CARBON DIOXIDE CAPTURE AND TRANSFORMATION SYSTEM

Abstract

System (100) for capturing and transforming carbon dioxide, comprising at least one reactor (10) having a cavity (11) in which is housed at least one compartment (12) comprising: a carbon dioxide capture block (13), said capture block comprising a capture charge capable of capturing and releasing carbon dioxide, and a catalyst block (14) comprising a catalyst capable of catalyzing a chemical methanation reaction between the carbon dioxide released by the capture block and dihydrogen; said at least one reactor having at least one gas inlet (20) in said cavity, and at least one gas outlet (30) from this cavity; said system further comprising at least one heating device (40) configured to heat said at least one reactor, and / or the cavity, and / or said at least one compartment. Figure for abstract: Figure 1

Description

Title of the invention: CARBON DIOXIDE CAPTURE AND TRANSFORMATION SYSTEM Technical field of the invention

[0001] The present invention relates to a system for capturing and transforming carbon dioxide and a method for implementing such a system. Technological background

[0002] It is commonly accepted that carbon dioxide is a greenhouse gas whose release into the atmosphere by human activities has an impact on the environment. Solutions are being implemented to reduce carbon dioxide emissions or to increase its value.

[0003] It is particularly well known that carbon dioxide can be captured or trapped in different materials, this is called sequestration. At the same time, it is known that carbon dioxide can be recovered by various chemical reactions such as methanation, in other words the production of methane. However, these sequestration and recovery operations are often carried out sequentially in separate installations, without the sequestered carbon dioxide necessarily being used as a reagent for methanation.

[0004] Also, an objective of the invention is to propose a system which combines in a simple manner the operations of sequestration and recovery of carbon dioxide. Summary of the invention

[0005] A system for capturing and transforming carbon dioxide is therefore proposed, comprising at least one reactor having an internal cavity in which is housed at least one compartment comprising: - a carbon dioxide capture block, this capture block comprising a capture charge capable of capturing and releasing carbon dioxide, and - a catalyst block comprising a catalyst capable of catalyzing a chemical methanation reaction between the carbon dioxide released by the capture block and dihydrogen; the at least one reactor further comprising at least one gas inlet into the internal cavity, and at least one gas outlet from this internal cavity;

[0006] the system further comprising at least one heating device configured to heat the at least one reactor, and / or the internal cavity, and / or the at least one compartment.

[0007] Thus, thanks to the invention, a simplification of a methanization operation is ensured by bringing together in a single system the constituents necessary for such an operation. operation. In fact, the carbon dioxide is captured, and therefore stored, in the capture block located in the internal cavity of the reactor and is subsequently released into this same internal cavity for the methanization reaction. This helps to limit the size of the system.

[0008] The system according to the invention may comprise one or more of the following characteristics, taken in isolation from one another or in combination with one another: - the internal cavity comprises several compartments stacked on top of each other, the compartments being stacked from the at least one gas inlet to the at least one gas outlet, such that the at least one inlet is located at a lower end of the internal cavity and the at least one outlet is located at an upper end of the internal cavity, - the capture charge is based on calcium oxide mixed with a chemically inert compound, - the gas inlet comprises two gas inlets capable of supplying the internal cavity with two separate gases, such as carbon dioxide and dihydrogen, - the outlet comprises two gas outlets capable of evacuating at least two distinct gases from the internal cavity, such as a surplus of carbon dioxide-based gas on the one hand and one or more products of the chemical methanation reaction on the other hand, - the at least one compartment comprises a first layer of carbon felt between the capture block and the catalyst block, and a second layer of carbon felt such that the catalyst block is between the first and second layers of carbon felt, - the at least one reactor and the at least one heating device are included in a hollow enclosure comprising a volume of a heat transfer gas, - the at least one reactor and the at least one heating device are each, in the enclosure, in a tubular form, the at least one reactor and the at least one heating device being parallel to each other, - the system comprises a plurality of tubular reactors and a plurality of tubular heating devices mounted, in the enclosure, in parallel with each other, so that each reactor is in the vicinity of at least one heating device and each heating device is in the vicinity of at least one reactor, - the at least one heating device is a heat exchanger configured for circulation of a heat transfer fluid capable of recovering and / or providing a heat energy to the at least one reactor, and / or to the internal cavity, and / or to the at least one compartment, - the at least one compartment is in the form of a plate, the plate having a layer formed by an interpenetration of the carbon dioxide capture block and the catalyst block, the layer connecting each of the opposite faces of the plate, - the plate is configured to define a passage path for a gas or gas mixture, - the system comprises a plurality of plates arranged one above the other so that a given plate has at least one of its faces opposite another face of another plate, the faces of each plate extending respectively in parallel planes, - - the capture block has a porous or microporous structure, permeable to a gas, preferably carbon dioxide, - - the catalyst block has a porous or microporous structure, permeable to a gas, preferably carbon dioxide, - - the catalyst block comprises a catalyst compound mixed with a compound chemically inert, - - the circulation of the heat transfer fluid in the heat exchanger is in a direction opposite to the direction of gas flow in the reactor, - - at least one input is a gas distributor, - - the gas distributor is made of carbon fiber composite material, - - the capture block is on the side of the at least one gas inlet and the block ca talyser is on the side of at least one gas outlet.

[0009] The invention also relates to an installation comprising at least one carbon dioxide capture and transformation system as described above and a pyrocarbon densification system, the carbon dioxide capture and transformation system being configured to receive carbon dioxide and / or dihydrogen from the pyrocarbon densification system.

[0010] The invention also relates to a method for capturing and transforming carbon dioxide as described above, this method comprising the following steps: a. selectively introducing carbon dioxide-based gas into the internal cavity of the reactor through the at least one inlet such that carbon dioxide is captured by the compartment capture block; b. selectively introducing dihydrogen-based gas into said internal cavity of the reactor through said at least one inlet; c. heating the reactor and / or the internal cavity and / or the compartment by means of the heating device such that carbon dioxide captured by the capture block is released from the capture block, the released carbon dioxide chemically reacting with dihydrogen upon contact with the catalyst block; and d. evacuating the gaseous mixture from the internal cavity of the reactor through the at least one outlet.

[0011] The method according to the invention may comprise one or more of the following characteristics, taken in isolation from one another or in combination with one another: - - the process comprises a step e) of separation of the gases from the gas mixture, - - after step d), a neutral gas is injected into the reactor so as to purge the remaining gas mixture before repeating the process from step a). Brief description of the figures

[0012] The invention will be better understood with the aid of the following description, given solely by way of example and with reference to the appended drawings in which:

[0013] [Fig.l] represents a schematic view of an embodiment of the carbon dioxide capture and transformation system according to the invention,

[0014] [Fig.2] represents a schematic view of an example of a compartment included in the system according to the invention,

[0015] [Fig. 3] represents a schematic view of another embodiment of the system according to the invention, in particular when the system comprises a plurality of reactors and tubular heating devices, the assembly being housed in a hollow enclosure,

[0016] [Fig.4] represents a schematic view along a transverse sectional plane of the system of [Fig.3],

[0017] [Fig. 5] represents a schematic sectional view of another embodiment of the system according to the invention, in particular when the system comprises a plurality of U-shaped reactors and a heat exchanger as a heating device,

[0018] [Fig. 6] represents a schematic view of another embodiment of the system according to the invention, in particular when the system is in the form of a plate exchanger,

[0019] [Fig.7] represents a very schematic view of the circulation of gas flows between the plates of [Fig.6],

[0020] [Fig.8] represents a very schematic view of an installation comprising a system for capturing and transforming carbon dioxide and a source system for carbon dioxide and / or dihydrogen,

[0021] [Fig.9] represents a block diagram of a method for implementing a system carbon dioxide capture and transformation. Detailed description of the invention

[0022] The system 100 for capturing and transforming carbon dioxide according to the invention comprises at least one reactor 10 which comprises an internal cavity 11 in which is housed at least one compartment 12 comprising a carbon dioxide capture block 13 and a catalyst block 14. The carbon dioxide capture block 13 further comprises a capture charge capable of capturing and releasing carbon dioxide. The catalyst block 14 further comprises a catalyst capable of catalyzing a chemical methanation reaction between the carbon dioxide released by the capture block 13 and dihydrogen.

[0023] Each reactor 10 comprises at least one gas inlet 20 in the internal cavity 12 and at least one gas outlet 30 from this internal cavity 11.

[0024] The system 100 according to the invention further comprises at least one heating device 40 configured to heat each reactor 10, and / or the internal cavity 11 of each reactor 10, and / or each compartment 12 of each reactor 10. The heating device 40 may for example be configured to surround all or part of the reactor 10.

[0025] The heating device 40 may be a heat exchanger configured for circulation of a heat transfer fluid capable of recovering and / or supplying heat energy to the reactor 10, and / or internal cavity 11, and / or compartment 12. As a variant, the heating device 40 may be an electrical appliance equipped with one or more heating resistors.

[0026] [Fig. 1] shows that the internal cavity 11 of the reactor 10 may comprise several compartments 12 which are stacked on top of each other. In such a configuration, the compartments 12 are stacked from the gas inlet 20 to the gas outlet 30, so that the inlet 20 is located at a lower end of the internal cavity 11 and the gas outlet 30 is located at an upper end of the internal cavity 11. It is understood that, in this example, the system 100 is oriented generally vertically. In this example of [Fig. 1], three compartments 12 are shown in a non-limiting manner. The reactor 10 may comprise more than three compartments in the internal cavity 11.

[0027] Advantageously, the carbon dioxide capture block 13 is positioned on the side of the gas inlet 20 and the catalyst block 14 is positioned on the side of the gas outlet 30. This configuration is preferred in order to facilitate the interaction of the carbon dioxide released by the capture block 13 with the catalyst block 14. Thus, when several compartments 12 are stacked in the cavity 11, an alternation between the capture blocks 13 and catalyst blocks 14 can be observed.

[0028] With reference to [Fig.2], each compartment 12 or at least one compartment 12 may comprise a first layer 15a of carbon felt between the capture block 13 and the catalyst block 14. Each compartment 12 or at least one compartment 12 may also comprise a second layer 15b of carbon felt located on the catalyst block so that, when the compartment 12 comprises two layers 15a, 15b of carbon felt, the catalyst block 14 is between the first and second layers 15a, 15b of carbon felt.

[0029] Carbon felt is a material that has thermal insulation properties. Also, within the framework of the invention, the first and second layers 15a, 15b of carbon felt make it possible to limit the dissipation of heat outside the compartment. This heat can be provided on the one hand by the heating device 40 or on the other hand come from exothermic chemical reactions that take place in the compartment 12. These exothermic reactions can take place at the carbon dioxide capture block 13.

[0030] Advantageously, the charge of the capture block 13 is based on calcium oxide mixed with a chemically inert compound. This chemically inert compound can serve as a support for the calcium oxide which is then distributed on or diluted in this inert compound. The chemically inert compound is for example, in a non-limiting manner, an aluminum oxide (A12O3) or a silicon oxide (SiO2). It is well known that calcium oxide is a material allowing capture of carbon dioxide according to a chemical carbonation reaction defined as follows:

[0031] [Math.l] CO2 (g) 3" (LciCO^ ( q

[0032] The reaction of gaseous carbon dioxide (CO2) with solid calcium oxide (CaO) leads to the formation of solid calcium carbonate (CaCO3). This reaction is exothermic, with a standard reaction enthalpy of -178 kJ / mol. It is understood that to shift the equilibrium of the reaction in the opposite direction and therefore release carbon dioxide from the calcium carbonate, an input of energy is necessary. This energy is notably provided by the heating device 40.

[0033] Generally speaking, during the carbonation reaction, the carbon dioxide will tend to combine with the capture charge, for example the calcium oxide mentioned above, on the surface of the grains of the capture charge. As a result, a layer that can be described as a passive layer is formed and blocks the interactions between the carbon dioxide and the capture charge.

[0034] Also, the capture block 13 advantageously has a porous or microporous structure which is permeable to a gas, preferably to carbon dioxide. This has the advantage of increasing the contact surface between the capture charge and the gas. In this way, the rate of capture of carbon dioxide by the capture block can be improved.

[0035] Advantageously, the catalyst block 14 comprises a chemical reaction catalyst compound mixed with a chemically inert compound. The chemically inert compound can serve as a support for the catalyst compound which is then distributed over or diluted in this inert compound. The inert compound is, for example, in a non-limiting manner, an aluminum oxide or a silicon oxide. The catalyst of the catalyst block 14 can be, in a non-limiting manner, a compound based on nickel, manganese, platinum, palladium, ruthenium, rhodium or cobalt.

[0036] As for the capture block 13, the catalyst block 14 may have a porous or microporous structure which is permeable to a gas. This makes it possible to develop the contact surface between the catalyst and the gaseous species such as carbon dioxide and dihydrogen in order to improve the efficiency of the chemical methanation reaction described below.

[0037] The catalyst block 14 is capable of catalyzing a chemical reaction between the carbon dioxide released by the capture block 13 and dihydrogen, defined by the following methanation reaction:

[0038] [Math.2] ^ ^2 (g) + 4H2 (g) (g) + 2 H2O^

[0039] The reaction of carbon dioxide gas with hydrogen gas leads to the formation of methane (CH4) and water vapor. This reaction is exothermic, with a standard enthalpy of reaction of -168 kJ / mol.

[0040] The gas inlet 20 in the internal cavity 11 may be a gas distributor. The gas distributor may be made of a carbon fiber composite material.

[0041] The gas inlet 20 in the internal cavity 11 may comprise two gas inlets 21, 22 capable of supplying the internal cavity 11 with two distinct gases, such as carbon dioxide and dihydrogen.

[0042] The gas outlet 30 may comprise two gas evacuations 31, 32 capable of evacuating at least two distinct gases from the internal cavity 11, such as a surplus of carbon dioxide-based gas on the one hand and one or more product(s) of the chemical methanation reaction on the other hand.

[0043] We now turn to Figures 3 and 4 which represent another embodiment of the system 100. In this embodiment, the reactor(s) 10 and the heating device(s) 40 may be included in a hollow enclosure 50. This hollow enclosure 50 is furthermore designed to comprise a volume 51 of a heat transfer gas. This heat transfer gas is preferably argon.

[0044] In the particular example of Figures 3 and 4, the system 100 comprises four reactors 10 and four heating devices 40. The number of reactors 10 or heating devices 40 is not limiting. Similarly, the parity between reactors 10 and heating devices 40 is not limiting. In other words, there may be more than reactors 10 than heating devices 40, or vice versa.

[0045] In this example, the reactor(s) 10 are in the enclosure 50 in a tubular shape. The heating device(s) 40 are in the enclosure 50 in a tubular shape. By tubular shape is meant a shape that extends along a longitudinal axis. The section of this tubular shape may be generally circular or rectangular.

[0046] The reactor(s) 10 and the tubular heating device(s) 40 may be parallel to each other. This has the advantage of limiting the space requirement in the enclosure 50.

[0047] When the system 100 comprises a plurality of tubular reactors 10 and a plurality of tubular heating devices 40 mounted, in the enclosure 50, in parallel with each other, each reactor 10 is advantageously in the vicinity of at least one of the heating devices 40 and each heating device 40 is advantageously in the vicinity of at least one reactor 10.

[0048] In the example of Figures 3 and 4, each reactor 10 of the plurality of reactors 10 can be connected, upstream, to the gas inlet 20 and, downstream, to the gas outlet 30.

[0049] In the embodiment of Figures 3 and 4, the heating device(s) 40 are advantageously heat exchangers. In a heat exchanger circulates a heat transfer fluid which advantageously circulates in a direction opposite to the direction of flow of the gases in a reactor 10. In other words, the heat transfer fluid enters the heat exchanger through an inlet path 41 located on the same side as the gas outlet 30, and leaves the heat exchanger through an outlet path 42 located on the same side as the gas inlet 20. In this configuration, the heat exchanger makes it possible to control on the one hand the heat energy supplied to the system but also, when necessary, to remove excess heat energy from the system when the temperature becomes too high.

[0050] [Fig. 5] illustrates a variant of the embodiment of Figures 3 and 4. In this embodiment, the reactor(s) 10 have a U-shape. The reactor(s) 10 are advantageously located directly in the heating device 40 which is a heat exchanger configured for the circulation of a heat transfer fluid as mentioned above. The heat exchanger also has a plurality of baffles 43 designed to lengthen the path of the heat transfer fluid in the heat exchanger and thus improve the transfers of heat energy between the heat transfer fluid and the reactor(s) 10.

[0051] Figures 6 and 7 illustrate another embodiment of the system 100. In this embodiment, the system 100 is in the form of a plate exchanger. In such a plate exchanger, the plates 60 are staged parallel to each other in the reactor 10. A first primary flow F1 of a gas based on carbon dioxide circulates in the reactor 10 by entering through the inlet 20, and a second primary flow F3 of a dihydrogen-based gas circulates in the reactor 10 by entering through the inlet 20'. From the first primary flow F1, a plurality of first secondary flows F1' can circulate between the plates 60 along a passage path 64. Similarly, from the second primary flow F3, a plurality of second secondary flows F3', F3” can circulate between the plates 60 along a passage path 64'. The exchanger is designed such that the first secondary flows F1' and the second secondary flows F3', F3” do not mix, in other words that the passage paths 64, 64' specific to them do not communicate. It is understood that each of the secondary flows F1', F3', F3” circulates alternately from one stage to the other.Thus, we understand that on a given first stage we will have the second secondary flow F3', on a second stage, located above or below the given first stage, we will have the first secondary flow Fl', then on a third stage, located above or below the given first stage, we will have the second secondary flow F3”, and so on. We also understand that the terms first stage, second or third stage do not designate a stacking order but any stages of the plate exchanger. In this plate exchanger configuration, the gases circulate continuously.

[0052] After their respective passage between the plates 60, the first secondary flows F1' join a first tertiary flow F2 which is evacuated from the reactor 10 via the outlet 30. The first tertiary flow F2 is depleted of carbon dioxide.

[0053] After their respective passage between the plates 60, the second secondary flows F3', F3” join a second tertiary flow F4 which is evacuated from the reactor 10 via the outlet 30'. The second tertiary flow F4 is depleted in dihydrogen but enriched in methane and water vapor, products of the methanation reaction.

[0054] In this embodiment, each compartment 12 is in the form of a plate 60, this plate 60 having on each of its opposite faces both the capture block 13 and the catalyst block 14. Advantageously, the capture block 13 and the catalyst block 14 interpenetrate and form a layer 61. That is to say that the capture block 13 and the catalyst block 14 are merged into one another. In the above, it has been described that the capture blocks 13 and catalyst 14 may be porous or microporous. It is understood that the layer 61 may also be porous or microporous. Generally, the layer 61 may have characteristics similar to those described for the capture blocks 13 and catalyst 14.

[0055] With reference to [Fig.7], the layer 61 advantageously connects the opposite faces 62, 63 of a plate 60. During the passage of the first secondary flow F1' between the plates 60, the carbon dioxide will be captured by the layer 61 (arrows S), in particular by the capture charge, such as the calcium oxide described previously. In the same time, the dihydrogen supplied by the second secondary flow F3, F3' can diffuse into the layer 61 (arrows D). Under the effect of heat and the displacement of the reaction equilibrium, the carbon dioxide can be released by the capture charge and be entrained by the dihydrogen to a catalyst grain of the layer 61 so that the carbon dioxide and the dihydrogen react together according to the methanation reaction to give methane and water which are released into the first secondary flow Fl' (arrows R).

[0056] The invention also relates, with reference to [Fig.8], to an installation 200 which comprises at least one system 100 for capturing and transforming carbon dioxide as described above and a pyrocarbon densification system 110, the system being configured to receive carbon dioxide and / or dihydrogen resulting from the pyrocarbon densification.

[0057] Pyrocarbon densification refers to a controlled pyrolysis of a mixture of light hydrocarbons, i.e. those containing a carbon chain of one to four carbons. This pyrolysis generally takes place at high temperature and low pressure. At the end of this pyrolysis, a carbon deposit is produced while by-products such as volatile hydrocarbons and dihydrogen are evacuated and separated.

[0058] At the outlet of the pyrocarbon densification system 110, the dihydrogen emitted does not have a sufficient degree of purity to be directly recovered in other technical applications such as fuel cells. To be recovered in these applications, an expensive purification treatment is necessary.

[0059] On the other hand, the degree of purity of the dihydrogen for the chemical reaction of methanation is of little importance. Also, the installation 200 has the advantage of allowing direct recovery of by-products. The advantage is also to reduce the environmental impact of an industrial site by reducing the emission of carbon dioxide.

[0060] The carbon dioxide may also come from system(s) 120 other than the pyrocarbon densification system 110. Thus, the dihydrogen may come from a pyrocarbon densification system 110 and the carbon dioxide may come from a pyrocarbon densification system 110 and / or from another system 120 generating carbon dioxide.

[0061] The invention also relates to a method 200 for implementing the system 100 for capturing and transforming carbon dioxide as described above, and illustrated by a block diagram in [Fig.9]. The different steps of the method 200 are detailed below.

[0062] In a step 302, or step a), the carbon dioxide-based gas is selectively introduced into the internal cavity 11 of the reactor 10 through the gas inlet 20 so that the carbon dioxide is captured by the capture block 13 of the compartment 12. Carbon dioxide gas can, for example, be fumes emitted by an incineration plant or come from various industrial processes.

[0063] In a step 304, or step b), the dihydrogen-based gas is selectively introduced into the internal cavity 11 of the reactor 10 via the gas inlet 20. The dihydrogen may be the by-product of various industrial processes such as, for example, a pyrocarbon densification process.

[0064] In step 304, the dihydrogen can be introduced into the internal cavity 11 with a pressure of between 1 and 3 bars.

[0065] In a step 306, or step c), the reactor 10 and / or the internal cavity 11 and / or at least one compartment 12 is heated by means of the heating device 40 so that carbon dioxide captured by the capture block 13 is released from the capture block 13, the released carbon dioxide reacting chemically with dihydrogen in contact with the catalyst block 14.

[0066] In step 306, the heating of the reactor 10 and / or the internal cavity 11 and / or at least one compartment 12 shifts the balance of the capture charge of the capture block 13, which ensures a release of carbon dioxide. The released carbon dioxide then reacts with the dihydrogen according to the methanation reaction described previously. It is understood that with the heating device 40, control of the kinetics of the chemical reactions is ensured.

[0067] The reactor 10 and / or the internal cavity 11 and / or at least one compartment 12 can be heated to reach a temperature between 550°C and 750°C.

[0068] During step 306, the pressure in the reactor 10 and / or the internal cavity 11 and / or at least one compartment 12 can be monitored by means of a pressure sensor. Monitoring the pressure makes it possible to monitor the progress of the chemical methanation reaction. Indeed, during methanation, a drop in pressure is observed. When this pressure no longer drops and becomes stable in the reactor 10 and / or the internal cavity 11 and / or at least one compartment 12, this indicates that the available carbon dioxide has been entirely consumed.

[0069] In a step 308, or step d), the gas mixture is evacuated from the internal cavity 11 of the reactor 10 via the gas outlet 30.

[0070] After step 308, a neutral gas such as argon or nitrogen may be injected into the reactor 10 and / or the internal cavity 11 and / or the compartment(s) 12 so as to purge the remaining gas mixture.

[0071] At the end of the purge, the method 300 can start again from step 302, or step a).

[0072] In a step 310, or step e), the gases which make up the gas mixture are advantageously separated so as to isolate the methane resulting from the chemical methanation reaction between carbon dioxide and dihydrogen from step 306. A system with membranes can be used for separation.

Claims

Claims

1. System (100) for capturing and transforming carbon dioxide, comprising at least one reactor (10) having an internal cavity (11) in which is housed at least one compartment (12) comprising: a carbon dioxide capture block (13), said capture block (13) comprising a capture charge capable of capturing and releasing carbon dioxide, and a catalyst block (14) comprising a catalyst capable of catalyzing a chemical methanation reaction between the carbon dioxide released by the capture block (13) and dihydrogen; said at least one reactor (10) further comprising at least one gas inlet (20) into said internal cavity (11), and at least one gas outlet (30) from this internal cavity; said system (100) further comprising at least one heating device (40) configured to heat said at least one reactor (10), and / or the internal cavity (11), and / or said at least one compartment (12).

2. System (100) according to claim 1, wherein the internal cavity (11) comprises several compartments (12) stacked on top of each other, said compartments (12) being stacked from said at least one gas inlet (20) to said at least one gas outlet (30), such that said at least one inlet is located at a lower end of the internal cavity (11) and said at least one outlet is located at an upper end of the internal cavity (11).

3. System (100) according to any one of claims 1 or 2, wherein said capture charge of the capture block (13) is based on calcium oxide mixed with a chemically inert compound.

4. System (100) according to any one of claims 1 to 3, wherein said at least one gas inlet (20) comprises two gas inlets (21, 22) capable of supplying said internal cavity (11) with two distinct gases, such as carbon dioxide and dihydrogen.

5. System (100) according to any one of claims 1 to 4, wherein said at least one gas outlet (30) comprises two gas evacuations (31, 32) capable of evacuating at least two distinct gases from the internal cavity (11), such as a surplus of carbon dioxide-based gas on the one hand and one or more products of the chemical methanation reaction on the other hand.

6. System (100) according to any one of claims 1 to 5, in wherein said at least one compartment (12) comprises a first layer (15a) of carbon felt between the capture block (13) and the catalyst block (14), and a second layer (15b) of carbon felt such that the catalyst block is between the first and second layers (15a, 15b) of carbon felt.

7. System (100) according to any one of claims 1 to 6, wherein said at least one reactor (10) and said at least one heating device (30) are included in a hollow enclosure (50) comprising a volume (51) of a heat transfer gas.

8. System (100) according to claim 7, wherein said at least one reactor (10) and said at least one heating device (30) are each, in said enclosure (50), in a tubular form, said at least one reactor and said at least one heating device being parallel to each other.

9. System (100) according to claim 8, comprising a plurality of tubular reactors (10) and a plurality of tubular heating devices (40) mounted, in the enclosure (50), in parallel with each other so that each reactor (10) is in the vicinity of at least one heating device (40) and that each heating device (40) is in the vicinity of at least one reactor (10).

10. System (100) according to any one of claims 1 to 9, wherein said at least one heating device (40) is a heat exchanger configured for circulation of a heat transfer fluid capable of recovering and / or supplying heat energy to said at least one reactor (10), and / or to said internal cavity (11), and / or to said at least one compartment (12).

11. System (100) according to any one of claims 1 to 5, wherein said at least one compartment (12) is in the form of a plate (60), said plate having a layer (61) formed by an interpenetration of said carbon dioxide capture block (13) and said catalyst block (14), said layer (61) connecting each of the opposite faces (62, 63) of said plate (60).

12. The system (100) of claim 11, wherein said plate (60) is configured to define a passage path (64, 64') for a gas or gas mixture.

13. System (100) according to any one of claims 11 or 12, comprising a plurality of plates (60) stacked one above the other so that a given plate has at least one of its faces (62) opposite another face (63) of another plate, said faces extending respectively in parallel planes.

14. Installation (200) comprising at least one system (100) for capturing and transforming carbon dioxide according to any one of claims 1 to 13 and a pyrocarbon densification system (110), said system (100) for capturing and transforming carbon dioxide being configured to receive carbon dioxide and / or di-hydrogen from said pyrocarbon densification system (110).

15. A method of implementing a carbon dioxide capture and transformation system according to any one of claims 1 to 13, said method comprising the following steps: a. selectively introducing carbon dioxide-based gas into the internal cavity (11) of the reactor (10) through said at least one inlet (20) so that carbon dioxide is captured by the capture block (13) of the compartment (12); b. selectively introducing into said internal cavity (11) of the reactor (10) through said at least one inlet (20) dihydrogen-based gas; c. heating the reactor (10) and / or the internal cavity (11) and / or the compartment (12) by means of the heating device (40) so that carbon dioxide captured by the capture block (13) is released from said capture block (13), said released carbon dioxide reacting chemically with dihydrogen in contact with the catalyst block (14); and d. evacuate the gas mixture from the internal cavity (11) of the reactor (10) through said at least one outlet (30).

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