Photo-electrochemical cells and corresponding devices

Abstract

The present invention relates to an electrochemical cell (1) comprising a first reaction chamber with a first electrode (104a), a second reaction chamber with a second electrode (104b), and a membrane-electrode assembly (106) arranged between the two reaction half-chambers and comprising an ion-exchange membrane (106a). The electrochemical cell further comprises a photovoltaic system (101) configured to absorb solar energy and generate an output voltage between two output terminals. The two output terminals are each selectively coupleable to each of the two electrodes, and the ratio between the light-sensitive area of ​​the photovoltaic system and the active area of ​​the two electrodes is less than or equal to 50. The photovoltaic system comprises a plurality of photovoltaic cells (150) selectively coupleable between the two output terminals in a configuration including series, parallel, or a mixed series / parallel configuration. The electrochemical cell comprises an electronic control unit (109) configured to couple the plurality of photovoltaic cells in a selected one of said configurations.

Description

[Technical field]

[0001] The present disclosure relates to electrochemical cells (eg, electrolysers or electrochemical reactors) and corresponding devices for producing chemical products, such as hydrogen produced by electrolysis. [Background technology]

[0002] Global energy demand is increasing and was about 150,000 TWh in 2020. To produce this amount of energy, about 35 billion tons of carbon dioxide (CO2) and many other pollutants are emitted every year.

[0003] When using photovoltaic systems to convert solar energy into energy that can be used for human activities, problems arise with the storage of the generated energy. Also, storage systems such as batteries have a low energy density, which makes them inconvenient for many applications and long-term storage. It is therefore desirable to directly convert solar energy into an energy vector of a chemical nature, such as hydrogen.

[0004] Hydrogen is a fuel that has attracted great interest, especially in the energy and transportation industries, due to its high energy density (or specific energy) per unit mass. Hydrogen can be produced by extraction from natural compounds in various ways, but so far, most of the hydrogen produced worldwide has been obtained from fossil fuels. For example, so-called brown hydrogen is produced from coal in a process known as gasification, while grey hydrogen is extracted from natural gas by a process known as "steam reforming" of methane. Both processes emit large amounts of carbon dioxide. So-called blue hydrogen is produced from fossil fuels while simultaneously using carbon capture and storage technologies to reduce carbon dioxide emissions into the atmosphere.

[0005] Another method of producing hydrogen is based on the electrolysis process, in which an electrolysis cell uses an electric current to split compounds into their components. In the case considered here, the starting compound is water, which is split into hydrogen and oxygen in the so-called water splitting reaction. If the electrical energy supplied to the electrolysis cell comes from renewable sources such as wind or solar power, the hydrogen produced is defined as "green hydrogen".

[0006] Three main types of systems (so-called solar hydrogen technologies) are known in the art that utilize solar energy for the production of hydrogen by electrolysis: photocatalytic (PC) systems, photoelectrochemical (PEC) systems, and photovoltaic-photoelectrochemical (PV-EC) systems.

[0007] Photocatalytic (PC) type cells represent a water splitting device that is simpler in terms of the technology and components used in the device. In photocatalytic cells, the photocatalytic material is in powder form in an electrolyte solution, so the charge transfer path between the two electrodes of the cell is short and the reaction occurs quickly. Hydrogen and oxygen are produced on the same particle of photocatalytic material. Therefore, photocatalytic systems require further processes to separate the gases after they are produced. In general, photocatalysts are composites consisting of a light-harvesting semiconductor and one or more cocatalysts. When the semiconductor absorbs photons with energy higher than the band gap of the semiconductor material, electron-hole pairs are generated. Meanwhile, the hydrogen evolution reaction (HER) and oxygen evolution reaction (OER) occur on the cocatalyst.

[0008] Photoelectrochemical (PEC) type cells are generally obtained by photoelectrodes (photoanode and / or photocathode) connected to a charge collector and electrically connected to each other. Conventionally, only the light absorbing side of the photoelectrode is in contact with the electrolytic phase, while the side connected to the charge collector is isolated from the liquid. Photoelectrochemical cells are usually A single p-type photocathode; an OER catalytic anode or an n-type photoanode; a HER catalytic cathode; Equipped with.

[0009] Photoelectrochemical cells with the above configuration require the application of an external voltage to compensate for overpotential and overall losses. A practical way to provide this additional potential consists of combining a photocathode / photoanode system (i.e., a PEC cell) with a photovoltaic cell to obtain a photovoltaic-photoelectrochemical (PV-PEC) cell.

[0010] A photovoltaic-photoelectrochemical (PV-EC) system consists of a photovoltaic device connected to a selected electrocatalytic material, providing the energy required to trigger the water splitting reaction. The efficiency of a PV-EC cell therefore depends on both the performance of the photovoltaic cell and the performance of the electrocatalyst.

[0011] Photovoltaic-photoelectrochemical devices (PV-EC) have several advantages over PC and PEC systems. In particular, PV-EC devices do not envisage, by construction, immersion of the photovoltaic element in the electrochemical phase solutions and reagents or direct contact with them, and do not suffer from problems of corrosion or low stability of the light absorber. Furthermore, the fact that the photogeneration of charges (electron-hole pairs) and electrocatalysis occur separately allows for easy scalability of the system, allowing independent adjustment of the dimensions of the photovoltaic cell and the electrocatalyst. On the other hand, the complexity of the individual systems and their communication and synergistic arrangement leads to an overall increase in the cost of the PV-EC device, and represents the main drawback of PV-EC type cells.

[0012] The US patent application US2018 / 0171492A1 and the document "Direct Solar-to-Fuel CO2 Reduction", Alessandro Monticelli, University of Illinois at Chicago, Thesis, 2015 (available online at the following internet address: https: / / hdl.handle.net / 10027 / 19561) describe a simple electrolysis cell suitable for producing synthesis gas (a mixture of hydrogen and carbon monoxide) starting from water and carbon dioxide. In general, the document US2018 / 0171492A1 mainly teaches the chemical catalytic aspects of the reduction reaction of CO2. According to the document, the reaction half-chamber of the electrolysis cell and the photovoltaic cell are arranged such that the photovoltaic cell is in electrical contact with the anode and the cathode and the two reaction half-chambers are in ionic contact with each other.

[0013] However, the known devices described in the above two documents have low efficiency and are difficult to scale to dimensions suitable for industrial and commercial situations, making them less applicable in industrial applications. Summary of the Invention [Problem to be solved by the invention]

[0014] In view of the above, there is a need in the art to provide improved electrochemical cells suitable for industrial applications, for example, it is desirable to provide electrochemical cells that allow the production of chemical products with directly supplied solar energy, that are capable of producing chemical energy vectors (e.g. hydrogen) in a wide range of ways, and that allow distributed and stand-alone production. [Means for solving the problem]

[0015] It is an object of one or more embodiments to provide an electrochemical cell (or electrochemical reactor) integrated with a solar energy absorption system, having higher efficiency and more versatile uses compared to known devices.

[0016] According to one or more embodiments, this object is achieved by an electrochemical cell having the features set forth in the claims.

[0017] One or more embodiments may relate to a corresponding device that includes a plurality of electrochemical cells.

[0018] The claims form an integral part of the technical teachings provided herein in connection with the embodiments.

[0019] Briefly, one or more embodiments relate to an electrochemical cell comprising a first reaction chamber including a first electrode and a second reaction chamber including a second electrode, with a membrane-electrode assembly (MEA) disposed between the first and second reaction chambers. The membrane-electrode assembly includes an ion exchange membrane. The electrochemical cell further comprises a photovoltaic system configured to absorb solar energy and generate an output voltage between a first output terminal and a second output terminal of the photovoltaic system. The first output terminal of the photovoltaic system can be selectively coupled to the first electrode, and the second output terminal of the photovoltaic system can be selectively coupled to the second electrode. A ratio of a photosensitive area of ​​the photovoltaic system to an active area of ​​the first and second electrodes is 50 or less.

[0020] Furthermore, in one or more embodiments, the photovoltaic system comprises a plurality of photovoltaic cells, which can be selectively coupled between a first output terminal and a second output terminal of the photovoltaic system in a series configuration, a parallel configuration, or one or more mixed series / parallel configurations, where a mixed series / parallel configuration is to be understood as a configuration in which the cells are arranged in groups, each group comprising a plurality of cells connected in parallel, and different cell groups being connected in series. The electrochemical cell comprises an electronic control unit configured to couple the photovoltaic cells in a selected one of said configurations depending on one or more parameters that can be set by a user, and / or depending on one or more signals received from an external control unit, and / or depending on one or more signals received from one or more sensors included in the electrochemical cell.

[0021] One or more embodiments relate to an apparatus comprising a plurality of electrochemical cells according to one or more embodiments, a first storage reservoir in fluid communication with a first reaction half-chamber of the electrochemical cells for receiving a first gaseous reaction product, a second storage reservoir in fluid communication with a second reaction half-chamber of the electrochemical cells for receiving a second gaseous reaction product, and an apparatus electronic control unit. The apparatus further comprises a first distribution circuit in fluid communication with the first reaction half-chamber of the electrochemical cells for distributing a first reaction fluid, and a second distribution circuit in fluid communication with the second reaction half-chamber of the electrochemical cells for distributing a second reaction fluid. The first distribution circuit comprises a first apparatus pump controlled by the apparatus electronic control unit to regulate the flow of the first reaction fluid introduced into the first distribution circuit, and the second distribution circuit comprises a second apparatus pump controlled by the apparatus electronic control unit to regulate the flow of the second reaction fluid introduced into the second distribution circuit.

[0022] Various embodiments will now be described, by way of example only, with reference to the accompanying drawings, in which: [Brief description of the drawings]

[0023] [Figure 1] 1 is an exploded view of an electrochemical cell according to one or more embodiments; [Diagram 2] FIG. 2 is an exploded view of the electrochemical cell of FIG. 1, highlighting some of the operating principles of the electrochemical cell; [Diagram 3] FIG. 1 illustrates the operating principle of an electrochemical cell according to one or more embodiments. [Figure 4] FIG. 1 illustrates an apparatus for producing a chemical product comprising a plurality of electrochemical cells, according to one or more embodiments. [Diagram 5] FIG. 5 illustrates an embodiment of the device of FIG. [Figure 6] FIG. 5 shows a further embodiment of the device of FIG. [Figure 7A] FIG. 2 is a plan view showing details of an electrochemical cell implementation according to one or more embodiments. [Figure 7B]FIG. 1 is an axonometric view showing implementation details of an electrochemical cell according to one or more embodiments. [Figure 7C] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 7D] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 7E] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 7F] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 7G] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 7H] FIG. 1 illustrates details of an electrochemical cell implementation according to one or more embodiments. [Figure 8A] FIG. 1 is an exploded view of some components of an electrochemical cell according to one or more embodiments. [Figure 8B] FIG. 1 is an exploded view of some components of an electrochemical cell according to one or more embodiments. [Figure 8C] FIG. 1 is an exploded view of some components of an electrochemical cell according to one or more embodiments. [Figure 9] 1 is a current-voltage graph illustrating the operating principle of one or more embodiments; [Figure 10] 1 is a current-voltage graph illustrating the operating principle of one or more embodiments; [Figure 11] 1 is a current-voltage graph illustrating the operating principle of one or more embodiments; [Figure 12] 1 is a current-voltage graph illustrating the operating principle of one or more embodiments; [Figure 13A] FIG. 1 is a diagram showing an example of operation of one or more embodiments according to a first configuration example. [Figure 13B] FIG. 1 is a diagram showing an example of operation of one or more embodiments according to a first configuration example. [Figure 14A] FIG. 13 is a diagram showing an example of the operation of one or more embodiments according to a second configuration example. [Figure 14B] FIG. 13 is a diagram showing an example of the operation of one or more embodiments according to a second configuration example. [Figure 15] FIG. 1 illustrates possible details of an implementation of an electrochemical cell according to one or more embodiments. [Figure 16A] FIG. 13 is a diagram showing an example of the operation of one or more embodiments according to the third configuration example. [Figure 16B] FIG. 13 is a diagram showing an example of the operation of one or more embodiments according to the third configuration example. [Figure 17] FIG. 1 is a diagram of an apparatus according to one or more embodiments. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0024] In the following description, one or more specific details are presented for the purpose of providing a thorough understanding of example embodiments of the present disclosure. The embodiments may be obtained without one or more of the specific details, or may be obtained using other methods, components, materials, etc. Additionally, well-known structures, materials, or operations may not be shown or described in detail to avoid obscuring certain aspects of the embodiments.

[0025] In the context of this description, "one embodiment" or "one embodiment" is intended to indicate that a particular configuration, structure, or feature described in connection with an embodiment is included in at least one embodiment. Thus, the appearance of phrases such as "in one embodiment" or "in one embodiment" in one or more places in this description do not necessarily refer to the same embodiment. Furthermore, particular configurations, structures, or features may be combined in any suitable manner in one or more embodiments.

[0026] In all figures appended hereto, like parts or elements are indicated by like reference numerals, unless the context dictates otherwise, and corresponding descriptions are not repeated herein for the sake of brevity.

[0027] References used herein are provided merely for convenience and therefore do not define the scope or coverage of the embodiments.

[0028] FIG. 1 is an exploded view of an electrochemical cell 1 (or electrochemical reactor) according to one or more embodiments, showing some components of the cell 1.

[0029] The electrochemical cell 1 comprises a photovoltaic system 101 (e.g., a photovoltaic panel) configured to absorb solar energy and convert it into electrical energy (current and voltage available at output terminals 101a, 101b of the system 101) for supplying the electrochemical cell.

[0030] The electrochemical cell 1 comprises gaskets 103, insulating elements 102, sealing elements, and liquid-tight elements configured to electrically insulate certain components (e.g., to electrically insulate the photovoltaic system 101 from the outer walls of the reaction chamber of the electrochemical cell 1) and / or to maintain the liquid-tightness of the reaction chamber and prevent the diffusion of liquids and / or gases into the environment external to the electrochemical cell 1.

[0031] The electrochemical cell 1 comprises a first conductive plate 104a and a second conductive plate 104b, which act as electrodes in contact with the two reaction half-chambers of the electrochemical cell 1, such that when a potential difference is applied between the two conductive plates (one for the anode and the other for the cathode), a chemical reaction can occur in the reactor. For example, as shown in FIG. 1, the conductive plate 104a can be electrically coupled to the positive terminal 101a of the photovoltaic system 101, and the conductive plate 104b can be electrically coupled to the negative terminal 101b of the photovoltaic system 101. Furthermore, each conductive plate 104a, 104b comprises one or more flow channels 105a, 105b for flowing reagents in the corresponding reaction half-chamber (e.g., flow channels in a serpentine configuration). Such flow channels allow for internal distribution of fluids to maximize exchange during the chemical reaction.

[0032] The electrochemical cell 1 comprises a membrane-electrode assembly (MEA) 106, which includes an anion exchange membrane (AEM) 106a or a proton exchange membrane (PEM) 106a, one or two layers of catalytic material (one on the anode side and one on the cathode side), and two gas diffusion layers (GDLs) 106b. In particular, the MEA 106 can be configured according to a CCS (catalyst coated substrate) configuration, where the catalytic material is disposed on a substrate, or according to a CCM (catalyst coated membrane) configuration, where the catalytic material is disposed on a membrane 106a.

[0033] Thus, the conductive plates 104a and 104b can operate directly as electrodes or as conductive elements that supply power to the membrane-electrode assembly 106.

[0034] The electrochemical cell 1 comprises a temporary energy storage (buffer) system 107 , for example a battery, which can be selectively coupled to the photovoltaic system 101 .

[0035] The electrochemical cell 1 comprises one or more pumps 108a, 108b (e.g., micropumps, such as piezoelectric pumps). For example, the cell 1 may comprise a pump 108a that allows for recirculation or flow of the anode and a pump 108b that allows for recirculation or flow of the cathode.

[0036] The electrochemical cell 1 comprises an electronic control unit 109 (e.g., a PLC) configured to manage the operation of the electrochemical cell 1, as will be explained later. For example, the control unit 109 can be configured to regulate the system for recirculation of reagents by operating the pumps 108a, 108b as a function of one or more signals detected by one or more flow sensors (not shown in FIG. 1) installed in the electrochemical cell 1. Additionally or alternatively, the control unit 109 may be configured to regulate the operating point of the electrochemical system (i.e. the pair of current-voltage values ​​j, V applied to the electrodes of the cell 1) by dynamically configuring the photovoltaic system 101. Additionally or alternatively, the control unit 109 may be configured to control the energy storage system 107 so that the electrochemical reactor can operate continuously.

[0037] In one or more embodiments, the pump 180a and pump 108b, the energy storage system 107, and / or the circuitry of the electronic control unit 109 may be integrated within the electrochemical cell 1.

[0038] Also shown in FIG. 1 are gas reservoirs 110a, 110b that are coupled in fluid communication with the two reaction half-chambers (anode and cathode) of cell 1 and configured to collect the respective reaction products.

[0039] Figure 2 is an exploded view of the electrochemical cell 1 described with reference to Figure 1, showing the main flows of liquids and gases, as well as some of the electrical connections between the various components of cell 1. Alternatively, Figure 3 is a simplified view of cell 1, showing in a schematic manner the main flows of liquids and gases, as well as some of the electrical connections between the various components of cell 1.

[0040] As illustrated in Figures 2 and 3, the cell 1 is configured as follows: A liquid supply (anode reagent) is fed into the circuit through inlet hole 201a, which transports the liquid to the cathode side 104a of the electrochemical cell 1 and into the flow channel 105a. When the liquid is introduced into the flow channel 105a and comes into contact with the MEA 106, it reacts with the liquid introduced into the anode flow channel 105b and is partially converted into gaseous reaction products. The mixture containing the partially unconverted reagent and the gaseous products reaches the outlet hole 202a of the plate 105a and passes through the cell 1 to the hole 203a. It then passes through a split valve 204a which separates the gaseous products from the reagents that have not yet been converted, the gaseous products are transported towards the respective storage reservoirs 110a and the reagents that have not yet been converted are reintroduced into the circuit via pump 108a and the conversion cycle begins again. Similarly, on the anode side, the delivery of liquid (anode reagent) is fed into the circuit through hole 201b, which transports the liquid directly through the anode flow channel 105b. When the liquid is introduced into the flow channel 105b and comes into contact with the MEA 106, it reacts with the liquid of the cathode circuit and is partially converted into gaseous products. The mixture containing the partially unconverted reagent and the gaseous products reaches the outlet hole 203b and passes through a split valve 204b which separates the gaseous products from the reagents that have not yet been converted, the gaseous products are transported towards the respective storage reservoirs 110b, and the reagents that have not yet been converted are reintroduced into the circuit via pump 108b to restart the conversion cycle.

[0041] In one or more embodiments, the photovoltaic system 101 is configured to provide the power required for the operation of the electrochemical reactor 1, and the control unit 109 is configured to regulate and distribute said power among the various components of the cell 1. In particular, as further explained below, the photovoltaic system 101 comprises a plurality of photovoltaic cells, the electrical connections of which are (dynamically) reconfigurable in various series / parallel modes to convert the absorbed solar energy into various current-voltage (jV) combinations, and to power the electrochemical cell 1 in the most efficient manner to increase the amount of reaction products (i.e., increase the efficiency of the electrochemical cell). Such (dynamic) reconfiguration of the series / parallel connections of the photovoltaic cells in the photovoltaic system 101 is performed by the control unit 109.

[0042] Specifically, the control unit 109 Adjusting the operating parameters of the electrochemical cell 1 as a function of programmed logic and / or as a function of signals detected by one or more sensors (flow sensors, ammeters, voltmeters, etc.) inside the electrochemical cell 1 and / or as a function of signals received from outside (e.g., from an external interface, from an Internet-of-Things device) by opening and closing electrical and power connections or by adjusting the operation of subcomponents of the electrochemical cell 1; receiving as an external input ideal values ​​for the operating parameters of one or more selected electrochemical reactions, adjusting the system to approach as closely as possible the ideal values ​​for the operating parameters of the selected chemical reactions, and providing feedback to the outside; - adjusting the operation of the recirculation pumps 108a, 108b as a function of the change in flow rate and as a function of the difference between the flow rate at the input to the electrochemical cell 1 and the flow rate at the output from the electrochemical cell 1; Configuring the electrical connections of the photovoltaic system 101 to utilize a portion of the power generated by the photovoltaic system 101 for charging the energy storage system 107, in particular the portion of the power thus utilized being equal to the difference between the power absorbed from solar irradiation and the power that can be converted into a current that is useful for electrochemical reactions (i.e. it can represent the excess energy that cannot be used to immediately activate a chemical reaction); The device may be configured to perform one or more of the following functions:

[0043] In one or more embodiments, the energy storage system 107 can provide electricity to the control unit 109 and / or the pumps 108a, 108b. Additionally or alternatively, the energy storage system 107 can provide minimal current and voltage to the electrochemical cells 1 during periods of inactivity at night, which can increase the speed and efficiency of start-up of the electrochemical cells 1 in the morning (when the photovoltaic system 101 begins converting solar irradiance into electrical energy) and slow degradation of the chemical catalytic components of the cells 1, thereby extending their useful life and increasing the stability of the system.

[0044] Additionally or alternatively, in one or more embodiments, to increase the stability of the chemical reactions occurring in the electrocatalytic system, the energy storage system 107 can compensate for possible oscillations, interruptions, and / or sudden fluctuations in the generation of electrical energy by the photovoltaic system 101.

[0045] One or more embodiments may relate to a system including a plurality of electrochemical cells 1, as described with reference to Figures 1 to 3. The cells 1 may thus constitute a modular unit of a more complex system, which may for example be a panel including a plurality of electrochemical cells, each of which may be associated with a respective photovoltaic panel.

[0046] Figure 4 illustrates such a system 40 with multiple cells 1, according to one or more embodiments, showing the main flows of liquid (thick solid lines and short dashed lines), gas / product flows (dashed lines towards reservoirs 110a', 110b'), and electrical signals (thin solid lines and long dashed lines) regulating the system 40 with multiple electrochemical cells 1 operating synergistically.

[0047] Specifically, in such a system, a reaction product common to all the cells 1 can be present in two reservoirs 110a', 110b'. The system 40 can further include two pumps 408a, 408b powered by an electric motor 420. The first pump 408a can receive a liquid containing an anodic reagent from a corresponding fluid input and convey it towards the corresponding plurality of pumps 108a of each cell 1. Similarly, the second pump 408b can receive a liquid containing a cathodic reagent from a corresponding fluid input and convey it towards the corresponding plurality of pumps 108b of each cell 1. The arrangement of the common pumps 408a, 408b and the dedicated pumps 108a, 108b can improve the control and distribution of the reagents in all the cells.

[0048] Furthermore, the system 40 may include a common electronic control unit 409 (e.g., a PLC) that controls the motors 420 that drive the pumps 408a, 408b. The common electronic control unit 409 may also be connected to each local control unit 109 of each cell 1 to exchange control and / or feedback signals.

[0049] 4, a variable flow intake pump 408a controlled by a common electronic control unit 409 delivers fluids to the various cells 1 on the anode side (and similarly on the cathode side by a variable flow intake pump 408b). Reactions occur within the electrochemical cells 1, and various split valves (provided in the cells 1) separate the gaseous products from the liquid reagents, conveying the former into circuits provided for the anode and cathode products (where they are then collected in the respective reservoirs 110a', 110b') and conveying the latter through the cells 1 again.

[0050] 5 is a diagram illustrating the system 40, in which one of the electrochemical cells 1 contained therein is shown in more detail. The local control units 109 of the cells 1 exchange control and / or feedback signals with a common electronic control unit 409. Fluids received through ducts controlled by pumps 408a, 408b are introduced into the electrochemical cells 1 through their respective inlet holes 201a, 201b, according to the action of local control obtained through the pumps 108a, 108b controlled by the local control unit 109.

[0051] 6 illustrates an alternative embodiment of the system 40, showing a different connection between the local fluid ducts of cell 1 and the common fluid duct controlled by pumps 408a, 408. Specifically, in this configuration, the liquid is introduced into the local recirculation system in the intermediate part of the duct between the split valve and the pumps, i.e., upstream of the pumps 108a, 108b. Obviously, a person skilled in the art will understand that many alternative configurations are possible that achieve the same functions as those described herein, all of which are within the scope of the present invention.

[0052] FIG. 7A is an exemplary front view of the back side of a conductive plate (e.g., an anode side conductive plate or a cathode side conductive plate) for use in an electrochemical cell according to one or more embodiments. FIG. 7B is an axonometric view of the same back side as shown in FIG. 7A. FIG. 7C is an exemplary front view of the front side of the conductive plate of FIGS. 7A and 7B (i.e., the conductive plate surface facing the inside of the reaction chamber). FIG. 7D is an axonometric view of the same front side as shown in FIG. 7C. FIG. 7E shows an enlarged portion of the conductive plate of FIG. 7D.

[0053] 7A to 7E show in detail an example of the structure of the flow channels 105a, 105b provided on the sides of the conductive plates 104a, 104b facing the reaction chamber. A water-based reagent flow from an inlet reaches the conductive plate from the front side (shown in Figs. 7C-7E) and passes through the plate from point 701 (at the front) to point 702 (at the rear). The flow goes down through mini-channels 702a to point 703 and passes through the conductive plate again from point 703 (at the rear) to point 704 (at the front). From point 704, the liquid filled with reagent (e.g., anodic reagent) flows through the flow channels (105a, 105b) where it is separated by an ion exchange membrane and comes into contact with a countercurrent flow (e.g., cathodic flow) flowing in a second conductive plate and is converted to products. In one or more embodiments illustrated herein, the flow paths diverge at point 704a and merge at point 705a to increase the exchange area while decreasing the velocity of the constant flow rate of fluid. Finally, the combined stream of gaseous products and liquid reagents reaches point 706. From here, the stream passes again through the conductive plate and through point 707 at the rear to the main duct (point 708 at the rear, then through the conductive plate again to point 709 at the front). From the main duct, the stream reaches the respective split valves, which allow the liquid portion of the stream (unconverted reagent) to circulate again through the reaction chamber and collect the gaseous portion of the stream in the respective reservoir.

[0054] In FIG. 7E, the structure of the flow channel is highlighted, which may have a structure similar to a capillary tube with a semicircular cross-section that is closed at the front by MEA 106 (not visible in FIGS. 7A-7E).

[0055] 7F is a cross-sectional (side) view of the interior of an electrochemical cell 1 according to one or more embodiments. As described with reference to FIG. 1, the cell 1 comprises two conductive plates 104a, 104b, each of which has a flow channel 105a, 105b for reagents to flow (e.g., in a serpentine manner) that are inscribed in corresponding locations on opposing surfaces of the conductive plates 104a, 104b. This allows two liquids (anode liquid and cathode liquid) to flow to corresponding locations on two opposing sides of the MEA 106, allowing chemical exchange to occur across the membrane. The liquid containing the reagents for the cathode half reaction flows through the cathode flow channel 105a, and the liquid containing the reagents for the anode half reaction flows through the anode flow channel 105b. When a potential difference is applied across the conductive plates 104a, 104b, an electrochemical reaction is stimulated by a catalyst contained in the MEA 106, closing an electrical circuit and producing gaseous products, which are transported along with the unconverted reagents through a flow path to a split valve where the gaseous products are separated from the unconverted reagents, allowing the latter to return to circulation.

[0056] Figure 7G is a further exemplary front view of the conductive plate of Figures 7A-7E (i.e., the side of the conductive plate facing the inside of the reaction chamber). Figure 7H is a cross-sectional view of the conductive plate shown in Figure 7G taken along line VII-VII of Figure 7G. The left portion of Figure 7H shows an enlarged view of the cross-sectional view, highlighting the semicircular structure of the flow channel 105 on the front surface of the conductive plate 104.

[0057] Thus, one or more embodiments may comprise an independent fluid dynamic system for recirculation, collection and / or separation of the (gaseous) product. In particular, one or more embodiments may comprise a system for distribution and microfluidic recirculation that allows an increase in the surface of the electrodes in contact with the reagents and a reduction in head loss. For example, one or more embodiments feature a structure that facilitates the separation of the gaseous part (product) from the liquid part (reagents). The fluid dynamic system has the function of distributing the reagents (in liquid form) at both the anode and cathode inputs and of maximizing the contact surface between the liquids and the surfaces of the electrodes and ion exchange membranes (e.g. proton exchange membranes - PEMs or anion exchange membranes - AEMs), allowing the system to operate with continuous flow.

[0058] Furthermore, one or more embodiments may comprise one or more sensors for adjusting the fluid dynamic and recirculation system. The circulation and / or recirculation of reagents and products in a microfluidic system may be obtained by pressure fluctuations and may be controlled by a system including one or more sensors monitoring the operating parameters of the reactor. In particular, a system for managing flows according to various embodiments comprises a first system for managing flows in individual electrochemical cells and a second system for managing flows in a system composed of multiple interconnected cells, as illustrated above in Figures 4 to 6.

[0059] In one or more embodiments, the system for managing the flows in a system composed of a number of electrochemical cells is configured to convey the output flows of the cells in a single duct and to feed the individual input ducts of the reagents of the individual electrochemical cells, starting from a single main duct of the reagents. For example, the flow management system may comprise check valves and pressure switches that can be adjusted as a function of the working point selected based on the chemical reactions occurring in the individual electrochemical cells. For example, one or more embodiments may comprise a control unit (e.g., a microprocessor, etc.) configured to adjust and manage the working points of the electrochemical cells both in an automatic manner (e.g., according to pre-set regulations and parameters) and in a parametric or manual manner (e.g., by inputting the required operating parameters via a user interface). This solution increases the flexibility of use of the electrochemical system, allowing the update and / or modification of the working parameters depending on the reactions carried out in the electrochemical cells and / or in response to changes in the catalytic system used, without the need to make structural modifications to the electrochemical cells.

[0060] Figure 8A is an exploded view of several components of an electrochemical cell 1 according to various embodiments, Figure 8B is a corresponding exploded rear view of a preferred embodiment, and Figure 8C is an exploded front view of the electrochemical cell shown in Figure 8B.

[0061] In particular, Fig. 8A shows a photovoltaic panel 101 and two conductive plates 104a, 104b. Fig. 8A also shows a schematic representation of area 101S, i.e. the area of ​​the surface of the photovoltaic panel 101 (divided into six areas in this example, as the photovoltaic panel 101 can contain multiple photovoltaic cells that can be connected in series and / or in parallel as required). Fig. 8A also shows a schematic representation of area 106S, i.e. the active area of ​​the surface of the electrode of cell 1. The area of ​​the electrode considered as active is the area of ​​ion exchange between the first and second reaction half-chambers and is therefore common to the two electrodes.

[0062] 8B and 8C are exploded views of an electrochemical cell 17 according to one or more embodiments of the present invention. The electrochemical cell 17 is particularly suitable for functioning in a PV-EC configuration where the photovoltaic element is not immersed in the reaction chamber, but is outside the chamber itself. The electrochemical cell 17 comprises a first frame element 170A, which preferably comprises a plate made of a plastic material. As illustrated in FIGS. 8B and 8C, the shape of the frame element 170A is preferably hexagonal, but may also be square or rectangular, as in other embodiments described herein.

[0063] The plate comprises on one of its faces (i.e. the "inner" face of the electrochemical cell) a recess (preferably of square or rectangular shape) that defines the volume of a first reaction half-chamber. The recess is in fluid communication with the external environment by ducts 171A, 172A, 173A, 174A passing through the frame element 170A. The recess is configured to receive therein a tesserae (tiled) element 176A (corresponding to the conductive plate 104b in FIG. 8A) that defines the first reaction half-chamber and acts as a charge collector for the first half-chamber.

[0064] The electrochemical cell 17 further comprises an ion exchange membrane 1700, which separates a first reaction half-chamber defined by the tesserae-like element 176A from a second reaction half-chamber defined by a similar second tesserae-like element 176B (corresponding to the conductive plate 104a in FIG. 8A) received in a recess in the second frame element 170B. As illustrated in FIGS. 8B and 8C, the second frame element may not be provided with ducts for fluid communication between the recess and the external environment. The frame element and the ion exchange membrane may comprise perimetral holes (not visible in the attached drawings) for assembling the electrochemical cell 17.

[0065] In one or more embodiments, the electrochemical cell 17 comprises a photovoltaic cell 178 (corresponding to the photovoltaic element 101 of FIG. 8A) electrically coupled to the electrodes.

[0066] The electrochemical cell 17 is configured to operate in a continuous-flow mode using a photovoltaic system 178, an electrical system, a catalytic system, and a system for managing the flows and collecting the products (e.g., gaseous products such as hydrogen) as previously described. In particular, the electrochemical cell 17 can include a continuous-flow system and a recirculation system, a system for light absorption and conversion, and a configuration that minimizes losses and maximizes system synergies and versatility.

[0067] Specifically, as illustrated in Figures 8B and 8C, the charge collectors 176A, 176B of the electrochemical cell 17 comprise one or more etched channels with a serpentine configuration that distribute the flow over the active surfaces of the electrodes and membrane 1700, maximizing the exchange area and contact time if the flow rates through the cell are the same, thereby improving the amount of reagents converted to products under the same flow rate. In one or more embodiments, the anode channel system is placed above the cathode channel and configured with the two flows in countercurrent to maximize proton / anion exchange and increase conversion rates.

[0068] As previously discussed, in one or more embodiments, pump 180a and pump 108b, energy storage system 107, and / or circuitry of electronic control unit 109 may be integrated within electrochemical cell 1. For example, with reference to Figures 8B and 8C, one or more of the above-referenced systems may be integrated within frame element 170A and / or frame element 170B.

[0069] It should be noted that to integrate photovoltaic and electrolysis technologies (or electrochemical or EC systems) in a single system, it is necessary to supply the electrochemical system with the maximum possible charge density at the potential required by the selected catalytic system. In known solutions, for this purpose, large photovoltaic surfaces are used to power one electrolyser (and therefore one set of electrodes). As a result, the ratio between the photovoltaic surface and the active surface of the electrodes is usually much higher than 100, even by one or several orders of magnitude. Obtaining a low ratio between the photovoltaic surface and the active surface of the electrodes (ratios of the order of a few tens to one) is a desirable property that cannot be achieved with the solutions according to the prior art. In fact, for each square meter of a photovoltaic panel, it is economically disadvantageous to provide the same number of electrodes as electrolysers. Moreover, the very large surface areas (e.g. 1 m 2 ) are placed on electrodes with the same surface area (e.g., 1 m 2 When connected to a photovoltaic panel of a solar cell, ohmic losses and voltage drops occur, which may be so significant that the operating conditions of the electrolysis system cannot be guaranteed, or in any case may jeopardize its efficiency, making the system economically unsustainable.

[0070] In one or more embodiments, the ratio of photovoltaic surface to active surface of the electrodes is kept as low as possible (e.g., 100 or less, 50 or less, 10 or less, 5 or less, or 1 or less going from a lumped to an extended configuration) while still maintaining the conditions necessary for the operation of the catalytic system (e.g., at least 8 mA / cm 2 To maintain a current density of at least 1.5 V and a potential difference of at least 1.5 V, the photovoltaic panel is divided into a number of units (e.g., each unit is 25 cm 2 1m from 2 between 50cm, selectively 2 From 25dm 2 between 100cm and 100cm 2 Each of these units can be electrically coupled directly to an electrode having a surface corresponding to the surface of the photovoltaic unit (e.g., 25 cm 2 1m from 2Optionally, 50cm between 2 From 25dm 2 Between, optional 100cm 2 is equal to).

[0071] According to the above solution, the system 40 according to one or more embodiments comprises a number of small photovoltaic panels connected to an equal number of small electrochemical cells, the electrochemical cells having electrodes of dimensions corresponding to the electrodes of the respective photovoltaic panels that supply power thereto.

[0072] One or more embodiments comprise a system for the regulation and management of the (integrated) photovoltaic system, which is designed to reduce ohmic losses and increase the surface charge density required for the reaction by adjusting the operating voltage. For example, the connection of the individual photovoltaic units can be configured to be connected in series, parallel or a combination of the two, which allows the operating curve of the photovoltaic system to be adjusted to suit the specific electrochemical reaction occurring in the reactor and also to the catalyst system used, and thus improves the efficiency of the photovoltaic electrochemical system. The reactor according to one or more embodiments can comprise a catalyst system selected based on the given reaction to be obtained with the desired product (e.g. hydrogen or syngas). Each reaction and / or each catalyst system may require a different minimum operating voltage. The ability to set up the connection between the individual photovoltaic units in series and / or parallel allows the modification of the operating voltage applied to the membrane-electrode assembly (MEA), which can improve the electrochemical performance of the system when the selected catalyst system is changed. For example, for the reaction of splitting water to produce hydrogen to take place, a minimum voltage equal to 1.23 V must be applied to the cell. However, the particular catalytic system selected has a maximum efficiency at a voltage of 1.7 V. In this case, in one or more embodiments, the individual photovoltaic units can be connected in a series and / or parallel configuration such that the electrodes are supplied with the maximum current density possible at a minimum voltage of 1.7 V.

[0073] Thus, one or more embodiments may advantageously provide a system for conditioning, managing, and / or connecting a photovoltaic system to the electrodes of a cell (specifically, to an MEA), which may increase versatility of use of the cell itself.

[0074] For example, FIG. 9 illustrates a typical current-voltage (JV) curve of an electrochemical reaction (EC). The dashed line in FIG. 10 indicates the theoretical potential Vth of the reaction. The closer the reaction curve is to the theoretical reaction curve (dashed line) (e.g., the more it shifts to the left), the higher the efficiency of the electrochemical system and the lower the overvoltage losses. FIG. 10 illustrates a typical current-voltage (JV) curve of a photovoltaic system (PV). The highest efficiency point of the photovoltaic system is highlighted in the dashed area of ​​the graph in FIG. 10 and corresponds to a pair of values ​​(Je, Ve) corresponding to the elbow of the curve. The working point (WP) of the photovoltaic-photoelectrochemical system, which determines the efficiency of the electrochemical cell and its power output rate, is determined by the intersection of the reaction (EC) curve and the photovoltaic (PV) curve of the cell, and the working point is determined by a pair of values ​​of current-voltage (JV) as shown in FIG. 11. wp ,V wp ) Assuming the same reaction (EC) curve, the higher the current delivered by the photovoltaic system, the higher the output of the electrochemical reactor (in terms of the amount of reaction product obtained per unit time).

[0075] FIG. 12 shows how different configurations of the electrical (series / parallel) connections between the various photovoltaic cells contained in the photovoltaic system 101 can modify the JV characteristic curve of the photovoltaic system and thus the working point WP of the electrochemical reactor 1. For example, when connecting a number of photovoltaic cells in parallel, a JV curve is obtained in which the current (J) is equal to the sum of the characteristic currents of the individual cells and the voltage (V) is equal to the voltage of only one cell, as shown by the curve PAR in FIG. 12. When connecting a number of photovoltaic cells in series, a JV curve is obtained in which the voltage (V) is equal to the sum of the characteristic voltages of the individual cells and the current (J) is equal to the current of only one cell, as shown by the curve SER in FIG. 12. The photovoltaic system 101 allows a dynamic configuration of the series and parallel connections between the various photovoltaic cells to optimize the working point (WP) of the PV-EC system, operating the EC system with the maximum possible current of absorbed sunlight and operating the photovoltaic system as close as possible to the elbow of the photovoltaic curve. For example, in FIG. 12, the parallel configuration corresponding to the application point WP2 is more efficient than the series configuration corresponding to the application point WP1.

[0076] Furthermore, since the power provided by the sun and therefore absorbed by the photovoltaic system 101 is not constant over the course of the day or throughout the year, the power may be adjusted according to pre-set logic managed, for example, by the electronic control units 109 of the individual electrochemical cells 1 and / or by the electronic control unit 409 of the system 40, to increase the efficiency of the system and ensure a minimum voltage required for the EC reaction to occur. By dynamically changing the series / parallel connections inside the photovoltaic system 101, it is possible to change the operating point of the system.

[0077] For example, Figures 13A, 13B, 14A and 14B show a comparison between two different configurations of the same electrochemical cell 1, where the photovoltaic system 101 comprises, by way of example only, six photovoltaic cells. In Figures 13A and 13B, the six cells are connected in two sets connected in parallel, each set containing three cells connected in series. In Figures 14A and 14B, the six cells are connected in three sets connected in parallel, each set containing two cells connected in series. Assuming the same EC reaction curve in both cases, the configuration of Figures 14A and 14B determines the operating point at a higher current, so that the electrochemical cell 1 achieves high product production and the photovoltaic system operates closer to the elbow of the PV curve and has high efficiency.

[0078] 15 is a diagram illustrating one or more embodiments of an electrochemical cell 1 in which a photovoltaic system 101 includes a series of electronic switches controlled by a control unit 109 to dynamically change the series and parallel connections of the individual photovoltaic cells included in the photovoltaic system 101. Specifically, each photovoltaic cell 150 in the photovoltaic system 101 is an electronic switch S+ that can be actuated to connect the positive terminal of cell 150 to the positive terminal of electrochemical cell 1 (anode 105a); an electronic switch S- that can be actuated to connect the negative terminal of cell 150 to the negative terminal of electrochemical cell 1 (cathode 105b); an electronic switch SS that can be actuated to connect the negative terminal of a cell 150 to the positive terminal of a next cell 150; an electronic switch SP that can be actuated to connect the negative terminal of a cell 150 to the negative terminal of a next cell 150; Equipped with.

[0079] As previously mentioned, one or more embodiments include an energy storage system 107. As illustrated in Figures 16A and 16B, by varying the electrical series / parallel connections within the photovoltaic system 101, when the PV-EC system cannot be operated at the elbow of the photovoltaic curve, the excess voltage can be used to charge the buffer system 107. The buffer system 107 can then be selectively coupled to the output of the photovoltaic system 101 (e.g., via one or more corresponding electronic switches).

[0080] FIG. 17 shows an example of a device 40 that includes multiple electrochemical cells 17 assembled in a checkerboard or hexagonal mosaic configuration.

[0081] Thus, one or more embodiments of the present invention include: the possibility of directly utilizing solar energy to produce hydrogen by electrolysis of water, without the need for intermediate buffers (e.g. batteries for storing electrical energy) or intensive systems (e.g. electrolysers); The possibility of generating green hydrogen on a large scale and in-situ (if required) using a combination (e.g., integration) of photovoltaic and catalytic systems via stand-alone devices; The possibility of combining the hydrogen-producing water splitting reaction with other reactions in the same reactor, such as reactions that allow the valorization of carbon dioxide emissions and the recycling and reuse of carbon dioxide; To improve the flexibility and ease of installation and use of electrochemical reactors compared to known reactors; The present invention may provide one or more of the following advantages:

[0082] Thus, one or more embodiments may provide a solution to two major problems in the energy sector: The problem of intermittent solar radiation is solved by a form of (chemical) energy storage that is very compact (e.g. up to 200 times more compact) and stable in time compared to lithium-ion batteries, through the production of green hydrogen. The problem of CO2 emissions is solved by valorization of CO2 emissions in usable products.

[0083] One or more embodiments indeed allow the recycling of CO2 emissions and the production of green hydrogen and / or other by-products (e.g. glycolic acid) through the direct and in-situ use of a renewable energy source (solar energy). This is made possible by integrating a solar absorption system (PV system) and an electrochemical system (EC system) in one system. This solution offers flexibility of use, ease of installation and use, and also allows the coupling of the water splitting reaction (for hydrogen production) with other reactions, for example reactions to utilize the emissions of carbon dioxide and glycerol (biogas waste), allowing the recycling or reuse of these products.

[0084] At several points herein, the possibility of using the electrochemical cell according to the invention for producing hydrogen by electrolysis of water has been described, but optionally also for CO2 reduction reactions (e.g. with the production of synthesis gas). One or more embodiments may provide an electrochemical reactor that is suitable for carrying out various types of reduction-oxidation reactions in a continuous and stable manner, activated only by the solar energy collected by the cell itself, and that is suitable for use in industrial production.

[0085] Without losing the underlying principles, details and embodiments may vary considerably from those described herein purely by way of example, without departing from the scope of protection.

[0086] The scope of protection is defined by the accompanying claims.

Claims

1. An electrochemical cell (1), comprising: a first reaction chamber comprising a first electrode (104a); a second reaction chamber comprising a second electrode (104b); a membrane-electrode assembly (106) disposed between the first reaction chamber and the second reaction chamber and including an ion exchange membrane (106a); a photovoltaic system (101) that absorbs solar energy and generates an output voltage between a first output terminal (101a) and a second output terminal (101b) of the photovoltaic system (101), the first output terminal (101a) of the photovoltaic system (101) being selectively coupleable to the first electrode (104a) and the second output terminal (101b) of the photovoltaic system (101) being selectively coupleable to the second electrode (104b), and a ratio of a light-sensitive area of ​​the photovoltaic system (101) to an active area of ​​the first electrode (104a) and the second electrode (104b) being less than or equal to 50; Equipped with The photovoltaic system (101) comprises a plurality of photovoltaic cells (150), the plurality of photovoltaic cells (150) being selectively coupleable (S+, S-, SP, SS) between the first output terminal (101a) and the second output terminal (101b) of the photovoltaic system (101) in a configuration including series, parallel, or one or more mixed series / parallel configurations; the electrochemical cell (1) comprises an electronic control unit (109) configured to couple the plurality of photovoltaic cells (150) in a selected one of said configurations as a function of one or more user-settable parameters and / or as a function of one or more signals received from an external control unit and / or as a function of one or more signals received from one or more sensors included in the electrochemical cell (1), Electrochemical cell (1).

2. The one or more sensors included in the electrochemical cell (1) a current sensor configured to sense a current flowing through the first electrode (104a) and the second electrode (104b); a voltage sensor configured to sense a voltage applied between the first electrode (104a) and the second electrode (104b); At least one of: Electrochemical cell (1) according to claim 1.

3. the ratio between the photosensitive area of ​​the photovoltaic system (101) and the active area of ​​the first electrode (104a) and the second electrode (104b) is less than or equal to 10, preferably less than or equal to 5, and more preferably equal to 1; Electrochemical cell (1) according to claim 1.

4. The photosensitive area of ​​the photovoltaic system (101), the active area of ​​the first electrode (104a), and the active area of ​​the second electrode (104b) are 25 cm ２ 1m from ２ Preferably within 50 cm ２ From 25dm ２ More preferably, it is within the range of 100 cm ２ is equal to Electrochemical cell (1) according to claim 1.

5. the first electrode (104a) comprises a first conductive plate, the first reaction chamber being comprised of at least one flow channel (105a) inscribed in a surface of the first conductive plate facing the ion exchange membrane (106a); the second electrode (104b) comprises a second conductive plate, and the second reaction chamber is formed with at least one flow channel (105b) engraved on a surface of the second conductive plate facing the ion exchange membrane (106a) at a position corresponding to the flow channel (105a) engraved on the first conductive plate; A first reaction fluid introduced into the first reaction chamber and a second reaction fluid introduced into the second reaction chamber flow at corresponding positions on two opposite sides of the ion exchange membrane (106a); Electrochemical cell (1) according to claim 1.

6. a first gas diffusion layer (106a) disposed between the first electrode (104a) and the ion exchange membrane (106a); a second gas diffusion layer (106b) disposed between the second electrode (104b) and the ion exchange membrane (106a); Equipped with Electrochemical cell (1) according to claim 1.

7. an electrical energy storage device (107); The electronic control unit (109) and / or coupling the electrical energy storage device (107) to the photovoltaic system (101) to store excess electrical energy generated by the photovoltaic system (101) in response to the photovoltaic system (101) providing an output voltage above a first voltage threshold. and / or coupling the electrical energy storage device (107) to the first electrode (104a) and the second electrode (104b) to supply electrical energy stored in the electrical energy storage device (107) to the first electrode (104a) and the second electrode (104b) in response to the photovoltaic system (101) providing an output voltage lower than a second voltage threshold. coupling the electrical energy storage device (107) to the first electrode (104a) and the second electrode (104b) to provide a minimum supply voltage to the first electrode (104a) and the second electrode (104b) during inactive phases of the photovoltaic system (101); and / or and / or coupling the electrical energy storage device (107) to the first electrode (104a) and the second electrode (104b) to supply electrical energy stored in the electrical energy storage device (107) to the first electrode (104a) and the second electrode (104b) in response to an output voltage of the photovoltaic system (101) being subjected to an oscillation, interruption, and / or sudden change. connecting said electrical energy storage device (107) to said electronic control unit (109) to provide power to said electronic control unit (109); 4. The method of claim 3, Electrochemical cell (1) according to claim 1.

8. a first pump (108a) controlled by said electronic control unit (109) to regulate the flow of a first reaction fluid introduced into said first reaction chamber; a second pump (108b) controlled by the electronic control unit (109) to regulate the flow of a second reaction fluid introduced into the second reaction chamber; Equipped with Electrochemical cell (1) according to claim 1.

9. one or more pressure sensors and / or one or more flow rate sensors for detecting one or more parameters indicative of the flows of the first and second reactant fluids; the electronic control unit (109) is configured to control the first pump (108a) and the second pump (108b) to regulate the recirculation and introduction of the reaction fluid as a function of the parameter indicative of the detected flow. Electrochemical cell (1) according to claim 8.

10. a first split valve (204a) located in an outlet duct from said first reaction chamber; a second split valve (204b) located in an outlet duct from said second reaction chamber; Equipped with the first split valve (204a) is configured to separate a first gaseous reaction product from a first reaction fluid introduced into the first reaction chamber, convey the first gaseous reaction product toward a first storage reservoir (110a), and reintroduce the first reaction fluid into the first reaction chamber; the second split valve (204b) is configured to separate a second gaseous reaction product from a second reaction fluid introduced into the second reaction chamber, convey the second gaseous reaction product toward a second storage reservoir (110b), and reintroduce the second reaction fluid into the second reaction chamber. Electrochemical cell (1) according to claim 1.

11. A plurality of electrochemical cells (1) according to claim 1; a first storage reservoir (110a) in fluid communication with the first reaction chamber of the electrochemical cell (1) for receiving a first gaseous reaction product; a second storage reservoir (110b) in fluid communication with the second reaction chamber of the electrochemical cell (1) for receiving a second gaseous reaction product; An apparatus electronic control unit (409); a first distribution circuit for a first reaction fluid in fluid communication with the first reaction chamber of the electrochemical cell (1), the first distribution circuit including a first device pump (408a); a second distribution circuit for a second reaction fluid in fluid communication with the second reaction chamber of the electrochemical cell (1), the second distribution circuit including a second device pump (408b); Equipped with the apparatus electronic control unit (409) is configured to control the first apparatus pump (408a) to regulate the flow of the first reactant fluid introduced into the first distribution circuit and to control the second apparatus pump (408b) to regulate the flow of the second reactant fluid introduced into the second distribution circuit; Apparatus (40).

12. the device electronic control unit (409) is configured to exchange control and / or feedback signals with the electronic control unit (109) of the electrochemical cell (1); 12. The apparatus (40) of claim 11.

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