On-site electricity generation which is not connected to an electrical grid from methane or methanol and has carbon dioxide circularity
Patent Information
- Application Number
- EP2023782210
- Authority / Receiving Office
- EP · EP
- Patent Type
- Applications
- Current Assignee / Owner
- Priority Date
- 2022-09-27
- Filing Date
- 2023-09-27
- Publication Date
- 2025-08-06
AI Technical Summary
The challenge is to reduce the environmental impact of electricity production in remote or mobile units not connected to the conventional electrical network, such as boats, by minimizing carbon dioxide emissions from fuel cells used to generate power, while also providing a reliable energy source.
A dual-unit system where the first unit produces methane or methanol from hydrogen and carbon dioxide, and the second unit uses a fuel cell to generate electricity from this fuel, with integrated carbon dioxide capture and recycling, enabling the reuse of CO2 in the synthesis process.
This approach significantly reduces carbon footprint by recycling carbon dioxide and providing a reliable energy source for units not connected to the electrical network, such as boats, while minimizing greenhouse gas emissions.
Smart Images
Figure 1.1
Abstract
Description
[0001] DESCRIPTION
[0002] TITLE: On-site, off-grid electricity production from methane or methanol, with carbon dioxide circularity
[0003] The present invention relates to an installation for producing electricity within a unit, hereinafter called the “second unit”, from methane or methanol produced on another unit, hereinafter called the “first unit”, with recovery of carbon dioxide, the two units being located on two separate industrial sites.
[0004] In particular, the invention will apply to the case of a first unit connected to the conventional electrical network (continental metropolitan network), preferably a terrestrial unit, and a second unit not connected to the conventional electrical network.
[0005] Examples of units not connected to the conventional electricity network include units on aquatic sites (sea, lake or river), units located in rural areas not served by an electricity network, units located in island areas, etc., and / or all mobile units.
[0006] For example, on an aquatic unit, many auxiliary elements consume energy: refrigerators, navigation lights, anchor lights, VHF, interior lighting, navigation aids, water pump, etc. This energy, necessary for safety and comfort, is drawn from the on-board batteries which therefore need to be recharged regularly.
[0007] An aquatic unit such as boats will have a significant energy requirement in terms of engine power.
[0008] One of the solutions that exists to generate this energy and recharge the batteries needed by the auxiliaries is the use of fuel cells.
[0009] A fuel cell generates an electric current through an electrochemical reaction between a combustible fluid and oxygen in the air. The fuel cell typically consists of one or more solid oxide fuel cells (or "SOFCs" for "Solid Oxide Fuel Cells").
[0010] These cells are intended primarily for stationary applications with an output power ranging from 1 kW to 2 MW. In the context of the invention, the fuel cell device will preferably provide an output power ranging from 15 MW to 100 MW.
[0011] An SOFC element typically consists of four layers, three of which are ceramic. A single stack of these four layers is typically a few millimeters thick. Dozens of these stacks are then stacked in series to form a stack.
[0012] In these batteries, oxygen ions formed on the cathode side are moved through a solid oxide electrolyte at high temperature to react with the fuel gas, for example hydrogen, on the anode side.
[0013] This electrochemical reaction leads to the production of electricity as well as the formation of carbon dioxide and water, resulting from the electrochemical reaction.
[0014] Carbon dioxide (CO2), however, is one of the main greenhouse gases, whose releases into the atmosphere contribute to global warming. In order to reduce the environmental impact of fuel cells, it is therefore necessary to reduce carbon dioxide emissions into the atmosphere as much as possible.
[0015] From this, a problem that arises is to provide an electricity production facility with a reduced environmental impact.
[0016] A solution of the present invention is an electricity production installation 1, comprising two units, a first unit A and a second unit B, located on two separate industrial sites with:
[0017] - the first unit A comprising a synthesis device 8 capable of producing methane or methanol 15 from hydrogen 2 and carbon dioxide 4 from the second unit B, and
[0018] - the second unit B comprising a fuel cell device 5 capable of supplying an electric current 1 from the methane or methanol 15 from the first unit A and an anode gas flow 6 comprising carbon dioxide, said fuel cell device being combined with a device 7 for capturing the carbon dioxide 17 included in the anode flow 6 and intended for the first unit A.
[0019] The installation according to the invention may include one or more of the following characteristics, taken in isolation or in any technically possible combination:
[0020] - the first unit is connected to the metropolitan electricity network and the second unit is not connected to the metropolitan electricity network;
[0021] - the first unit comprises an electrolyser capable of producing hydrogen from water and electricity, and a means of liquefying methane or methanol;
[0022] - the second unit comprises, upstream of the fuel cell device, a means for storing liquid methane or liquid methanol from the first unit and a means for gasifying the liquid methane or liquid methanol;
[0023] - the second unit comprises a means for liquefying carbon dioxide from the carbon dioxide capture device; - the second unit is chosen from a boat or a fixed or floating platform. The invention also relates to a method for producing electricity using an installation as defined above and comprising the following steps: a) On the first unit, a step of producing methane or methanol from hydrogen and carbon dioxide from the second unit, b) On the second unit, a step of producing electricity and an anode gas stream comprising carbon dioxide by means of the fuel cell device from methane or methanol from the first unit and c) On the second unit, a step of capturing carbon dioxide to form a gas stream of carbon dioxide used in step a) and an anode stream depleted in carbon dioxide.
[0024] The method according to the invention may comprise one or more of the following characteristics, taken in isolation or in any technically possible combination:
[0025] - the method comprises upstream of step a) a step of producing hydrogen by electrolysis, carried out on the first unit;
[0026] - the method comprises between steps a) and b):
[0027] - A step of liquefaction of the methanol or methane produced in step a), carried out on the first unit,
[0028] - A storage stage for liquefied methanol or liquefied methane, carried out on a second unit, and
[0029] - A gasification step of the stored methanol or stored methane, carried out on the second unit;
[0030] - the method comprises between steps b) and c) a step of cooling and condensing the anode flux comprising carbon dioxide so as to dry said anode flux;
[0031] - the method comprises downstream of step c) a step of recycling the anode flow depleted in carbon dioxide in the fuel cell device;
[0032] - the process comprises, downstream of step c), a step of liquefaction of the gaseous stream of carbon dioxide;
[0033] - in step c) the anodic flux is brought into contact with a liquid solvent capable of absorbing carbon dioxide to form the anodic flux depleted in carbon dioxide and a liquid bottom flux comprising the liquid solvent loaded with carbon dioxide.
[0034] [Fig 1] Figure 1 represents a diagram of the installation according to the invention.
[0035] By synthesis device is preferably meant a “synthesis reactor”. By “two separate industrial sites” is preferably meant two sites separated from each other by a distance greater than 30 km, preferably greater than 100 km, even more preferably a distance of several hundred kilometers.
[0036] Also, the invention consists of a coupling between a first unit for synthesizing a fuel, which in this case is methane or methanol, and a second unit for producing electricity.
[0037] Synthetic methanol can be produced by different methods:
[0038] - Thermocatalytic Methanation: hydrogen and CO2 are pressurized then mixed before being sent to a series of catalytic reactors to produce synthetic methane
[0039] - Methanation by Electrochemical Reduction: water and CO2 are injected into an electrolyzer to directly produce synthetic methane. Alternatively, this process can be done in two stages: a so-called co-electrolysis stage in which water and CO2 are transformed into CO and H2 in a SOEC, the CO and H2 then being transformed into CH4 via a thermocatalytic route.
[0040] - Biological methanation: methane synthesis by biological means, i.e. using micro-organisms. The H2 can be sent directly to a methanizer in order to have an in-situ transformation of CO2. According to an alternative method, a dedicated biological reactor is used, which is fed with H2 and CO2 in order to produce methane.
[0041] The synthesis of methanol from hydrogen and carbon dioxide is represented by three macroscopic reactions:
[0042] Reaction 1: CO2 + 3Hs — > CH3OH + H2O
[0043] Reaction 2: CO2 + H2 — > CO + H2O
[0044] Reaction 3: CO + 2H2— > CH3OH
[0045] CO2 reacts with hydrogen to produce methanol and water, via reaction 1. This is accompanied by reaction 2, the reverse water gas reaction (RWGS), which consumes the same reactants, but is not desired in our application. The production of CO by RWGS leads to the appearance of an additional route for the synthesis of methanol: by hydrogenation of CO (reaction 3).
[0046] Methanol synthesis is carried out on one or more types of solid catalysts, preferably copper-based catalysts. Among them, Cu / ZnO / Al2O3 is the classic catalyst due to its excellent activity as well as its low price compared to others. When copper is supported on alumina, the selectivity towards methanol is the highest, while the highest methanol yield was observed on zinc oxide. They concluded that alumina improves methanol selectivity because it facilitates the reduction of copper species that would be responsible for methanol synthesis.
[0047] The synthesis of methanol will preferably be carried out in a fixed-bed tubular reactor, preferably in a tubular reactor similar to that described in document FR3103714.
[0048] The principle of the process for producing methanol from CO2 is quite simple. The H2 / CO2 mixture, preferably preheated, is sent to the reactor, the outlet stream of which is directed to a separation section where the methanol (along with water and some small percentages of higher-order alcohols) is condensed. Unreacted gases are returned to the reactor to maximize yield, as conversion is often around 20%. The methanol is finally purified by distillation.
[0049] The synthesis of methane, called the Sabatier reaction (Sabatier 1902) is carried out from carbon dioxide and dihydrogen:
[0050] Reaction 4: CO2 + 4 H2 CH4 + 2 H2O
[0051] This reaction is carried out in the presence of a catalyst, preferably nickel. The conversion of CO2 to CH4 is negligible at temperatures below 200 °C. Methane synthesis is preferably carried out at a temperature between 250 and 700 °C.
[0052] Like the synthesis of methanol, the synthesis of methane will preferably be carried out in a fixed-bed tubular reactor, preferably in a tubular reactor similar to that described in document FR3103714.
[0053] The principle of the methane production process from CO2 is similar to that of methanol production. The H2 / CO2 mixture is sent to the reactor, whose outlet stream is directed to a separation section where the methane is condensed. Unreacted gases are returned to the reactor to maximize yield. The methanol is finally purified by distillation.
[0054] The fuel cell system consists of one or more solid oxide fuel cells (SOFCs). Each fuel cell is continuously supplied with the flow of methane or methanol injected at the anode system (partial reforming takes place before injection at the anodes) and with a gas flow rich in oxygen injected at the cathode system.
[0055] Depending on the case, the installation according to the invention may have one or more of the following characteristics:
[0056] - the first unit A is connected to the metropolitan electricity network and the second unit B is not connected to the metropolitan electricity network. As mentioned previously, as units not connected to the metropolitan electricity network, we can cite as examples units on aquatic sites (sea, lake or river), units located in rural areas not served by an electricity network, units located in island areas... and / or all mobile units;
[0057] - the first unit A and the second unit B are two land units;
[0058] - the first unit A is a fixed unit, preferably a land unit, and the second unit B is a mobile unit, preferably an aquatic unit;
[0059] - the second unit is chosen from a boat or a fixed or floating platform. A fixed platform is a platform anchored to the seabed. In the case of a boat, the electricity supplied by the fuel cell device can be used as motive power.
[0060] - the first unit A comprises an electrolyser 8 capable of producing hydrogen 2 from water 9 and electricity 10, and a means of liquefying methane or methanol 15. Preferably, the electricity will come from a renewable energy source. Preferably, the methane is liquefied through a series of cryogenic cycles. Alternatively, the methane can also be liquefied in an "open cycle", that is to say by passing the methane itself through compressors and coolers so as to subject it to expansion to generate the necessary cold.
[0061] - the second unit B comprises, upstream of the fuel cell device 5, a means 14 for storing liquid methane or liquid methanol from the first unit A and a means 11 for gasifying liquid methane or liquid methanol.
[0062] - the second unit B comprises a means 12 for liquefying the carbon dioxide 17 from the carbon dioxide capture device 7. The second unit will preferably comprise a compressor between the carbon dioxide capture device 7 and the liquefaction means 12. The liquefied carbon dioxide 16 can then be stored on the second unit B before being sent to the first unit A, then stored on this first unit A in a storage means 13 and finally used in the methane or methanol synthesis device 8.
[0063] - The gasification means 11 of liquid methane or liquid methanol and the liquefaction means 12 of carbon dioxide are combined into a single heat exchange device. The carbon dioxide transfers its heat to the liquid methane or liquid methanol and vice versa, thus the carbon dioxide is liquefied while the methane or methanol is gasified.
[0064] - the second unit comprises, upstream of the carbon dioxide capture device 7, a post-treatment, cooling and condensation device intended to cool and dry the anode gas flow 6 to form a dry anode flow.
[0065] - the carbon dioxide capture device 7 comprises: - an absorber intended to bring the dry anode flow into contact with a liquid solvent capable of absorbing carbon dioxide to form at the top of the absorber the anode flow depleted in carbon dioxide and at the bottom of the absorber a liquid bottom flow comprising the liquid solvent loaded with carbon dioxide,
[0066] - at least one heat exchanger system intended to heat the liquid foot flow to form a heated foot flow,
[0067] - a tank connected to said at least one heat exchange system intended to form at the top of the tank the stream of carbon dioxide and, at the bottom of the tank, a stream of partially regenerated liquid solvent intended to be injected into the absorber.
[0068] - The carbon dioxide capture device does not have a stripping column.
[0069] The electrolyser will preferably be powered by a carbon-free energy source, preferably a renewable energy source. In the electrolyser, at the anode, water (H20) is dissociated under the effect of the electric current, forming oxygen (02) and H+ ions; at the cathode, the H+ ions recombine and form hydrogen (H2). This hydrogen is called "green" when it is obtained from carbon-free energy.
[0070] The electrolyser will preferably be a proton exchange electrolyser (PEM) or a high temperature electrolyser (SOEC type) or Alkaline.
[0071] Preferably, the post-treatment, cooling and condensation device also makes it possible to convert at least a portion of the carbon monoxide present in the anode gas stream into dihydrogen and carbon dioxide, typically by reaction with water vapor. This conversion then makes it possible to limit the oxidation of the liquid solvent used in the carbon dioxide capture device by the oxidizing carbon monoxide molecules and to increase the carbon dioxide concentration in the anode gas stream in order to facilitate its capture in the capture device.
[0072] The installation according to the invention will preferably comprise a means for recovering a gas flow depleted in oxygen. This gas flow depleted in oxygen will be post-treated and / or discharged into the atmosphere.
[0073] The desulfurization step will not be necessary upstream of the fuel cell because the synthesis gases (methane or methanol) do not contain any.
[0074] The present invention also relates to a method for producing electricity at sea using an installation according to the invention and comprising the following steps: a) On the first unit A, a step of producing methane or methanol 15 from hydrogen 2 and carbon dioxide 4 from the second unit B, b) On the second unit B, a step of producing electricity 1 and an anode gas stream 6 comprising carbon dioxide by means of the fuel cell device from methane or methanol 15 from the first unit and c) On the second unit B, a step of capturing 7 carbon dioxide to form a gas stream of carbon dioxide 17 used in step a) and an anode stream depleted in carbon dioxide.
[0075] The method according to the invention may have one or more of the characteristics below:
[0076] - It comprises upstream of step a) a step of production of hydrogen by electrolysis 8, carried out on the first unit A,
[0077] - It includes between steps a) and b):
[0078] - A stage of liquefaction of the methanol or methane produced in stage a), carried out on the land unit,
[0079] - A storage stage 14 of liquefied methanol or liquefied methane, carried out on the offshore unit, and
[0080] - A gasification step 1 1 of the stored methanol or stored methane, carried out on the offshore unit.
[0081] - It comprises between steps b) and c) a step of cooling and condensing the anode flux comprising carbon dioxide so as to dry said anode flux;
[0082] - It comprises downstream of step c) a step of recycling the anode flow depleted in carbon dioxide in the fuel cell device;
[0083] - It comprises downstream of step c) a step 12 of liquefaction of the gaseous stream of carbon dioxide 17. Downstream of the capture device 7, the gaseous stream of carbon dioxide 17 is compressed to a pressure of between 15 and 40 bar, then cooled by heat exchange with the liquid methane or liquid methanol to a temperature of between -15 and -50°C before being expanded to reach the storage conditions of liquid CO2 (for example: 17 bar and -28°C). The liquid CO2 16 may initially be stored on the second unit then on the first unit in the storage means 13 before being used in the synthesis device 8 of methane or methanol;
[0084] - The gasification step 11 of methane or methanol is carried out by heat exchange with the thermal gas stream; - the anode flow depleted in carbon dioxide has a carbon dioxide content of 0% to 80% by volume, preferably of 20% to 70% by volume, even more preferably of 40% to 60% by volume;
[0085] - in step c) the anode flux is brought into contact with a liquid solvent capable of absorbing carbon dioxide to form the anode flux depleted in carbon dioxide and a liquid bottom flux comprising the liquid solvent loaded with carbon dioxide;
[0086] - the carbon dioxide absorbed in the liquid bottom stream is released by heating the liquid bottom stream to form part of the carbon dioxide stream used in step a) and a partially regenerated liquid solvent stream;
[0087] - before being injected into the fuel cell device 5, the methane or methanol is heated by heat exchange with the gaseous stream of carbon dioxide;
[0088] - at least 80% of the carbon dioxide produced during the operation of the process is recovered in the carbon dioxide gas stream, preferably at least 90% by mole, more preferably from 90% to 99% by mole.
[0089] Preferably, the installation according to the invention will further comprise a closed heat exchange circuit comprising a heat transfer fluid intended to be placed in heat exchange on the one hand with a liquid bottom flow comprising the liquid solvent loaded with carbon dioxide, at the level of said at least one heat exchanger system, and on the other hand with the anode gas flow and / or the cathode gas flow.
[0090] Advantageously, the methane or methanol introduced into the fuel cell device will be at a pressure between atmospheric pressure and 2 bars, preferably at a temperature between 300°C and 500°C.
[0091] The oxygen-rich gas stream typically has a dioxygen content of at least 10% by volume, preferably 15% to 25% by volume of dioxygen. Advantageously, the oxygen-rich gas stream is an air stream.
[0092] Preferably, the oxygen-rich gas stream is at a pressure between atmospheric pressure and 2 bars.
[0093] Preferably, the liquid solvent used in the capture device is chosen from aqueous amine solutions capable of adsorbing carbon dioxide.
[0094] Chemical absorption methods using aqueous amine solutions capable of absorbing carbon dioxide are well known to those skilled in the art and will not be further described here. Examples of aqueous amine solutions suitable for the invention include solutions composed of one or more of the following compounds: monoethanolamine, diethanolamine, N-methyldiethanolamine, piperazine, 2-Amino-2-methylpropan-1-ol, Bis(2-hydroxypropyl)amine, 1-methylpiperazine, dimethylaminoethanol.
[0095] A number of equipment and utility systems necessary for the proper operation of the absorption units are known to those skilled in the art and will therefore not be described further in the remainder of the description.
[0096] Upon contact with the dry anode flux, the liquid solvent absorbs the carbon dioxide present in the dry anode flux to form a liquid bottom flux consisting of the liquid solvent loaded with carbon dioxide, and at the top of the absorber 200, the anode flux depleted in carbon dioxide.
[0097] The carbon dioxide depleted anode flux typically comprises from 10% to 60% by volume of carbon dioxide CO2, preferably from 30% to 50% by volume.
[0098] The liquid bottom stream consisting of the liquid solvent loaded with carbon dioxide is then heated to form a preheated bottom stream. The preheated bottom stream 206 is then heated again so that the carbon dioxide absorbed in the liquid solvent is partially released in gaseous form. Typically, the preheated bottom stream is heated, preferably by heat exchange, to a temperature above 70°C, preferably above 80°C, in particular close to 90°C. The heated bottom stream is introduced into the flask to form, at the top of the flask, the carbon dioxide stream, and at the bottom of the flask, a stream of liquid solvent depleted in carbon dioxide.
[0099] The stream of liquid solvent depleted in carbon dioxide is then reinjected into the absorber for recycling.
[0100] The stream of liquid solvent depleted in carbon dioxide taken from the foot of the flask then includes the starting liquid solvent as well as a portion of the absorbed carbon dioxide which has not been released by the expansion in the flask 216.
[0101] Typically, at least 15% of the liquid solvent is still loaded with carbon dioxide, preferably at least 35%, more preferably 55 to 65%.
[0102] In other words, the stream of liquid solvent depleted in carbon dioxide has a carbon dioxide content greater than or equal to 0.1 mole of CO2 per mole of amine solvent on a dry basis, preferably from 0.15 to 0.4 mole of CO2 per mole of amine solvent on a dry basis, even more preferably from 0.30 to 0.35 mole of CO2 per mole of amine solvent on a dry basis.
[0103] Preferably, before being reinjected into the absorber, the carbon dioxide-depleted liquid solvent stream is cooled, preferably by heat exchange with the liquid bottom stream from the absorber.
[0104] The carbon dioxide-depleted liquid solvent stream may also undergo an additional cooling step before injection into the absorber, for example by passing through a heat exchanger, using an external refrigerant source.
[0105] In the solution proposed by the present invention, carbon circularity is implemented: the carbon dioxide produced by the fuel cell is reused in the methane or methanol synthesis device.
[0106] From this perspective, the main benefits are the reduction of the carbon footprint linked to the recycling of carbon dioxide. Since the quantities of CO2 required for methanation are significant and biogenic CO2 resources are limited, CO2 circularity makes it possible to reduce emissions from the chain.
Claims
CLAIMS 1. Electricity production installation (1), comprising two units, a first unit (A) and a second unit (B), located on two separate industrial sites with: - the first unit (A) comprising a synthesis device (8) capable of producing methane or methanol (15) from hydrogen (2) and carbon dioxide (4) from the second unit (B), and - the second unit (B) comprising a fuel cell device (5) capable of supplying an electric current (1) from the methane or methanol (15) from the first unit (A) and an anode gas flow (6) comprising carbon dioxide, said fuel cell device being combined with a device (7) for capturing the carbon dioxide (17) included in the anode flow (6) and intended for the first unit (A).
2. Electricity production installation according to claim 1, characterized in that the first unit (A) is connected to the metropolitan electricity network and the second unit (B) is not connected to the metropolitan electricity network.
3. Electricity production installation according to one of claims 1 or 2, characterized in that the first unit (A) comprises an electrolyzer (8) capable of producing hydrogen (2) from water (9) and electricity (10), and a means of liquefying methane or methanol (15).
4. Electricity production installation according to one of claims 1 to 3, characterized in that the second unit (B) comprises upstream of the fuel cell device (5) a means (14) for storing liquid methane or liquid methanol from the first unit (A) and a means (11) for gasifying liquid methane or liquid methanol.
5. Electricity production installation according to one of claims 1 to 4, characterized in that the second unit (B) comprises a means (12) for liquefying the carbon dioxide (17) coming from the carbon dioxide capture device (7).
6. Offshore electricity production installation according to one of claims 1 to 5, characterized in that the second unit (B) is chosen from a boat or a fixed or floating platform.
7. A method for producing electricity using an installation as defined in one of claims 1 to 6 and comprising the following steps: a) On the first unit (A), a step of producing methane or methanol (15) from hydrogen (2) and carbon dioxide (4) from the second unit (B), b) On the second unit (B), a step of producing electricity (1) and an anode gas stream (6) comprising carbon dioxide by means of the fuel cell device from the methane or methanol (15) from the first unit and c) On the second unit (B), a step of capturing (7) carbon dioxide to form a gas stream of carbon dioxide (17) used in step a) and an anode stream depleted in carbon dioxide.
8. Method for producing electricity according to claim 7, characterized in that it comprises upstream of step a) a step of producing hydrogen by electrolysis (8), carried out on the first unit (A).
9. Method for producing electricity according to one of claims 7 or 8, characterized in that it comprises between steps a) and b): - A step of liquefaction of the methanol or methane (15) produced in step a), carried out on the first unit (A), - A storage step (14) of liquefied methanol or liquefied methane, carried out on a second unit, and - A gasification step (1 1 ) of the stored methanol or stored methane, carried out on the second unit.
10. Method for producing electricity according to one of claims 7 to 9, characterized in that it comprises between steps b) and c) a step of cooling and condensing the anode flux comprising carbon dioxide so as to dry said anode flux.
11. Method for producing electricity according to one of claims 7 to 10, characterized in that it comprises downstream of step c) a step of recycling the anode flow depleted in carbon dioxide in the fuel cell device.
12. Method for producing electricity according to one of claims 7 to 11, characterized in that it comprises downstream of step c) a step of liquefaction (12) of the gaseous stream of carbon dioxide (17).
13. Method for producing electricity according to one of claims 7 to 12, characterized in that the anode flux depleted in carbon dioxide has a carbon dioxide content of 0% to 80% by volume, preferably of 20% to 70% by volume, even more preferably of 40% to 60% by volume.
14. Method for producing electricity according to one of claims 7 to 13, characterized in that in step c) the anode flux is brought into contact with a liquid solvent capable of absorbing carbon dioxide to form the anode flux depleted in carbon dioxide and a liquid bottom flux comprising the liquid solvent loaded with carbon dioxide.
15. Method for producing electricity according to one of claims 7 to 14, characterized in that at least 80% of the carbon dioxide produced during the operation of the method is recovered in the gaseous stream of carbon dioxide, preferably at least 90% by mole, more preferably from 90% to 99% by mole.