its position along the flow path by optimizing cell characteristics for the state-of-charge of the electrolyte(s) at each stage, as discussed herein.
In some embodiments, the shunt breakers may be configured to substantially reduce or eliminate shunt currents by creating a high electrical resistance in the electrolyte flow path. Various embodiments of suitable shunt breakers are discussed below, but generally any structure capable of substantially reducing or eliminating shunt currents in an electrolyte fluid may be used as a shunt breaker. Shunt currents are a form of short-circuit caused by electrical currents flowing through the liquid electrolyte resulting in a consumption of available discharge energy or delivered charge energy. It is desirable to limit shunt currents to minimize the negative impacts on system efficiency.
In the Z-flow arrangement illustrated schematically in
The name “Z-Flow” is derived from the illustrated schematic and is merely used for convenience to differentiate the arrangement. The name is not intended to limit the scope of the arrangement to any particular physical shape or configuration of elements. The skilled artisan will recognize that the actual spatial orientation of the cells in a Z-flow stack assembly may be arranged in any number of other ways as needed for a particular enclosure, application or other design requirements. For example, in some embodiments, the cells will be positioned in a vertical orientation with inlets at a bottom end and outlets at a top end. Such a vertical orientation has the additional advantage of allowing gas bubbles to be released near the outlet of each cell or each stage. As will also be clear to those skilled in the art, it is not necessary for adjacent stages in a Z-flow arrangement to have alternating inlets and outlets. For example, the arrangement illustrated in
The flow battery stack assembly illustrated in
In a direct cascade system, such as that shown in
In some embodiments, inter-stage components 1152 include one or more functional components such as shunt breakers, re-directing flow channels (e.g., to direct flow from the top of one cell block to the bottom of the next), state-of-charge sensors, electrical current sensors, electrical resistance sensors, volt meters, density sensors, spectroscopic sensors, OCV sensors, reactant balance sensors, de-gassing valves, heat exchangers, heaters, sight glasses, cooling devices, flow meters, pressure sensors, pressure relief valves, pressure mediators, pumping devices, etc.
Shunt breakers may include any components capable of substantially reducing or eliminating shunt currents in a fluid electrolyte. In some embodiments, a shunt breaker includes a long flow channel with sufficient length to create a large electrical resistance between stacks connected by the flow channel. For example, in some embodiments, shunt breakers with flow channels of more than 35 cm have been found to be suitable. Shunt breakers with flow channels of 150 cm have been found to reduce shunt currents by as much as 50% relative to arrangements with no shunt breakers in the same 3-stage, 10-cell Z-flow arrangement. In other embodiments, a shunt breaker may include a very narrow or small-diameter flow channel in addition to or in combination with a long flow channel to achieve the same objective.
Other shunt current structures suitable for mitigating or breaking shunt currents may also be used, such as structures which create a physical and/or electrical discontinuity or otherwise create a substantially high electrical resistance between an upstream and a downstream section of a flow path. One example of a structure for creating a physical discontinuity in an electrolyte flow path is described in U.S. Pat. No. 6,475,661, which describes a drip column for creating a discontinuity in a flowing electrolyte.
In some embodiments, a peristaltic pump, which advances fluid by compressing a section of flexible tubing, can be used as both a shunt breaker and as a metering pump between stages of a cascade flow battery system. In such embodiments, the electrolyte is isolated in pockets formed between pinched-together sections of the tubing, with the tubing material (typically plastic or rubber compound) providing a high resistance path between isolated pockets of electrolyte. Two examples of peristaltic pumps are illustrated and described in U.S. Pat. Nos. 4,522,571 and 4,702,679, the entire contents of both of which are hereby incorporated by reference. Many other peristaltic pumps are also known to those skilled in the art.
A variety of reactants and catalysts may be used in the redox flow battery system. One embodiment set of electrolyte reactants is based upon the iron and chromium reactions that is illustrated in
An undesirable non-faradic electron transfer reaction can occur between Fe 3+ and Cr 2+ if these ions come into proximity to one another. The non-faradic electron transfer reaction reduces the system's coulombic efficiency within a given charge-discharge cycle. Therefore, to maintain a high level of coulombic efficiency, electrolyte cross-mixing within a charged Fe/Cr redox flow battery stack assembly should be minimized. One way to minimize electrolyte cross-mixing is to use a highly selective membrane separator 12, such as Nafion®-117 ion-exchange membrane (DuPont, USA), that eliminates or severely limits transport of Fe 3+ and Cr 2+ through its cross-section. A disadvantage of highly-selective membrane separators is that they have low ionic conductivity which results in lower voltage efficiency within the redox flow battery stack assembly. Additionally, ion-exchange membranes are expensive, with a price in the neighborhood of $500/m2. Additionally, long-term stability and increased crossover of “other ions” (e.g., Fe 3+ and Cr 2+) can occur at elevated operating temperatures (e.g., 35° C. and higher). Since the DC energy storage efficiency of a redox flow battery is the product of coulombic and voltage efficiencies, an optimization tradeoff exists.
An embodiment of a flow battery system using the Fe/Cr system is known as a mixed reactant system where FeCl 2 (Fe 2+) is added to the anolyte and CrCl 3 (Cr 3+) is added to the catholyte, as described in U.S. Pat. No. 4,543,302, the entire contents of which are incorporated herein by reference. An advantage of the mixed reactant system is that the discharged anolyte and discharged catholyte are identical. Further, when the total concentration of Fe in the anolyte is the same as the catholyte, and the total concentration of Cr in the catholyte is the same as the anolyte, the concentration gradients across the membrane separators 12 may be eliminated. In this way the driving force for cross-mixing between anolyte and catholyte may be reduced. When the driving force for cross-mixing is reduced, less selective membrane separators may be used, thereby providing lower ionic resistance and lower system costs. Examples of less-selective membrane separators include microporous membrane separators manufactured by Celgard LLC, and membrane separators made by Daramic LLC, both of which cost in the neighborhood of $5/m2 to $10/m2. By optimizing the cell characteristics for the reactant state of charge at each cascade stage and completing the charge or discharge in one pass, the embodiments described herein provide suitably high efficiency in a redox flow battery stack assembly including materials that are approximately two orders of magnitude lower in cost than in conventional redox flow battery designs.
The benefits of the iron/chromium mixed reactant embodiment discussed above can also be enjoyed by applying the engineered cascade system embodiments to any other flow battery chemistry in which the chemical compositions of both electrolytes at one end of the state of charge range (e.g., discharged or charged) is exactly the same. For example, with other known flow battery chemistries it is possible to mix electrolytes in such a way that the discharged electrolytes are chemically identical, thus substantially reducing inefficiencies caused by migration of small amounts of electrolyte across the separator membrane, and allowing for the use of less-selective, lower cost separator membrane materials.
Other known flow battery chemistries include V(II)/V(III) (anolyte) and V(IV)/V(V) (catholyte), Sn (anolyte)/Fe (catholyte), Mn (anolyte)/Fe (catholyte), Ti (anolyte)/Fe (catholyte), V (anolyte)/Ce (catholyte), V (anolyte)/Br 2 (catholyte), Fe (anolyte)/Br 2 (catholyte), Cr (anolyte)/Br 2 (catholyte), and S (anolyte)/Br 2 (catholyte). An example of an alternate common discharged electrolyte system is a charged anolyte including Sn 2+ and Fe 2+ and charged catholyte including Fe 3+ and Sn 4+, in which the composition of both discharged electrolytes is Sn 4+ and Fe 2+. A second example of an alternate common discharged electrolyte system is a charged anolyte including Ti 2+ and Fe 2+ and charged catholyte including Fe 3+ and Ti 3+, in which the composition of both discharged electrolytes is Ti 3+ and Fe 2+. Another example of a common discharged electrolyte system includes a charged anolyte including V 3+ and Fe 2+, in which the composition of both discharged electrolytes is V 3+ and Fe 2+. Other common discharged electrolyte systems are also possible.
Another example of an alternate discharged electrolyte is a redox flow battery with semi-solid reactants as described in Chiang et al., U.S. Pat. No. 7,338,734, where the active material in the anolyte and catholyte in the discharged state is based on LiMn2O4 (lithium manganese spinel). In this system upon charging, Li ions will be extracted from the LiMn2O4-containing particles in contact with the positive electrode, raising the potential, and inserted into the LiMn2O4-containing particles in contact with the negative electrode, lowering the potential. The potential difference between the anolyte and catholyte will rise from 0 to approximately 1.5V. Variants of LiMn2O4 in which an element partially substitutes for the Mn may also be used.
The various system embodiments may employ a variety of electrolyte storage tank configurations, such as those described above with reference to
The voltage of a flow battery, and its concomitant power rating, may be adjusted by varying the number of cells in each stage. However, large numbers of cells in a stage can result in shunt currents through the conductive anolyte and catholyte that are parasitic to the flow battery's energy storage efficiency. Alternatively, the power rating of a flow battery may be raised without altering the voltage rating by increasing the area (e.g., m2) or the current density (e.g., mA/cm2) of the cells within one or more cascade stages, thereby increasing the total battery current. Thus, the number of stages, the number of cells in each stage, and the design configurations applied to each cell may be varied based upon the design goals and performance requirements of a particular flow battery system.
One beneficial characteristic of a flow battery including a cascade stack assembly is that the operating voltage is relatively flat due to the constant reactant profiles within each cascade stage during charge and discharge. Steady operating voltages may be advantageous in some embodiments as this may reduce the number of capacitors required within a flow battery's power conditioning system (PCS) that converts the direct current (DC) electricity output to alternating current (AC) electricity. Reducing the number of capacitors within a PCS reduces its cost, increases its reliability, and increases its efficiency.
Typically, for the same general operating conditions (e.g., current density, flow rate, temperature, etc.) the charge voltage from a given collection of cells is higher than the discharge voltage due to internal resistances. To achieve more similar charge and discharge voltages, the charge voltage can be reduced by lowering the reactant flow rate during charge to reduce current density. Alternatively, a larger number of series-connected cells within each stage may be used when the flow battery is in discharge mode. In a bi-direction stack assembly, this may be achieved by incorporating appropriate valve arrangements or other flow bypass mechanisms. Operating voltage may also be tuned by providing a plurality of engineered cascade stack assemblies dedicated to the discharge process in addition to one or more separate engineered cascade stack assemblies dedicated to charging. To make operating voltages more similar, the operating current density, the number of cells, or the area of each cell in the discharge stack assembly may be increased relative to the charge stack assembly.
Embodiments of flow battery systems utilizing the engineered cascade systems of the various embodiments provide several advantages over non-cascade or non-engineered cascade flow battery systems. For example, as shown in
Embodiments of redox flow battery cells, stack assemblies and systems described herein may be used with any electrochemical reactant combinations that include reactants dissolved in an electrolyte. One example is a stack assembly containing the vanadium reactants V(II)/V(III) or V 2+/V 3+ at the negative electrode (anolyte) and V(IV)/V(V) or V 4+/V 5+ at the positive electrode (catholyte). The anolyte and catholyte reactants in such a system may be dissolved in sulfuric acid. This type of battery is often called the all-vanadium battery because both the anolyte and catholyte contain vanadium species. Other combinations of reactants in a flow battery that can utilize the features and advantages of the systems described herein include Sn (anolyte)/Fe (catholyte), Mn (anolyte)/Fe (catholyte), V (anolyte)/Ce (catholyte), V (anolyte)/Br 2 (catholyte), Fe (anolyte)/Br 2 (catholyte), Ti (anolyte)/Fe (catholyte), and S (anolyte)/Br 2 (catholyte). In each of these example chemistries, the reactants may be present as dissolved ionic species in the electrolytes, which permits the advantageous use of engineered cascade flow battery cell and stack assembly designs in which cells have different physical, chemical or electrochemical properties at different expected state of charge conditions along the cascade flow path (e.g., cell size, type of membrane or separator, type and amount of catalyst, etc.). A further example of a workable redox flow battery chemistry and system is provided in U.S. Pat. No. 6,475,661, which is incorporated herein by reference.
The foregoing description of the various embodiments is provided to enable any person skilled in the art to make or use the present invention. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the invention. Thus, the present invention is not intended to be limited to the embodiments shown herein, and instead the claims should be accorded the widest scope consistent with the principles and novel features disclosed herein.
This application is a Continuation-In-Part of U.S. patent application Ser. No. 12/883,511 filed Sep. 16, 2010, which is a Divisional of U.S. patent application Ser. No. 12/498,103, filed on Jul. 6, 2009, now U.S. Pat. No. 7,820,321, which claimed the benefit of priority to U.S. Provisional Patent Application No. 61/078,691 filed Jul. 7, 2008 and U.S. Provisional Application No. 61/093,017 filed Aug. 29, 2008, the entire contents of all four of which are hereby incorporated herein by reference.
Inventions conceived after the filing of the priority application (U.S. patent application Ser. No. 12/498,103, filed on Jul. 6, 2009) that are included in this continuation-in-part patent application were made with Government support under DE-OE0000225 “Recovery Act—Flow Battery Solution For Smart Grid Renewable Energy Applications” awarded by the US Department of Energy (DOE). The Government has certain rights in such inventions. However, the Government does not have rights in U.S. Pat. No. 7,820,321 which was conceived and filed without Government support, nor in the direct continuation and divisional applications thereof.
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| Number | Date | Country | |
|---|---|---|---|
| 20110223450 A1 | Sep 2011 | US |
| Number | Date | Country | |
|---|---|---|---|
| 61078691 | Jul 2008 | US | |
| 61093017 | Aug 2008 | US |
| Number | Date | Country | |
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| Parent | 12498103 | Jul 2009 | US |
| Child | 12883511 | US |
| Number | Date | Country | |
|---|---|---|---|
| Parent | 12883511 | Sep 2010 | US |
| Child | 12986892 | US |
