This invention generally relates to electrochemical flow systems, and more particularly to configurations of reaction cells and cell blocks within electrochemical flow systems.
Redox Flow Batteries (RFBs) are rechargeable systems in which the electrochemical reactants are dissolved in liquid electrolytes. The electrolytes, which are stored in external tanks, are pumped through a stack of reaction cells where electrical energy is alternately converted to and extracted from chemical energy in the reactants by way of reduction and oxidation reactions.
Redox flow battery systems provide substantial flexibility as energy storage capacity may be expanded by increasing tank sizes. Output power of a flow battery system may be expanded by increasing the number and/or size of electrochemical reaction cells. Reaction cells may be arranged into blocks or stacks containing multiple cells.
Thus in various embodiments, methods and systems are provided for configuring an electrochemical flow stack having various advantageous features. Embodiments of an electrochemical flow cell stack may comprising a plurality of frame layers, each of the plurality of frame layers having a peripheral gasket channel configured to receive a gasket material therein. The gasket channel may surround a recessed area having a size and a structure configured to receive an insert layer. Each of the plurality of frame layers may have at least one void area defining a first half-cell chamber of a flow cell. Further in embodiments, an electrochemical flow cell stack may have a plurality of insert layers, each of the plurality of insert layers being nested within a corresponding one of the plurality of frame layers. Each of the plurality of insert layers may have at least one void area defining a second half-cell chamber of the flow cell formed by one of the plurality of frame layers and one of the plurality of insert layers.
In embodiments, each of the plurality of frame layers may further include a plurality of openings defining inlet/outlet ports and at least a first channel defining a first flow path joining a first one of the plurality of openings defining the inlet/outlet ports to the first half-cell chamber and at least a second channel defining a second flow path joining the first half-cell chamber to a second one of the plurality of openings defining the inlet/outlet ports.
In embodiments, each of the plurality of insert layer may have a third channel defining a third flow path joining a third one of the plurality of openings defining the inlet/outlet ports to the second half-cell chamber and a fourth channel defining a fourth flow path joining the second half-cell chamber to a fourth one of the plurality of openings defining the inlet/outlet ports.
In embodiments, each of the plurality of insert layers and each of the recessed areas of the plurality of frame layers may be configured with a size and a shape such that each of the plurality of insert layers nests within corresponding ones of the plurality of frame layers in a single orientation.
In embodiments, each of the plurality of frame layers may have one or more flat surfaces surrounding the first channel, the one or more flat surfaces configured to seal against one or more adjacent structures in the electrochemical stack. Further in embodiments, the one or more adjacent structures may include one or more separator layers or one or more bipolar plate layers.
In embodiments, an electrochemical flow cell stack may also have a pair of structural base plates and a pair of structural clamping plates configured to secure the plurality of frame layers and the plurality of insert layers. Further in embodiments, an electrochemical flow cell stack may have a pair of sealing monopolar plate layers adjacent to the pair of structural base plates. In embodiments, the pair of sealing monopolar plate layers may be constructed from a non-reactive electrically conductive material that is impermeable to an electrolyte.
Further in embodiments, an electrochemical flow cell stack may have a first porous electrode positioned in the first half-cell chamber of each of the plurality of frame layers and a second porous electrode positioned in the second half-cell chamber of each of the plurality of insert layers. Further in embodiments, the first porous electrode may have a thickness greater than a thickness of one of the plurality of frame layers. Further in embodiments, the first porous electrode may be compressible such that a thickness of first porous electrode is reduced by compression when each of the plurality of frame layers and each of the plurality of insert layers are compressibly joined into a clamped configuration.
Further in embodiments, each of the plurality of frame layers and each of the plurality of insert layers may have at least one registration feature configured to align each of the plurality of insert layers relative to each of the plurality of frame layers.
Further in embodiments, an electrochemical flow cell stack may have a first electrode section positioned in the first half-cell chamber of each of the plurality of frame layers and a second electrode section positioned in the second half-cell chamber of each of the plurality of insert layers. Further in embodiments, an electrochemical flow cell stack may have a separator layer positioned between the first half-cell chamber of each of the plurality of frame layers and the second half-cell chamber of each of the plurality of insert layers. Further in embodiments, an area dimension of the first electrode section and the second electrode section may be substantially the same as an area dimension of an active area section of the separator layer.
Further in embodiments, the first half-cell chamber of each of the plurality of frame layers may be divided into a first sub-cell section and a second sub-cell section by a plenum channel, and the first sub-cell section may have a first porous electrode section and the second sub-cell section may have a second porous electrode section. Further in embodiments, each of the plurality of frame layers may have a first lateral channel adjacent to the first sub-cell section and a second lateral channel adjacent to the second sub-cell section. Further in embodiments, the plenum channel may have at least one flange extending into at least one of: the first sub-cell section and the second sub-cell section. Further in embodiments, at least one of the first lateral channel and the second lateral channel may have a flange extending into a respective at least one of the first sub-cell section and the second sub-cell section.
Further in embodiments, an electrochemical flow cell stack may have a separator layer having one or more active areas made of a semi-permeable membrane material and one or more inactive areas made of an impermeable material, and the one or more active areas may be configured to align with the first and second sub-cell sections. Further in embodiments, the semi-permeable membrane material of the one or more active areas may be bonded to the impermeable material of the one or more inactive areas by heat sealing.
Further in embodiments, a dimension of the first porous electrode section and the second porous electrode section may have substantially the same dimensions as the one or more active areas made of the semi-permeable membrane material.
Further in embodiments, an electrochemical flow cell stack may have a plenum channel having a central support rib. Further in embodiments, each of the plurality of frame layers may include a voltage test tab configured to provide an electrical connection to the first half-cell chamber.
Further in embodiments, an electrochemical flow cell stack may have a first structural end plate, a first base layer positioned adjacent to and in contact with the first structural end plate. The first base layer may have an outer peripheral gasket channel configured to receive a gasket material therein, and the outer peripheral gasket channel may surround a recessed area having a size and a structure configured to receive an insert layer. Further in embodiments, an electrochemical flow cell stack may have a first insert layer nested within the recessed area of the first base layer. The first insert layer may have at least one void area defining at least a portion of a first half-cell chamber of the first flow cell.
Further in embodiments, an electrochemical flow cell stack may have a first frame layer positioned adjacent to and in contact with at least portions of the first base layer and the first insert layer. The first frame layer may have an outer peripheral gasket channel configured to receive a gasket material therein. The gasket channel may surround a recessed area having a size and a structure configured to receive an insert layer. The frame layer may have at least one void area defining at least a portion of a second half-cell chamber of the first flow cell.
Further in embodiments, an electrochemical flow cell stack may have a second insert layer nested within the recessed area of the first frame layer, the second insert layer may have at least one void area defining at least a portion of a first half-cell chamber of a second flow cell. Further in embodiments, an electrochemical flow cell stack may have an Nth frame layer, where N is equal to the number of electrochemical cells in the stack. Further in embodiments, an electrochemical flow cell stack may have a second base layer positioned adjacent to and in contact with the Nth frame layer and a second structural end plate positioned adjacent to and in contact with the second base layer.
Further in embodiments, an electrochemical flow cell stack may have a first impermeable electrically conductive monopolar plate layer positioned between the first base layer and the first insert layer and sealing the first half-cell chamber from the first base layer.
Further in embodiments, an electrochemical flow cell stack may have a first separator layer sandwiched between the first insert layer and the first frame layer and having at least one semi-permeable active area section separating the first half-cell chamber from the second half-cell chamber. In embodiments, the first separator layer further may have one or more impermeable sections configured to seal one or more flow channels in at least one of the first insert layer and the first frame layer.
Further in embodiments, an electrochemical flow cell stack may have a first impermeable electrically conductive layer sandwiched between the first frame layer and the first insert layer, the first impermeable electrically conductive layer may seal at least one flow channel in at least one of the first frame layer and the first insert layer. In embodiments, the first insert layer may have a plenum channel dividing the first half-cell chamber into two sub-cell sections and first and second lateral flow channels across the sub-cell sections from the plenum channel.
Various embodiments are also provided herein for configuring a composite electrochemical separator. Some embodiments of a composite electrochemical separator may include a sheet of impermeable material with a first separator cutout section and a second separator cutout section, each of the first and the second separator cutout sections being entirely surrounded by a perimeter of the impermeable material. Further in embodiments, the composite electrochemical separator may have a first sheet of semi-permeable material and a second sheet of semi-permeable material bonded to the perimeter of impermeable material surrounding the first separator cutout section and the second separator cutout section of the impermeable material sheet.
In some embodiments, the semi-permeable material may comprise a micro-porous membrane material. Further in embodiments, the semi-permeable material may comprise an ion-selective membrane material.
Further in embodiments, the sheet of impermeable material may have inlet/outlet cutouts, each of which may be entirely surrounded by at least some of the impermeable material. Further in embodiments, the sheet of impermeable material may have a substantially rectangular shape and the inlet/outlet cutouts may be positioned adjacent each of the four corners of the rectangular shape.
Further in embodiments, the sheet of impermeable material may have positioning holes adjacent corners of the sheet of impermeable material, wherein the positioning holes may be arranged so as to not intersect the inlet/outlet cutouts.
Embodiments of an electrochemical flow cell stack may also include a first structural end plate and a first base layer positioned adjacent to and in contact with the first structural end plate. The first base layer may have an outer peripheral gasket channel configured to receive a gasket material therein, and the gasket channel may surround a recessed area having a size and a structure configured to receive an insert layer. Further in embodiments an electrochemical flow cell stack may have a first frame layer positioned adjacent to and in contact with at least portions of the first base layer and the first insert layer. The first frame layer may have an outer peripheral gasket channel configured to receive a gasket material therein, and the gasket channel may surround a recessed area having a size and a structure configured to receive an insert layer. Further in embodiments, an electrochemical flow cell stack may have a frame layer comprising at least one void area defining at least a portion of a first half-cell chamber of the first flow cell, and a first insert layer nested within the recessed area of the first frame layer. The first insert layer may have at least one void area defining at least a portion of a second half-cell chamber of the first flow cell. The first insert layer may also have a plenum channel dividing the first half-cell chamber into two sub-cell sections.
Further in embodiments, an electrochemical flow cell stack may have a first separator layer sandwiched between the first insert layer and the first frame layer and having at least one semi-permeable active area section configured to separate the first half-cell chamber from the second half-cell chamber. The first separator layer may have impermeable sections sealing at least one of the plenum channel and a flow channel in at least one of the first insert layer and the first frame layer.
Further in embodiments, an electrochemical flow cell stack may have a first impermeable electrically conductive layer positioned adjacent to and in contact with the first insert layer. The first impermeable electrically conductive layer may be configured to seal and enclose at least one of the first and the second lateral flow channel in the first insert layer.
Further in embodiments, an electrochemical flow cell stack may have an Nth frame layer, where N is equal to the number of electrochemical cells in the stack, a second base layer positioned adjacent to and in contact with the Nth frame layer, and a second structural end plate positioned adjacent to and in contact with the second base layer.
The novel features of the invention are set forth with particularity in the claims that follow. A better understanding of the features and advantages of the present invention will be obtained by reference to the following detailed description that sets forth illustrative embodiments, in which the principles of the invention are utilized, and the accompanying drawings of which:
The various embodiments will be described in detail with reference to the accompanying drawings. 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.
The various embodiments below provide improved electrochemical cell and stacked cell block structures that may improve operating efficiency and other performance metrics in electrochemical flow systems such as flow batteries, electrosysnthesis systems, and others. In some embodiments, flow-through electrochemical cells with a large active surface area may be divided into multiple active sections, such as two active sections separated by a flow-directing plenum. This configuration may allow for improved electrolyte flow and decreased pressure gradients within cells and cell blocks while maintaining a large active surface area. In some cases, positive and negative half-cells of such a divided active area cell may be separated by a composite separator layer that includes one or more permeable or semi-permeable sections that allow ions to diffuse from one half-cell to the other in active cell areas. Permeable or semi-permeable separator sections may be bonded to an impermeable material configured to prevent passage of ions or liquid from one half-cell to the other in inactive regions of the cell. Other embodiments may provide improved structures for sealing fluid-containing portions of adjacent half-cells while also sealing a stack against external leaks.
Certain terms that are used throughout the application are explained here. Other terms that appear less frequently are explained as they arise.
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 electrochemical flow system (or ECFS) may include redox flow batteries (“RFBs”) which may include electrochemical energy storage systems in which one or more fluid electrochemical reactants may be flowed through a reaction cell in which electrical energy may be converted to and/or from chemical energy. Electrochemical flow systems may also include electrosysnthesis systems in which chemical elements or compounds may be synthesized, purified or otherwise changed through electrochemical processes as one or more fluid (e.g., gas, liquid, slurry, colloidal dispersion, etc.) reactant is flowed through one or more flow-through electrochemical reaction cells.
The term semi-permeable membrane as used herein may refer to any semi-permeable membrane, selectively permeable membrane, partially permeable membrane, or differentially permeable membrane, as understood by those skilled in the art. For example, the term semi-permeable membrane may refer to any membrane material that will allow certain molecules or ions to pass through it by diffusion while preventing other molecules from passing through. In various embodiments of electrochemical flow systems, semi-permeable separator membranes may be ion-selective membranes such as Nafion, or microporous membranes which are not necessarily ion-selective. Microporous membranes may include microporous membrane separators manufactured by Celgard LLC, and membrane separators made by Daramic LLC. In some cases, the term “permeable” may be used herein to refer to materials that are not entirely impermeable, and may include both highly permeable materials and semi-permeable materials. Impermeable materials may include any materials that are substantially impermeable to any of the molecules or ions involved in the electrochemical flow system some examples of impermeable materials for particular aspects of an electrochemical flow system are described below.
As used herein, the terms “optimized,” “optimum” and similar variants are merely intended to indicate relative quantitative or qualitative improvements to performance or other variables. Use of these terms is not intended to imply or require that such factors are necessarily designed for the best possible or theoretical performance. The terms may alternatively or additionally refer to a configuration that achieves a degree of performance, such as a specific or predetermined degree of performance that will have beneficial effects in the configured part or other parts of the system.
Unless otherwise specified, the terms anolyte and catholyte are used herein as if the battery were always in a discharge mode. Hence, the term “anolyte” will refer to the electrolyte in contact with the negative electrode of an electrochemical reaction cell and the term “catholyte” will refer to the electrolyte in contact with the positive electrode of an electrochemical reaction cell.
As used herein, the phrase “state of charge” and its abbreviation “SOC” refer to the instantaneous ratio of useable to theoretical stored electrical charge (measured in ampere-hours). The terms may be applied either to the charge storage capacity of a complete RFB system or to electrolytes within a particular component of the RFB. “Useable” charge may refer to stored charge that may be delivered at or above a threshold voltage (e.g. about 0.7 V in some embodiments of Fe/Cr RFB systems).
The energy produced or consumed by an electrochemical cell can be expressed as the product of cell voltage, current and time (Joules=Volts×Amps×Seconds). Energy losses within the cell can arise from two distinct effects, known as “Voltage efficiency” and “Faradaic efficiency”.
Voltage efficiency falls below unity when the measured cell voltage deviates from the theoretical potential difference (the so called “thermodynamic reversible potential”) for that cell. The magnitude of the voltage deviation is known as the cell “overpotential” and in general the overpotential includes contributions from energy losses at each electrode. The overpotential at the cell anode (i.e., the electrode at which oxidation is occurring) has a positive sign, while the overpotential at the cell cathode (i.e., the electrode at which reduction is occurring) has a negative sign. Hence, on charge, the two overpotentials combine to increase the cell voltage (wasting some of the input energy) and on discharge, they combine to decrease the cell voltage (wasting some of the output energy).
As used herein, the term “Faradaic efficiency” refers to the proportion of the electric current flowing at an electrode that achieves the intended oxidation or reduction reaction. A Faradaic efficiency of unity means that none of the current is wasted on parasitic reactions (defined below). In RFBs, Faradaic efficiencies smaller than unity can arise from an inadequate supply (or “flux”) of redox reagent to the electrode surface or imperfect selectivity for the preferred reaction.
As used herein, the terms “stoich” and “stoich flow” refer to the ratio of the flux of a redox reactant entering an electrochemical cell (or cell module) to the rate at which the reactant is consumed in the cell (or cell module). The reactant flux depends on both the concentration of the reactants in the electrolytes and the flow rate of the electrolytes into the cell. The rate at which reactants are consumed depends on the electric current supplied to the cell (during charging) or drawn from the cell (during discharge).
To illustrate the meaning of stoich, we may consider a cell that is being supplied with 10−4 mole per second of the reactant Fe3+, which is being consumed in the reduction reaction expressed in EQ(1):
Fe3++e−=Fe2+ EQ(1)
A current of 10−4 moles per second of electrons (e.g., 10−4 Faraday per second or approximately 9.65 amps) provides electrons at a rate and molar concentration equal to the supply of the reactant. Hence a current of the above noted magnitude would give a stoich value of unity in the cell. Similarly, a current of half the above noted magnitude would result in a reduced rate of consumption of the reactant giving a stoich value of 2.0.
Like Faradaic efficiency, stoich is a dimensionless quantity and the term applies to both charging and discharging reactions. For these and other reasons, stoich values substantially greater than unity may be required to prevent significant losses in Faradaic efficiency.
When the Faradaic efficiency at one or both electrodes in a cell falls below unity, the electrode or electrodes can be driven into overpotential ranges where “parasitic” electrode reactions arise to make up the deficit in Faradaic current. For example, in the Fe/Cr RFB, low stoich conditions in the negative electrolyte during charge can drive the electrode potential low enough to initiate hydrogen evolution via the electrode reaction expressed in EQ(2):
2H++2e−=H2. EQ(2)
Similarly, low stoich conditions in the positive electrolyte during charge can drive the electrode potential high enough to initiate chlorine evolution via the electrode reaction expressed in EQ(3):
2Cl−═Cl2+2e− EQ(3)
Parasitic reactions can also arise when low stoich conditions develop during discharge.
All of the charge consumed in parasitic reactions subtracts directly from the “useable” charge stored by the battery. As used herein, the term “useable” charge refers to stored charge that may be delivered at or above a threshold voltage (e.g. about 0.7 V in some embodiments of the Fe/Cr RFB system).
In some cases, the positive and negative electrodes 24, 34 may comprise a porous electrically conductive material configured to allow a fluid reactant to flow through the chamber while conducting electrical currents to the positive and negative current collectors 22, 32. Such electrode materials may include carbon or graphite felt or other porous matrix carbon or graphite materials. In some cases, electrodes may comprise metallic materials formed into felt, braids, or other structures suitable for flowing electrolyte through. Terms such as “electrode,” “felt,” or “electrode felt” may be used herein to refer to any suitably configured flow-through conductive structure.
In some cases, metallic electrodes may be entirely made of or coated with a non-reactive or positively-reactive surface layer. Depending on the intended application of the flow system, the electrodes may comprise other reactive and/or non-reactive materials. Current collector plates may generally be made of any material with a suitable combination of electrical conductivity, reactivity (or non-reactivity) with electrolytes, and structural strength/flexibility. Such materials may include carbon plates, carbon-impregnated polymer materials or others.
A single electrochemical cell may provide a limited voltage or limited processing capacity. In order to increase the voltage of a system, a plurality of cells may be combined in an electrically series-connected configuration.
During operation, the reactants may undergo reduction and oxidation reactions as the fluid reactants pass through and contact the positive and negative electrodes 24 and 34 respectively, generating or consuming DC power. In a recirculating system (an example of which is shown
In other electrochemical flow system architectures, electrolytes may be fully discharged in a single fluid pass through the cell stack and the spent electrolytes may be collected in separate tanks (for a total of at least four separate tank volumes). An effective implementation of this single pass (or “4-tank”) architecture is a cascade flow stack in which electrolytes pass through a series of stages, each of which incrementally increases or decreases the state-of-charge of electrolytes.
A variation of the cascade ECFS architecture is an engineered cascade in which cells, stages and/or arrays within the battery are configured to increase the battery's performance over that achievable in a cascade RFB in which all cells, stages and/or arrays along the reactant flow path are substantially the same as one another. For example, within an engineered cascade RFB, each cascade stage may be tailored to a specific SOC range. Various examples of such engineered cascade RFB systems are provided in U.S. Patent Application Publication No. 2011/0223450, which is incorporated in its entirety herein by reference.
The term “engineered cascade” is used herein to refer generally to a cascade ECFS in which cells, stages and/or arrays within the battery are configured in terms of materials, shapes and sizes, reactant flow, and/or other variables based on an expected condition of reactants. The engineered cascade may be configured, for example, to achieve a range of electrolyte SOC to be experienced by the cells so as to increase the battery's performance. Performance parameters such as round trip energy efficiency, power output, reduced electrolyte breakdown, reduced hydrogen generation, improved safety, decreased material degradation, or other performance metric may be advantageously increased over that achievable in a cascade ECFS in which all cells, stages and/or arrays along the reactant flow path are substantially the same as one another.
U.S. Patent Application Publication No. 2011/0223450 provides several examples of possible configurations for individual flow battery cells, blocks containing multiple cells, and stacks containing multiple cell blocks. The embodiments set forth herein, and other embodiments, may be used in combination with any of the systems disclosed in U.S. Patent Application Publication No. 2011/0223450 or other available systems.
In some embodiments, frame layers and insert layers may be injection molded or otherwise molded from a suitable material such as nylon, high density polyethylene, low density polyethylene, polyvinyl chloride, chlorinated polyvinyl chloride, or other moldable or machinable thermoplastic or thermoset plastic or composite materials. Alternatively, frame layers and insert layers may be molded or machined from plastics, metals, carbon, or other materials selected or treated to be impervious to corrosive electrolytes.
With reference to
The cell frame layer 120 of
The internal section 128 may also include a first shunt channel 135 providing a fluid path between a first corner port 140a and the plenum channel 133. A second shunt channel 137 may provide a fluid channel between a third corner port 140c and lateral flow channels 142. The shunt channels 135 and 137 in
In some embodiments, the shunt channels 135, 137 may be formed as channels in the top surface 122 of a cell frame layer 120, or as channels in the bottom surface 123 of a cell frame layer 120 (e.g., as shown in
As shown in
As shown in
In some embodiments, as shown for example in
One advantage of the above described nested construction is the provision of multiple sealing surfaces as can be seen in various figures including in
An O-ring gasket 164 may be provided in an O-ring channel 166 surrounding each in-flow and out-flow port, such as the corner ports 140a, 140b, 140c, 140d. In addition to providing mating surfaces for the O-ring gaskets 164 in the O-ring channels 166, the nested cell layer configuration may also provide substantial flat surfaces with large surface areas relative to liquid flow channels, such as the shunt channels 136, 138, 135 and 137. The flat surfaces may be pressed together when the stack is clamped together. The mating flat surfaces themselves, and the pressure applied to hold the flat surfaces together, may provide further sealing action preventing electrolyte from flowing through areas other than designated flow channels.
Further, the cell frame layer 120 may be configured with an apron portion 170 configured to surround and engage a corresponding shoulder 172 of an adjacent cell frame layer 120 as shown for example in
In various embodiments, each electrode chamber of a cell in either a frame layer 120 or an insert layer 110 may be divided into two or more sub-sections as shown, for example, in various figures including
In some embodiments, electrolyte flow structures such as plenum channels, lateral flow channels, shunt channels may be configured substantially similarly in both frame layers and insert layers. Alternatively, such structures may be configured differently in frame layers than corresponding structures in insert layers. For example, in some embodiments, electrolyte flow structures of an insert layer may be configured to cause a greater resistance to flow relative to flow structures in a frame layer. Such a variation of structure or other parameter may be configured or optimized to counteract a pressure gradient between two flowing liquid electrolytes, such as by increasing flow resistance for an electrolyte that tends to be at a lower pressure under equal flow conditions.
As shown in various examples, each half-cell chamber may be divided into two sub-cell sections. In alternative embodiments, half-cell chambers may be divided into three, four or more sub-cell sections by providing additional plenum structures and/or other flow channels extending through or around a peripheral portion of a half-cell chamber or a sub-cell section.
In some cases, as shown for example in
The plenum channels 133, 134 may further include structures for providing mechanical support when multiple cells are stacked together into a cell block. For example, as shown in
In various embodiments, other plenum support structures may also be provided in order to resist abrasion of bipolar sheets or other materials when stacked cells are compressed. For example, the supporting central rib 182, walls of the plenum channel 133, 134, the flanges 190, or other structures may have other shapes, such as the sinusoidal shape 430 as shown in
In the arrangement of
With reference to
In some cases, electrolytes may be directed through the sub-cell sections 132a, 132b of the insert layer 110 and cell frame layer 120 in the same direction at the same time. Thus, for example, if one electrolyte is flowed through a cell frame layer 120 such that the electrolyte moves from the plenum channel 134 to the lateral channels 142a, 142b, then the second electrolyte may be simultaneously flowed through the insert layer 110 such that the second electrolyte moves from the plenum channel 134 to the lateral channels 142a, 142b. Alternatively, a cross-flow configuration may be used in which a first electrolyte may flow through a cell frame layer 120 in an opposite direction relative to the second electrolyte flowing through the insert layer 110.
As shown in
As shown in
In some cases, flow structures may be provided in the insert layer 110 in a substantially identical pattern to those in the cell frame layer 120. By placing the insert layer 110 into the cell frame layer 120 such that the flow structures are rotated 180 degrees relative the structures in the cell frame layer 120, the electrolytes may flow into and out of the insert-layer sections such as the sub-cell sections 132a, 132b via the two ports that are not joined to the flow or shunt channels 135, 137 of the cell frame layer 120. Thus, the insert layer 110 and the cell frame layer 120 may provide chambers for the opposite (positive and negative) electrolytes while preventing mixing or other interaction of the electrolytes. Configuring insert layers and frame layers with identical flow structures provides the advantage that each electrolyte flow stream will experience the same flow resistance as electrolytes are pumped through a complete stack.
In some embodiments the cell frame layer 120 and the insert layer 110 may include mating structures configured to cause the insert layer 110 to only fit in the frame layer in a desired orientation. Thus, for example, one corner of a cell frame layer 120 may include an enlarged recess 211 (e.g., see
In some embodiments, a separator membrane may be positioned between a cell frame layer 120 and an insert layer 110 nested within the cell frame layer 120 with a first current collector layer below the cell frame layer 120 and a second current collector layer above the cell frame layer 120. In such embodiments, a complete cell may be formed by a cell frame layer 120 and an insert layer nested therein.
Alternatively, a current collector plate may be positioned between a cell frame layer 120 and an insert layer 110 nested within the same cell frame layer 120, and a separator layer may be positioned between an insert layer 110 and a concave region of an adjacent cell frame layer 120. In such embodiments, a complete cell may be formed by an insert layer and an adjacent frame layer.
As shown in
In some embodiments, active regions 222a, 222b may be permeable or semi-permeable and may be joined to impermeable inactive regions 224 by any suitable sealing or bonding method. For example, the sections may be heat sealed by applying heat and pressure to a region at which a portion of the permeable or semi-permeable separator material overlaps a portion of the impermeable material, thereby forming seams 225 surrounding the perimeter of the active regions 222a, 222b. Alternatively, the sections may be ultrasonically welded by overlapping a portion of the permeable or semi-permeable material with a portion of the impermeable material and treating the overlapping region with high frequency ultrasound energy with or without pressure applied to the overlapping regions. Alternatively, the sections may be bonded with adhesives or solvents by applying an adhesive or solvent to a portion of one or both of the permeable or semi-permeable material and the impermeable material and pressing the materials together. Alternatively any combination of such methods or any other sealing or bonding methods may be used.
With reference to
In some cases, to provide further structural rigidity, the central recessed area 344 of the base plate 314 may be configured to receive a rigid element such as a structural metallic plate 348 as shown in
As shown in
In some embodiments, a bipolar plate layer 360 of a non-reactive electrically conductive material may be placed over the electrically conductive end plate 356 in the base plate 314 as shown for example in
As shown in
As shown in
In some embodiments, the electrode felt sections 366a, 366b may be sized to be thicker in an un-compressed state than a maximum thickness of the insert layer 110, allowing the felt sections to be compressed when the final stack assembly is clamped together. Using material that is thicker when uncompressed, and compressing the material during clamping may advantageously increase the electrical conductivity of the felt sections due to the bulk increase in the amount of material used. Similarly, the O-ring gaskets 164 and gaskets 162 may be sized so as to have a thickness that extends beyond a surface of an insert layer 110 or cell frame layer 120. The O-ring gaskets 164 and the gaskets 162 may also be made of materials selected to compress or deform slightly when a final assembly is clamped together to improve the sealing action. The electrode felt sections 366a, 366b may generally be made of a non-reactive electrically conductive material through which a liquid electrolyte may flow, even when compressed. For example, carbon or graphite felt may be cut or stamped to a desired shape.
As shown in
In some embodiments, the separator layer 220 may be configured as a continuous layer of an ion-selective membrane or a microporous membrane. In other embodiments, as shown in
Whether configured as a continuous permeable or semi-permeable material or a composite construction, the separator layer 220 may include cutout regions at the inlet/outlet ports, such as the corner ports 140a-140d. The cutouts may have a size and shape that substantially matches the inlet/outlet ports such that, when compressed, the separator layer seals against flat surfaces of an insert layer 110 and an adjacent cell frame layer 120.
As shown in
As shown in
As shown in
Once a desired number of cells has been assembled, a top base plate 380 may be placed over the final cell frame layer 120.
When configuration of the components and assembly of the stack is completed, the stack may be sandwiched between top and bottom clamping plates, such as the upper structural end plate 310, and the lower structural end plate 312.
In some cases, an assembly of a group of cells between a top base plate 380 and a base plate 314 may be referred to herein as a “cell block.” A cell block may be defined as a group of electrochemical cells in a common bipolar stack configured to operate as a common unit. In some cases, two or more cell blocks may be provided between a single pair of clamping plates such as the upper structural end plate 310, and the lower structural end plate 312. When two or more cell blocks are provided between a single pair of clamping plates, such as the upper structural end plate 310, and the lower structural end plate 312, the cell blocks may each be electrically isolated from adjacent cell blocks, thereby allowing for convenient mechanical assembly while allowing for variability in electrical connection configurations.
As shown in the close-up view of
Nested Frame Layers with Inner and Outer Seals
One consideration in flow through cells and cell blocks is the hydraulic pressures needed to pump electrolytes through the chambers of multiple cells in a bipolar stack. In some cases, significantly high pressures may be required. In such cases, seals for preventing electrolytes from leaking out of a cell or out of a cell block may be needed. On one hand, it may be desirable to seal each cell chamber from adjacent sub-cell sections in order to reduce cross-cell leakage which may reduce operating efficiency of a flow battery. In addition, it may also be desirable to seal an entire stack to prevent electrolytes from leaking out of the stack and causing external damage or contamination.
Configuration of seals in a flow battery stack may involve balancing many competing factors, including minimizing cross-cell leaks, minimizing pressure drop, minimizing weight, minimizing material costs, maximizing safety, etc. In some flow battery arrangements, a certain degree of cross-mixing of positive and negative electrolytes may be acceptable. Thus, in some cases it may be possible to de-couple some stack configuration objectives, such as decreasing the risk of external leaks and minimizing pressure drop and material cost. Some flow battery configurations using structures and configurations described herein may deal separately with these two sealing needs.
For example, as can be seen in
A main inner seal, such as the compressible gasket 408, may surround each positive cell chamber 412 and may provide a seal substantially preventing electrolyte from leaking out of a cell chamber 412 into adjacent cell chambers 420. The inner seal, such as the compressible gasket 408 may be configured to withstand a relatively low pressure, which may be substantially close to an operating pressure of a flow battery stack. In some examples, operating pressures may be about 10 psi to about 50 psi. In some embodiments, such as shown in
An outer seal 416 may be provided to surround substantially all of the cell components, and may be configured to withstand a substantially higher pressure, thereby providing a high margin of safety against electrolyte leaking from the stack assembly. The outer seal 416 may include a compressible gasket 410 sandwiched and compressed into a seal channel.
Although this invention has been disclosed in the context of certain preferred embodiments and examples, it will be understood by those skilled in the art that the present invention extends beyond the specifically disclosed embodiments to other alternative embodiments and/or uses of the invention and obvious modifications and equivalents thereof. Various modifications to the above 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. For example, any of the individual components described above, or some combinations of the components may be considered non-essential to a complete electrochemical flow cell stack. Any of the components may be modified or omitted as may be suitable for a particular embodiment application. Thus, it is intended that the scope of the present invention herein disclosed should not be limited by the particular disclosed embodiments described above, but should be determined only by a fair reading of the claims that follow.
In particular, materials and manufacturing techniques may be employed as within the level of those with skill in the relevant art. Furthermore, reference to a singular item, includes the possibility that there are plural of the same items present. More specifically, as used herein and in the appended claims, the singular forms “a,” “and,” “said,” and “the” include plural referents unless the context clearly dictates otherwise. As used herein, unless explicitly stated otherwise, the term “or” is inclusive of all presented alternatives, and means essentially the same as the phrase “and/or.” It is further noted that the claims may be drafted to exclude any optional element. As such, this statement is intended to serve as antecedent basis for use of such exclusive terminology as “solely,” “only” and the like in connection with the recitation of claim elements, or use of a “negative” limitation. Unless defined otherwise herein, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
The present application claims the benefit of priority to U.S. Provisional Application No. 61/901,160 entitled “CELL AND CELL BLOCK CONFIGURATIONS FOR REDOX FLOW BATTERIES,” filed on Nov. 7, 2013, the entire contents of which are incorporated by reference herein.
Inventions included in this 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 these inventions.
Number | Date | Country | |
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61901160 | Nov 2013 | US |