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    • 专利摘要:
    The invention relates to a novel method of operating a Soec stack reactor ("solid oxide electrolyzer cell") according to which, in the absence of electricity, H2 + CO or an H2 + CO2 mixture is injected into the reactor. cathode inlet of the reactor so as to produce methane within the reactor itself. The catalytic methanation reaction being exothermic, the stack reactor can therefore be maintained in temperature, without loss of fuel. The fuel used for the methanation (synthesis gas or hydrogen) can advantageously be that produced beforehand during the operating phases with available electricity.
    公开号:FR3014117A1
    申请号:FR1362024
    申请日:2013-12-03
    公开日:2015-06-05
    发明作者:Magali Reytier；Marie Petitjean；Guilhem Roux
    申请人:Commissariat a lEnergie Atomique CEA；Commissariat a lEnergie Atomique et aux Energies Alternatives CEA；
    IPC主号:
    专利说明:

    [0001] PRO DEPENDS ON -ONCTIO EMILINT OF A TYPE STACKED RU RU. The present invention relates to the production of methane by heterogeneous catalysis. TECHNICAL FIELD The present invention relates to the production of methane by heterogeneous catalysis. The production method according to the invention comprises beforehand a step of electrolysis of high temperature water (EUT, or EVHT for electrolysis of water vapor at high temperature, or HTE acronym for "High Temperature Electrolysis" , or HTSE for High Temperature Steam Electrolysis) or a so-called co-electrolysis step of water and carbon dioxide CO2 at high temperature, in a cell type electrolysis stack reactor. SOEC (acronym for "Solid Oxide Electrolyzer Cell") that is supplied with electricity.
    [0002] The invention relates more particularly to the production of methane from the same reactor in the absence of available electricity. Previous art Among the massive energy storage solutions already envisaged, hydraulic storage is already widespread. The remaining capacity of this type of storage may be quickly saturated. In addition, hydraulic systems require particular geographical and geological conditions and can therefore be quite expensive. For storage problems at. hydraulic storage can only be a partial solution. An alternative storage solution has also been considered: compressed air storage (CAES). According to this technology, it is planned to store compressed air produced with electricity in subterranean cavities. These also require specific geological characteristics, such as salt cavities. However, the yield of this solkk! storage is not satisfactory.
    [0003] Finally, hydrogen is announced as a vector of energy that can massively store electricity in certain configurations: here we can cite the project already carried out in Corsica under the acronym MYRTE (acronym for Renewable Hydrogen Mission for Integration into Electrical Network) on the initiative of the plaintiff. However, all these massive energy storage solutions require significant infrastructure to develop (clean sites for hydraulics, sub-ground cavities, hydrogen storage systems). This is why, more recently, the massive energy storage by conversion of renewable electricity into energy that through the production of synthetic fuel has made a significant breakthrough, representing a high potential storage alternative. One can quote here the patent application US 2009/0289227 which evokes technical solutions of conversion. 10 In addition, reduce CO2 carbon dioxide emissions resulting from the use of fossil fuels, use as much CO2 as possible from the use of these energies instead of storing it indefinitely, use on demand electricity from so-called carbon-free energy sources, especially during periods of overproduction, converting this electricity into a storable product that can possibly produce electricity on demand during periods of production deficits without having to resort to highly carbonaceous energies are as many objectives to be achieved in the interest of overall efficiency. The manufacture of a synthetic fuel gas from a mixture of water vapor and carbon dioxide CO2, thanks to so-called carbon-free electricity, meets these objectives. The electrolysis of H20 water vapor to produce hydrogen H 2 and / or the co-electrolysis of H 2 O + CO2 at high temperature in a solid oxide electrolyzer is one of the possibilities. The electrolysis reactions of the water vapor () and of the coelectrolysis of H2O + CO2 (11) are carried out according to the following equations: Electrolysis of water: H2O - * H2 + 1/202 (1) Co- electrolysis: CO2 + H20 - CO + H2 + O2 Thus, the electrolysis of the water vapor 1120 allows a so-called direct manufacture of the fuel gas by heterogeneous catalysis by injection of a mixture of hydrogen H2 produced by the electrolysis ( I) and CO2 carbon dioxide on a catalyst. The co-electrolysis of H2O + CO2 allows so-called indirect manufacture of the fuel gas at p. r synthesis gas (H2 + CO) produced according to the co-electrolysis The fuel gas thus manufactured may be a hydrocarbon and especially methane, the main component of natural gas. The production of synthetic natural gas gives the possibility to immediately use all the existing infrastructures developed for this energy: transmission and distribution networks, storage capacities, electricity production systems, etc. In addition, it is clear also that the carbon footprint of this production could be zero or even negative, since the electricity used would be of decarbonated origin and that the CO2 would come from systems using fossil fuels that one would have: previously captured.
    [0004] To carry out the electrolysis of the water (1), it is advantageous to carry it out at high temperature, typically between 600 and 950 ° C., since part of the energy required for the reaction can be provided by the heat which is less expensive that electricity and activation of the reaction is more efficient at high temperature and does not require catalyst. To implement high temperature electrolysis, it is known to use a SOEC type electrolyser (acronym for "Solid Oxide Electrolyzer Cell"), consisting of a stack of elementary patterns each comprising an electrolysis cell. solid oxides, consisting of three layers of anode / electrolyte / cathode superimposed on each other, and interconnect plates of metal alloys also called bipolar plates, or interconnectors. The function of the interconnectors is to ensure both the passage of electric current and the circulation of gases in the vicinity of each cell (injected water vapor, hydrogen and oxygen extracted in an EHT electrolyser, injected air and hydrogen and water extracted in a SOFC stack) and separate the anode and cathode compartments that are comp. - Flow of gas flow on the side respectively of the anodes and the cathodes of the cells. To carry out the electrolysis of water vapor at high temperature EHT, water vapor 1120 is injected into the cathode compartment. Under the effect of the current applied to the cell, the dissociation of water molecules in vapor form is carried out at the interface between the hydrogen electrode (cathode) and the electrolyte: this dissociation produces dihydrogen gas 112 and oxygen ions. The hydrogen is collected and discharged at the outlet of the hydrogen compartment.
    [0005] O2-Oxygen ions migrate through the electrolyte and recombine in oxygen at the interface between the electrolyte and the oxygen electrode (anode).
    [0006] The co-electrolysis of water vapor and CO2 (II) potentially offers the same energy and economic advantages as those described above for the electrolysis of water vapor (reaction (I)). Its interest lies in the possibility of carrying out the reaction of co-electrolysis (II) in the same reactor by maintaining it in a temperature range of about 800 ° C. Indeed, at this temperature, the voltages required for the reduction of CO2 in CO and H2O in 112 are almost identical. By way of example, the voltages at abandonment, that is to say the electrical voltages obtained without electric current but only e: ce the different gases on either side of a cell, for a mixture of 90% of oxidized species and 10% of reduced species at 800 ° C are respectively equal to 0.852V for the pairs 1120, H2 / 02 and 0.844V for the couples CO2, C0 / 02. In addition, the high temperature co-electrolysis has the same energy interest as the electrolysis of water vapor between 750 and 900 ° C compared to the electrolysis of water at low temperature. Indeed, the energy necessary for the dissociation of the molecules 1120 is reduced by the vaporization energy. Moreover, the kinetics of the electrolysis reactions of H20 and CO2 are strongly thermally activated and follow an Arrhenius law with activation energies of the order of 120 kj / mol. As a result, the effectiveness of the reactions increases greatly as the temperature is increased. The higher electrochemical activity at high temperature also makes it possible to add expensive catalyst such as platinum at lower temperatures. In addition, the production of synthesis gas in the cathode compartment of the co-electrolysis reactor is accompanied by an oxygen production in the anode compartment that can be upgraded subsequently, for example 2to. the oxycombustion of natural gas. However, if the high-temperature co-electrolysis (II) as envisaged offers the aforementioned advantages that are the investment of a single electrolysis reactor, the thermal coupling between the various reactions, it has the drawback of do not allow to obtain variable H2 / CO ratio in the mixing gas at the outlet of the reactor. In other words, when the co-electrolysis is carried out, a desired H2 / CO ratio at the output 30 imposes an input ratio 11201CO2. Indeed, operation close to the thermo-neutral operating point sets the voltage to be applied to the electrolyzer. Thus, for a desired ratio of H2 / CO output with a water conversion rate close to 100%, flow rates and input compositions in CO2 and H2O must necessarily be determined. However, each synthesis gas intended to produce a fuel gas requires a given H2 / CO ratio depending on the target fuel. Similarly, the direct manufacture of the fuel gas requires a given CO2 / F12 ratio depending on the target fuel. Table 1 below illustrates the ratios required depending on the synthesis processes of different fuels: T LEAU 1 PRODUCT PROCESS TIO H2 / CO NECESS RATIO SYNTHESIS CO I: USTIBLE CO2 / H2 OBTAINED NECESSARY synthesis of methane Natural gas 1 / 3 1/4 synthesis of methanol 1/2 1/3 methanol synthesis of dimethyl ether (D DME 1/1 1/2 synthesis Ficher Diesel 1/2 1/3 Tropsch The applicant proposed in the patent application filed December 10 17 2012 under the number FR 12 62174 a new process and coelectrolysis reactor to obtain at output a variable ratio H2 / CO and thus a synthesis gas whose composition is adapted to produce the desired fuel gas. The operation retained for an electrolysis or co-electrolysis reactor also fixes the thermal conditions in the electrolysis reactor: in fact, for the electrolyses carried out at high temperature, the energy AH required for Dissociation of the input molecule (H 2 O or CO 2) can be provided in electrical form and / or heat. The thermal energy delivered Q is then defined as a function of the voltage U at the terminals of each electrolysis cell by the relation: 2F in which U is the electrical voltage, I is the electric current and F is the Faraday constant. Thus, three operating regimes corresponding to three different thermal modes for the stacking of electrolysis cells are defined: the so-called autothermal mode in which the imposed voltage Uimp is equal to 4H / 2F. The heat consumed by the dissociation reaction is completely compensated by the different electrical resistances of the electrolyser (irreversibilities). The electrolysis reactor (electrolyser) does not need any particular thermal management while remaining stable in temperature. the so-called endothermic mode in which the imposed voltage Uimp is lower than AH / 2F. The electrolyser consumes more heat than the electrical losses within it. This necessary heat must then be provided by another means, otherwise its temperature will drop irretrievably. the so-called exothermic mode in which the imposed voltage Uimp is greater than AH / 2F. Electrolysis then consumes less heat than electric losses by Joule effect. This release of heat within the electrolyser must then be evacuated by another means, under penalty of seeing its temperature to you enter unacceptably. The endothermic mode requires less electricity consumption: there is little production and heat must be supplied to the electrolysis reactor. The advantage of this endothermic mode lies in the availability of an inexpensive source of heat. Everything depends on the nature and temperature of this heat source. On the other hand, the exothermic mode requires a greater consumption of electricity: there is therefore a significant production, but the electrolysis reactor must be cooled, which can be very expensive. The interest of this exothermic mode then depends a lot on the cost of electricity and the use of excess heat. Thus, thermal management of an electrolysis or co-electrolysis reactor is an important factor to consider. In addition, the transportation, storage and use of hydrogen require its pressurization. It is already known that instead of compressing the hydrogen produced, which has a significant cost, to carry out the electrolysis of the water directly from pressurized water vapor, the water then being compressed at the same time. liquid state beforehand, which is much less expensive. Different processes for obtaining a fuel gas by heterogeneous catalysis either directly from a mixture of H 2 and carbon dioxide CO 2, or indirectly from a synthesis gas (112+ CO) have been obtained. already been studied. In particular, the hydrogenation of CO2 in methane is an industrial process that has been studied at each energy shock, either to produce synthetic methane from pure CO2 and H2, or in gasification plants of coal with gases and more complicated conditions (Fischer-Tropsch process).
    [0007] For the methanation process, two ways are possible and have been more or less studied according to the state of the art. The first path is the direct one, with a single reaction according to the following equation: CO2 + 4H2 -) CH4 + 2H20: hydrogenation of CO2 The second pathway is indirect, with a two-step reaction according to the following equations: CO2 + H2 -> CO + H20: Inverse reaction of the gas with water (RWGS), C0 + 3H2-> CH4 + H20: hydrogenation of CO. As evidenced by the authors of the publication [1] (see in particular Figures 3 and 4), the methanation reactions are favored at high pressure and at low temperature according to Le Chatelier's law. Indeed, the thermodynamic calculations indicated in [1] indicate a theoretical conversion of 100% of CO2 to CH4 at less than 150 ° C against 83% at 400 ° C. However, it is also indicated that an optimum temperature and gas velocity are to be adjusted to achieve the best thermodynamic equilibrium in terms of CO2 conversion rate. The catalysts used for methanation are generally based on nickel (Ni) supported by an oxide of zirconium (ZrO 2), or based on Ni supported by aluminum oxide (Al 2 O 3). The publication [1] has highlighted the important catalytic activity for a nickel-based catalyst (Ni) supported by mixed cerium (Ce) oxides and Ce0.72Zr0.2802 foamed zirconium. Similarly, the publication [2] has shown, for a methanation under pressure of 30 bar, the excellent catalytic activity of a nickel-based (Ni) and iron (Fe) supported bimetallic catalyst supported by an aluminum oxide. (A1203) of the formula Ni-Fe / 7-Al 2 O 3. The use of hydrogen or synthesis gas by electrolysis EHT or co-electrolysis at high temperature requires, by definition, sufficient electricity available. However, when the energy sources, known as carbon-free, are by nature intermittent (wind, solar), situations can arise in which it is no longer possible with such sources to electrically power an electrolysis reactor. EHT or co-electrolysis at high temperature, or at least in sufficient quantity for the implementation is effective. However, once such an EHT electrolysis or co-electrolysis reactor has been put into operation, it is necessary to maintain the temperature, despite the possible intermittence of electricity production. , on the one hand, to avoid a thermal cycling that can damage it and on the other hand, to offer early start-up possibilities from the availability of electricity again. One solution that has already been considered to solve this problem of maintaining the temperature of the reactor in the absence of available electricity, is to reverse its operation, that is to say to operate in SOFC fuel cell ( acronym for "Solid Oxide Fuel Cell") to produce current from hydrogen H 2 or synthesis gas (mixture of hydrogen H 2 and carbon monoxide CO), which makes it possible to maintain the temperature of the reactor. This has the major disadvantage of producing electric power not on demand, but as soon as there is no more electricity available from outside sources. In addition, another major disadvantage is that one consumes, that is to say that one burns, thus fuel, ie H2 or synthesis gas, solely for purposes of keeping the reactor temperature and without obtaining other combustible product but only electricity that may not be useful at this time. There is therefore a need to improve the operating method of an electrolytic EHT or co-electrolysis reactor in order to maintain its temperature in the absence of available electricity, in particular without having to invert it in a fuel cell. SOFC and / or without burning H2 fuel or synthesis gas. The object of the invention is to respond at least in part to this need.
    [0008] SUMMARY OF THE INVENTION To this end, the invention relates, in one of its aspects, to a reactor operating method, referred to as a first reactor, comprising a stack of elementary electrolysis cells of SOEC type each formed of a cathode, an anode and an electrolyte interposed between the cathode and the anode, and a plurality of electrical and fluidic interconnectors each arranged between two adjacent elementary cells with one of its faces in electrical contact with the anode of one of the two elementary cells and the other of its faces in electrical contact with the cathode of the other of the two elementary cells, the cathodes being made of methanation reaction material (s).
    [0009] According to the invention, the following steps are carried out: a / electrically feeds the first reactor and, is fed and distributed to each cathode is water vapor 1120 or a mixture of water vapor and carbon dioxide. carbon dioxide, where steam is fed and distributed to the cathode of one of the two adjacent elementary cells and carbon dioxide is fed and distributed to the cathode of the other of the two elementary cells, so that to achieve at each cathode is a high temperature electrolysis of water vapor H20, or a high temperature co-electrolysis of water vapor and carbon dioxide, b / after step a1 and in the absence In the first reactor power supply, a mixture of hydrogen H 2 and CO 2 carbon monoxide, or a mixture of hydrogen H 2 and carbon dioxide CO 2, is fed and distributed to each cathode so as to realize at each cathode a methanation by cat heterogeneous alysis. By "absence of power supply" is meant here and in the context of the invention, an insufficient level of electric current to implement an electrolysis EHT or a co-electrolysis of H20 and CO2 in the SOEC reactor to stack. The invention thus consists, in the absence of electricity, in injecting synthesis gas H2 + CO or a H2 + CO2 mixture at the inlet of cathodes of the stack reactor so as to produce methane within the reactor itself. As the catalytic methanation reaction is exothermic, the stack reactor can therefore be maintained in temperature without loss of fuel, that is to say without it being burned. The fuel used for the methanation (synthesis gas or hydrogen) can advantageously be that produced beforehand during the operating phases with available electricity. Thus, according to the invention, the operation of the reactor is bi-mode in a way, that is to say in (co-) electrolyzer or methanation reactor.
    [0010] Indeed, when electricity is available in sufficient quantity for the reactor, the H2 hydrogen or the synthesis gas (H2 + CO) is produced respectively by electrolysis of water vapor H20 or by co-electrolysis of H2O + CO2. . In the absence of available electric current, synthesis gas (1-12 + CO) or hydrogen H2 with CO2 feeds the input of the cathodes of the stack so as to produce methane (CH4) in situ . The possible two-mode operation of the reactor according to the invention also makes it possible to envisage exclusively using the latter in a methanation reactor in the event of an electrical failure of the stack. Furthermore, thanks to the invention, the inversion of the reactor operation, that is to say the operation in electrolyser or co-electrolyser SOFC fuel cell can be made at will, at the request of a need for electricity, and not in a way imposed for the sole purpose of ensuring thermal control of the reactor in the absence of electricity. It is specified here that the interconnection devices, electrical and fluidic, also called interconnectors or interconnect plates, are the devices which provide the series connection from an electrical point of view of each electrolysis cell in the electrolysis cell. stacking of the EHT reactors and in parallel from a fluid point of view, thus combining the production of each of the cells. The interconnectors thus provide the power supply and collection functions and define circulation compartments (distribution and / or collection) of the gases. The electrolysis cells are advantageously of the support cathode type. By "cathode cell support" means here and in the context of the invention the definition already given s. s the field of electrolysis of water at high temperature EHT and designated by the acronym CSC for "Cathode-supported Cell", that is to say a cell in which the electrolyte and the electrode to oxygen (anode) are arranged on the thicker hydrogen or carbon monoxide electrode (cathode) which therefore serves as a support. For stage a /, the co-electrolysis of water vapor and carbon dioxide can advantageously be carried out in the stack reactor according to the teaching of the above-mentioned application FR 12 62174: the steam is fed and distributed. water to the cathode of one of the two adjacent elementary cells and carbon dioxide is supplied and distributed to the cathode of the other of the two elementary cells. This makes it possible to vary at will the ratio H2 / CO obtained at the outlet before mixing to constitute the synthesis gas converted into combustible gas in the chamber, and to facilitate the thermal management of the stack electrolysis cells whatever either the mode of operation (endothermic or exothermic mode), and this, reversibly according to the cost of the current. According to an advantageous embodiment, the hydrogen H 2 or the mixture of hydrogen H 2 and carbon monoxide CO supplying the cathodes during step b 1 is produced beforehand during step a /. Preferably, step a / is carried out at temperatures between 600 ° C and 1000 ° C. Preferably also, the step a / being carried out at pressures between 0 and 100 bar, preferably between 4 and 80 bar. According to an advantageous variant, step b / is carried out at pressures between 0 and 100 bar, preferably between 4 and 80 bar. The cathodes are preferably based on nickel (Ni) supported by zirconia (ZrO 2), preferably stabilized with yttrium oxide (Y 2 O 3) or based on Ni supported by ceria, such as ceria gadolinium (Ni-CGO). Advantageously, a draining gas, such as air, circulates at each anode during step a1. Advantageously, a draining gas, such as air, circulates at each anode during step b /. The draining gas flow rate at each anode is preferably adapted to the flow rate at the cathode to manage the thermal and pressure equalization in each of the chambers. The invention also relates, in another aspect, to a method for producing methane using the operating method just described, comprising the following step: c / one feeds, methane produced at the output a first reactor (SOEC), a second reactor adapted to perform a methanation, when the methane conversion rate at the outlet of the first reactor is less than a threshold value, and then feeds methane produced at the outlet of the second reactor, a storage tank or distribution network. or it is fed directly to methane produced at the outlet of the first reactor, a storage tank or a distribution network. The methane feed of the second reactor is also done by adding the unconverted H2 + CO (or CO2) mixture. Finally, the subject of the invention is a method for producing C1-14 methane, preferably according to the preceding method, from a so-called intermittent energy source, implementing the operating method described above, the step b / being implemented when said intermittent source is no longer capable of producing electricity in an amount sufficient to perform step a /. DETAILED DESCRIPTION Other advantages and characteristics of the invention will emerge more clearly from a reading of the detailed description of exemplary embodiments of the invention, given by way of illustration and without limitation with reference to the following figures among which: FIG. 1 is a schematic view showing the principle of operation of a high temperature water electrolyser; FIG. 2 is an exploded diagrammatic view of a l. high temperature steam electrolyser including interconnectors; FIG. 3 is a schematic view of a methane production process from step b / me. According to the invention, FIG. 4 is a schematic view of a single experimental electrochemical cell SOEC reactor for carrying out step b / of methanation of the process according to the invention. invention; 5A to 5C illustrate the production of the different species during step b / of methanation of the process according to the invention, p. of synthesis gas, and at respective pressures of 1 bar, 5 bar and 30 bar, FIGS. 6A to 6C illustrate the production of the various species during step b / of methanation of the process according to the invention, starting from of a mixture H2 and CO2, and at pressures of 1 bar, 5 bars and 30 bars, respectively. Throughout the present application, the outfits "vertical", "lower", "upper", "lower", "Up", "below" and "above" are to be understood by reference to a SOEC reactor as it is in vertical configuration of operation. Likewise, throughout the present application, the terms "inlet", "outlet", "downstream" and "upstream" are to be understood with reference to the direction of flow of the gases from their entry into the SOEC reactor up to their output from it. It should be noted that in FIGS. 1 to 3, the symbols and the arrows for supplying water vapor H20, for distributing and recovering hydrogen H 2 and oxygen O 2, and for the stream, for carbon dioxide CO 2, for The distribution and recovery of carbon monoxide CO and O 2 O 2 and current, and methane CH 4 are shown for the sake of clarity and accuracy, to illustrate the operation of a SOEC reactor 1 according to the invention. a separate methanation reactor 6. It is also specified that all the reactors operating according to steps a / and 13 / of the process according to the invention described are of the solid oxide type (SOEC), which operates at high temperature. Thus, all the constituents (anode / electrolyte / cathode) of an electrolysis cell are ceramics. Such constituents may be those of a SOFC fuel cell. The high operating temperature of the reactor 1 during electrolysis or co-electrolysis is typically between 600 ° C and 1000 ° C. Typically, the characteristics of a SOEC elemental electrolysis cell suitable for the invention, of the cathode support (CSC) type, may be those indicated as follows in Table 2 below. TABLE 2 25 Electrolysis Cell Constituent Material Ni-YSZ 5300 Current Density A.m2 Porosity 0.37 Permeability Ern Unit VC.eu Cathode 2 Thickness Thermal Conductivity Electrical Conductivity 315 1-Lm W 13.1 erl 10 'Tortuosity 4 One Water electrolyser is an electrochemical device for producing hydrogen (and oxygen) under the effect of an electric current. In electrolysers with high temperature EHT, the electrolysis of water at high temperature is carried out from steam. The function of a high temperature electrolyser EHT is to transform the water vapor into hydrogen and oxygen according to the following reaction: 2H 2 O -> 2H 2 O. This reaction is carried out electrochemically in the cells of the electrolyser. As shown schematically in FIG. 1, each elementary electrolysis cell 10 1 is formed of a cathode 2 and an anode 4 placed on either side of a solid electrolyte 3. The two electrodes (cathode and anode) 2, 4 are electronic conductors, porous material, and the electrolyte 3 is gas-tight, electronic insulator and ionic conductor. The electrolyte may be in particular an anionic conductor, more specifically - an anionic conductor of O 2 - ions and the electrolyzer is then referred to as anionic electrolyzer. The electrochemical reactions are at the interface between each of the electronic conductors and the ionic conductor. At the cathode 2, the half-reaction is the following: 2 H 2 O + 4 e - '2 H 2 + 2 O 2 -. At the anode 4, the half-reaction is as follows: 202- -> 02+ 4 e-. The electrolyte 3 interposed between the two electrodes 2, 4 is the migration site of the O 2 - ions, under the effect of the electric field created by the imposed potential difference Porosity 0.37 Permeability m2 2000 Current density A.m2 LSM Constituent material 20 Thickness L-1-1 m-1 Electrical conductivity YSZ Constituent material gra Thickness m Resistivity Anode 4 Thermal conductivity W mI K-1 Tortuosity 4 Electrolyte 3 0.42 9.6 1 iO4 between anode 4 and the cathode 2. As shown in parentheses in Figure 1, the water vapor at the cathode inlet can be accompanied. hydrogen and the hydrogen produced and recovered at the outlet can be accompanied by water vapor. Similarly, as shown in dashed lines, a draining gas, such as air can also be injected at the inlet to evacuate the oxygen produced. The injection of a draining gas has the additional function of acting as a thermal regulator. An elementary electrolysis reactor consists of an elementary cell as described above, with a cathode 2, an electrolyte 3, and anode 4 and two single pole connectors which perform the functions of electrical distribution, hydraulic and thermal. To increase the flow rates of hydrogen and oxygen produced, it is known to stack several elementary electrolysis cells on top of each other by separating them by interconnection devices, usually called interconnectors or bipolar interconnection plates. . The assembly is positioned between two end interconnection plates that support the power supplies and gas supplies to the electrolyser (electrolysis reactor). A high temperature water electrolyser (EHT) thus comprises at least one, usually a plurality of electrolysis cells stacked on top of each other, each element cell being formed of an electrolyte, a cathode and a cathode. an anode, the electrolyte being interposed between the anode and the cathode. The fluidic and electrical interconnection devices which are in electrical contact with one or more electrodes generally provide the power supply and collection functions and define one or more gas circulation compartments. Thus, a so-called cathodic compartment has the function of distributing electric current and water vapor as well as recovering hydrogen from the cathode in contact. A so-called anodic compartment has the function of distributing the electric current as well as recovering the oxygen produced at the anode in contact, possibly with the aid of a draining gas. Satisfactory operation of an electrolyzer EHT requires: good electrical insulation between two adjacent interconnectors in the stack, otherwise the elementary electrolysis cell interspersed between the two interconnectors will be short-circuited, a good electrical contact and a contact surface sufficient between each cell and interconnector, to obtain the lowest resis ce o between cell and interconnectors, a good seal between the two comp. separate, ie and cathodic, under penalty of recombination of the gases produced resulting in a drop in yield and especially the appearance of hot spots damaging the electrolyzer, - a good distribution of gases both in input and recovery of gases produced, at the risk of loss of yield, inhomogeneity of pressure and temperature within the different cells élémen; are even crippling cell degradations. FIG. 2 represents an exploded view of elementary patterns of a high temperature steam electrolyser according to the state of the art. This electrolyser EHT comprises a plurality of elementary electrolysis cells C1, C2 of solid oxide type (SOEC) stacked alternately with interconnectors 5. Each cell C1, C2 ... consists of a cathode 2.1, 2.2,. .. and an anode 4.1, 4.2, between which is disposed an electrolyte 3.1, 3.2 ....
    [0011] The interconnector 5 is a metal alloy component which provides separation between the cathode 50 and anode compartments 51, defined by the volumes between the interconnector 5 and the adjacent anode 4.2 and between the interconnector 5 and the adjacent cathode 2.1. respectively. It also distributes the gases to the cells. The injection of water vapor into each elementary pattern is done in the cathode compartment 50. The collection of the hydrogen produced and the residual water vapor at the cathode 2.1, 2.2 ... is carried out in the cathode compartment 50 downstream of the cell C1, C2 ... after dissociation of the water vapor therefrom. Collection of the oxygen produced at the anode 4.2 is performed in the anode compartment 51 downstream of the cell C1, C2 ... after dissociation of the water vapor therefrom.
    [0012] The interconnector 5 ensures the passage of the current between the cells C1 and C2 by direct contact with the adjacent electrodes, that is to say between the anode 4.2 and the cathode 2.1.
    [0013] In high temperature co-electrolysers EHT, high temperature co-electrolysis is carried out from water vapor and CO2 carbon dioxide. The function of a SOEC high temperature co-electrolyser is to transform water vapor and CO2 into hydrogen, carbon monoxide and oxygen according to the following reaction: CO2 + H20 -> CO + H2 ± 02. A co Electrolyser 1 may comprise exactly the same solid oxide constituents (SOEC) as an EHT electrolyser which has just been described. Usually, water vapor and CO2 carbon dioxide are mixed before entering the co-chlorinator and injected simultaneously into each cathode compartment 50.
    [0014] At present, when it is desired to carry out methanation by heterogeneous catalysis, two ways are possible. The first path is the direct one, with a single reaction according to the following equation: CO2 + 4H2 ---> CH4 + 2H20, The second path is the indirect one, with a two-step reaction according to the following equations: CO2 + H2 - > CO + 112 0 CO + 3112 - * GH4 + 1120 The methanation is carried out in a reactor in which the solid catalyst of the reaction is present. The hydrogen and optionally the carbon monoxide can be produced beforehand either by EHT electrolysis in an electrolysis reactor 1 described with reference to FIGS. 1 to 3, or by high temperature co-electrolysis also in a reactor of co-electrolysis 1 described. It is envisaged to carry out the electrolysis EHT or co-electrolysis at high temperature of water vapor H20 and carbon dioxide CO2, with so-called carbon-free energies which are by nature intermittent (wind, solar). However, with such energies, the production of electricity can be interrupted, or at least be reduced to a low level, over longer or shorter periods and which can be impromptu. Under these conditions, electrolysis EHT or co-electrolysis can no longer be provided by the SOEC reactor 1 because of the absence of electric current (voltage).
    [0015] However, if it is impossible to perform the electrolysis or the co-electrolysis, it is necessary to be able to maintain the temperature of the reactor 1 SOEC in order firstly to avoid a thermal cycling that can damage it and other to allow a quick restart as soon as the electric current is available again.
    [0016] To solve this problem, the inventors of the present invention have thought to feed and distribute at each cathode 2.1, 2.2, .... is a mixture of hydrogen H 2 and carbon monoxide CO, a mixture of hydrogen H 2 and of CO2 carbon dioxide, so as to achieve at each cathode methanation by heterogeneous catalysis. In other words, in the absence of available electricity, the SOEC reactor is assigned an additional function of a methanation reactor. In other words, the operation of the SOEC reactor 1 is bi-mode: - EHT electrolysis or co-electrolysis of H 2 O and CO 2 when the electricity is available in sufficient quantity, - methanation, in case of absence of available current, or any at least at a level insufficient to carry out an EHT electrolysis or coelectrolysis reaction. Wisely, the inventors have started from the realization that certain solid oxide cathode materials, particularly those based on zirconia (ZrO 2) supported nickel (Ni), used in SOEC reactors were also tested in as solid catalysts of the methanation reaction. The operation of methanation of a SOEC 1 reactor makes it possible to envisage a production of methane in the absence of electricity: Thus, the methane CH4 produced at the outlet of the reactor 1 supplies: either a second reactor 6, capable of methanation is carried out, in methane produced at the outlet of the first reactor when the conversion rate of the latter is less than. a threshold value, then supplying methane produced at the outlet of the second reactor, a storage tank or a distribution network, as shown in Figure 3; or directly a storage tank or a methane distribution network.
    [0017] The inventors of the present invention have made a solid-oxide single cell Cl reactor 1 to experimentally prove methanation within such a reactor. The experimental reactor 1 is shown in FIG. 4. It comprises a cell C1 consisting of a cathode 2.1, an anode 4.1 and an electrolyte 3.1 inserted between the cathode 2.1 and the anode 4.1. The cathode 2.1 used in question is a cermet with a diameter of 51 nm and consists of a stack of two layers, namely: a Ni-3YSZ support layer (ZrO 2 + 3 mol% Y 2 O 3), of thickness 500 - a Ni-8YSZ functional layer (ZrO 2 + 8 mol% Y 2 O 3), with a thickness of between 5 and 10 μm. The electrolyte 3.1 is 8YSZ (ZrO 2 + 8 mol% Y 2 O 3), with a thickness of 51 μm. The anode 4.1 is LSCo (strontium doped lanthanum cobaltite), of thickness 201.tm.
    [0018] The cell C1 is mounted in a support case 7 of alumina (A1203). The assembly of the cell C1 is sealed by means of a glass gasket 8 at the periphery of the electrolyte 3.1. The mounting of the cell C1 is further under compression with a maximum load of 2 kern2 as illustrated by the arrow F in FIG. 4. The housing 7 has in its lower part a central opening 70 for supplying gas (gas from synthesis or mixture H2 and CO2) and an opening 71 of gas recovery obtained by the reaction within the cathode 2.1. It also has, in its upper part, a central opening 72 for supplying draining gas (air) to the anode 4.1 and an opening 73 for draining the draining gas. Different contact grids 9, 10, 11 are arranged in contact respectively with the anode 4.1 and the cathode 2.1. More precisely, the gate 11 in contact with the cathode 2.1 is made of nickel, with a thickness of 0.45 mm, with 100 meshes / cm 2 and a unit diameter of wire of 0.22 mm. The contact grids 9, 10 are in turn gold and platinum. As illustrated in FIG. 4, the grids 9, 10, 11 allow a current I and / or voltage supply U of the cell C1 to carry out an EHT electrolysis or co-electrolysis reaction. H20 water vapor and CO2.
    [0019] A synthesis gas (H2 + CO) or an H2 + CO2 mixture at the inlet 70 of the cathode 2.1 and at the same time input air 72 of the anode 4.1, without polarization of the cell, was injected. The analysis of the gases was carried out, after condensation of the gases to eliminate 5 H2O, by gas micro-chromatography using the apparatus marketed by the company SRA under the name "MicroGC 3000". Two series of measurements were made with two different types of C1 cells from the same materials but from different manufacturers. The measurement results as well as calculations are reproduced below in Tables 3 and 4 each for a cell type. It is specified that the total value of the composition of the gases is slightly greater than 100% because of measurement uncertainties. k. I Flow rate Composition of the input gases Measured composition of the output gases Total gross 2 Total cell composition (% Vol) (% Vol) calculated from the exhaust gases with H20 (% Vol) (° C) input (NL / h)% H% C% CO% N% H% O% N% CH% C% CO% 0% N% CH% C% CO% H2 Total Gross 2 o 2 2 2 2 2 4 2 2 2 4 o 2 O 600 8.17 75 25 65.1 0.1 2.2 9.5 19.3 5.9 102, 59.5 0.1 2.0 8.7 17.7 5.4 8, 7 102, 2 2 600 8.17 80 20 71.0 0.1 1.8 3.8 11.8 12.8 101, 66.0 0.1 3.6 10.9 11.9 7.1 101 , 3 3 Cell temperature (° C) Tl T2 Total input flow (NL / h) Composition of input gases (% Vol)% H% C% CO% N 2 0 2 2 TABLE 4 Measured composition of Outflow gas (% Vol) Calculated composition of the outlet gases with H20 (% Vol)% CH 4% C o Total gross% H2 O Total gross 616, 603, 3 2 616, 604, 7 3 8,17 8,17 75 25 75 25 62.8 62.1 0.0 0.0 3.0 3.8 13.2 12.9 15.4 15.7 6.3 6.1 100, 7 100, 6 54.9 55 , 7 5,4 5,6 11,7 11,4 100, 7,100, 6% H 2% 0 2% N 2% CO 2% H 2% 0% N% CH% C 2 2 4 o% CO 2 0.0 3.4 11.7 13.6 Airflow (NL From these Tables 3 and 4, it can be concluded first that the C1 cell actually performs a methanation reaction. It can also be concluded that the cell C1 and therefore the reactor 1 undergoes a significant heating during methanation, all the more important that the air flow 5 to the anode is low. Therefore, it is advantageous to adjust the flow of draining gas (air) to the anodes of a SOEC reactor to control, by forced convection, the temperature rise due to methanation and thus preserve the SOEC cells from overheating. .
    [0020] The inventors of the present invention have performed thermodynamic calculations as follows to corroborate the experimental feasibility of methanation with CO2, CO, H2, and I-120 gases. They first considered the three reactions involved in the methanation of CO2 (and CO), which are: CO2 + 4H2 CH4 + 2hr-2 0 methanation of CO2 (1), CO + 3H2 <-> CH4 + H20 methanation of CO (2), CO2 + H2 <-> CO + H20 RWGS (Reverse Water Gas Shift) (3). The thermodynamic analysis, as done in the publication [3], was carried out by solving the system Pm, PH2O2 PH42 PCO2 Kf02 = 1H2 'CO, H2 CO2 KPWGS = 0 RPP co H20 (4) with equilibrium constants which write: p2 p - -1 Kp H20Δ CH4 =, pan - 21646 7.24E1 ° exp TP 1.22E13 exp -f 26830T K0 P = H20 CH4 = j (6) p3 p H2 CO PP 1.26E-2 exp r4639 7) Kp H20 cv = ^ T RWGS PP H2 CO2 The temperature T is given in degrees Kelvin, and the unit of the equilibrium constants KP in lease. The expressions of the kinetics of reaction are the following: C 0 2 f p. ## EQU1 ## ## STR2 ## KH + KPH2 + Kad PCH4 + co C H2 CH4 PH2 from (9) WR GS pp 20 K - H2 CO2 1 rRWGS _ - Pm, C0 H20 P. Koein Bad P '.. RWGS j 1+ Kad P + Kad P ± Kad P + -2- - 2- CO CO H2 Hi CH 4 CH4 P H2 i (10) with kmol as unit The symbols Pi represent the partial pressures in bars The kinetic constants here are given by the relations: kco2 = 1.02E15 exp (-243.9E3 RT (12) kRWGS = 1.955E6 exp RT and are expressed in lcmol.bail. kg, i1.11-1 It should be noted that these values have been identified for reforming between 400 and 600 ° C at 2 bar K-ad The adsorption constants are given by the relationships: K7 (1) = 8.23E-5 exp 70.65E3 2 RT 10 RT 1 (11) k = 4.225e expt 240.9E3 a, f - 67.13E3 Kaidi = 6.12E9 exp (82.9E3 38.28E3 = 6.65E4 exp RT RT KH` 220 = 1.77E5 exp (- 88.68E3 with com -e unit the bar4. FIGS. 5A to 5C show the curves of the molar fractions of each species obtained which were calculated as above for the methanation of CO at pressures of 1 bar, 5 bars and 30 bars, respectively. FIGS. 6A to 6C show the curves of the molar fractions of each species obtained which were calculated as above for the methanation of CO2 at pressures of 1 bar, 5 bars and 30 bars, respectively. From these curves, it follows that the pressure has a strong beneficial effect on the methanation from a temperature of 700K. For an identical conversion rate, the pressure makes it possible to work at temperatures higher than 250 ° C relative to the atmospheric pressure.
    [0021] Finally, whatever the pressure, the methanation of CO is preferable to that of CO2. The invention which has just been described, both by tests and by a thermodynamic analysis, makes it possible to envisage the production of methane in situ within a SOEC reactor.
    [0022] At 600 ° C and at atmospheric pressure, methane production is higher from CO than from CO2. Under the experimental conditions that have been selected, the production causes a significant rise in temperature of several degrees, which makes it possible to consider maintaining the temperature of a SOEC type reactor.
    [0023] Finally, methanation within a reactor under pressure makes it possible to envisage a higher conversion rate to higher methane as well as maintenance at a higher temperature. RT (17) The invention is not limited to the examples which have just been described; it is possible in particular to combine with one another characteristics of the illustrated examples within non-illustrated variants.
    [0024] References cited [1]: Fabien Ocampo et al, "Methanation of carbon dioxide over nickel-based Ce0.72Zr0.2802 mixed oxide catalysts prepared by sol-gel method", Journal of Applied Catalysis A: General 369 (2009) 90- 96; [2]: Dayan Tiang et al, "Bimetallic Ni-Fe total-methanation catalyst for the production of natural gas substitutes under high pressure", Journal of Fuel 104 (2013) 224-229. [3] Eduardo L. G. Oliveira, Carlos A. Grande, Alirio E. Rodrigues, "Effect of 10 catalyst activity in SMR-SERP for hydrogen production": Commercial Vs. broad-pore catalyst Chemical Engineering Science 66 (2011) 342-354
    权利要求:
    Claims (11)
    [0001]
    REVENDICATIONS1. A method of operating a reactor (1), said first reactor comprising a stack of elementary electrolysis cells (C1, C2, C3) of SOEC type each formed of a cathode (2.1,
    [0002]
    2.2, ...), an anode (4.1, 4.2, ...) and an electrolyte (3.1,
    [0003]
    3.2 ...) interposed between the cathode and the anode, and a plurality of electrical and fluidic interconnectors (5) each arranged between two adjacent elementary cells (C1, C2) with one of its faces in electrical contact with the anode (4.1) one (Cl) of the two elementary cells and the other of its faces in electrical contact with the cathode (2.2) of the other of the two cells (C2) elementary, the cathodes being of material (x) catalyst (s) of methanation reaction, process according to which the following steps are carried out: a / the first reactor is electrically powered and, at each cathode, either water vapor H20 or a mixture of steam vapor is supplied and distributed; water and carbon dioxide CO2, where steam is fed and distributed to the cathode of one of the two adjacent elementary cells and carbon dioxide is fed and distributed to the cathode of the other of the two elementary cells, so as to realize at a cathode is a high temperature electrolysis of water vapor H2O, or a high temperature co-electrolysis of water vapor and carbon dioxide, b / after step a1 and in the absence of power supply of the first reactor, is fed and distributed to each cathode is a mixture of hydrogen H 2 and CO carbon monoxide, a mixture of hydrogen H 2 and carbon dioxide CO 2, so as to perform at each cathode a methanation by heterogeneous catalysis. 2. The operating method according to claim 1, the H2 hydrogen or hydrogen mixture H2 and carbon monoxide CO supplying the cathodes during step b /, is produced beforehand in step ai. 3. Operating method according to claim 1 or 2, the step al = carried out at temperatures between 600 ° C and 1000 ° C.
    [0004]
    4. Method according to one of the preceding claims, step a / being carried out at pressures between 0 and 100 bar, preferably between 4 and 80 bar.
    [0005]
    5. Method according to one of the preceding claims, step b / being carried out at pressures between 0 and 100 bar, preferably between 4 and 80 bar.
    [0006]
    6. Method according to one of the preceding claims, the cathodes being based on nickel (Ni) supported by zirconia (ZrO 2) or ceria.
    [0007]
    7. Method according to one of the preceding claims, a draining gas, such as air, flowing at each anode during step a1.
    [0008]
    8. Method according to one of the preceding claims, a draining gas, such as air, flowing at each anode during step b /.
    [0009]
    9. The method of claim 8, the flow of draining gas at each anode is adapted to the cathodic flow rate for the thermal management and the balancing of the pressures between chambers.
    [0010]
    10. Process for producing methane using the operating method according to one of the preceding claims, comprising the following step: c / is fed, in methane produced at the outlet of the first reactor, a second reactor (6), capable of implementing a methanation, when the methane conversion rate at the outlet of the first reactor is below a threshold value, and then a methane produced at the outlet of the second reactor is fed with a storage tank or a distribution network, or it is fed directly to methane produced at the outlet of the first reactor, a storage tank or a distribution network.
    [0011]
    11. Process for producing methane CH4, preferably according to claim 10, at p. a so-called intermittent energy source, implementing the operating method according to one of claims 1 to 9, step b / being implemented when said intermittent source is no longer capable of producing electricity in an amount sufficient to perform step al.
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    同族专利:
    公开号 | 公开日
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    法律状态:
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    优先权:
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    PCT/IB2014/066171| WO2015083024A1|2013-12-03|2014-11-19|Method for operating an soec-type stack reactor for producing methane in the absence of available electricity|
    US15/101,584| US10145018B2|2013-12-03|2014-11-19|Method for operating an SOEC-type stack reactor for producing methane in the absence of available electricity|
    JP2016536194A| JP6564778B2|2013-12-03|2014-11-19|Method of operating a SOEC type stack reactor for the production of methane in the absence of available power|
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