Method for accumulating and generating energy associated with oxygen combustion without emitting greenhouse gases

Abstract

The present invention provides a method for producing liquid carbon monoxide and liquid oxygen to be used in oxy-fuel combustion that generates carbon dioxide as a driving fluid from electricity and available carbon dioxide.

Description

Technical Field

[0001] The present invention relates to a method for accumulating and generating energy associated with oxy-fuel combustion without emitting greenhouse gases.

Background Art

[0002] There are multiple technologies for both power storage and generation.

[0003] Regarding storage, electrochemical technologies (batteries), mechanical technologies (flywheels, compressed air, high-altitude water storage), and thermodynamic technologies (liquefied gas (liquid air) technology called liquefied air energy storage (LAES)) are most well-known.

[0004] Instead, regarding energy generation, energy can be generated from fuel by performing oxy-fuel combustion such that the fuel and oxygen are converted to CO2 and water and removed from the system, either by isolating combustion CO2, using carbon recovery technology from combustion flue gas, or by combusting in a synthetic atmosphere consisting mainly of CO2 and oxygen.

[0005] The oxy-fuel combustion process is configured as an energy generation system and may be used to cover the peak of network demand, but it is not an energy storage system itself.

[0006] In the oxy-fuel combustion process, it is necessary to generate oxygen with a purity exceeding 90%, and for this purpose, a large amount of air needs to be compressed and purified. However, most of it is simply released into the atmosphere after the oxygen is extracted.

[0007] The process of separating oxygen from air is also costly. This is because advanced technical means for maximizing efficiency are required to avoid compressing a much larger amount of air than the amount necessary to obtain oxygen.

[0008] Typically, oxygen combustion plants are significantly disadvantaged by the operation of extracting oxygen from air and liquefying combustion CO2.

[0009] To date, the most efficient oxygen combustion cycles with complete CO2 separation are the Allam cycle and the Graz cycle. In these cases, the efficiency calculated with respect to the lower heating value of the fuel and the energy invested in the production of the combustion product (high-purity oxygen) corresponds to approximately 52%.

[0010] Also, in the Allam cycle, it is necessary to cool the recycled CO2 to a temperature not exceeding 16 °C, and an appropriate cold sink is required, but it should also be noted that it is not always available depending on the season, geographical location, and in some cases the availability of water areas.

[0011] In the oxygen combustion cycle, combustion CO2 is not released into the atmosphere. However, the problem of permanent storage of combustion CO2 remains. In used hydrocarbon wells, it is estimated that they are currently insufficient to accommodate all the CO2 produced in one year.

[0012] For these reasons, and also because these technologies tend to move problems over time rather than solve them, these technologies have not been developed.

[0013] On the other hand, liquefied air energy storage (LAES) consumes a significant amount of energy in the production of liquid air. The inventors of the present application estimate this energy to be 0.45 kwh / kg. Therefore, the amount of recoverable energy is severely limited. In fact, the efficiency of this type of demonstration plant does not exceed 15%.

[0014] The main factor for this is the fact that among the fluids available for the condensation / vaporization cycle that does not require gas storage, air needs to reach a low temperature, so the amount of energy required for condensation is very high, increasing the thermodynamic inefficiency of the process.

[0015] Patent Document 1 (Italian Patent Application Publication No. 202000023167, Saipem) discloses a combination of an oxygen combustion cycle and LAES energy storage technology.

[0016] Patent Document 2 (International Publication No. 2021 / 255578, Energy Dome) discloses a plant for generating and storing energy, in which a closed thermodynamic cycle and oxygen combustion technology are integrated.

[0017] Patent Document 3 (U.S. Patent Application Publication No. 2019 / 211715) discloses the separation of hydrogen and carbon monoxide from a gaseous fuel, a combustor supplied with carbon monoxide, and a carbon dioxide separation unit for preparing supercritical carbon dioxide.

Prior Art Documents

Patent Documents

[0018]

Patent Document 1

Patent Document 2

Patent Document 3

Summary of the Invention

[0019] [Summary of the Invention] The inventor of the present application has surprisingly developed a method that enables available surplus power to be stored in the form of liquefied gas (particularly, carbon monoxide and oxygen) so that it can be used later in an oxygen combustion cycle involving energy production by integrating the technologies of oxygen combustion, dry carbon dioxide electrolysis, and energy storage in a cooling form.

[0020] [Object of the Present Invention] For a first object, the present invention provides a method for generating and storing energy, generating carbon monoxide and ultra-pure oxygen, and further utilizing carbon dioxide.

[0021] For a second object, the present invention provides a method for generating electric power.

[0022] The present invention comprehensively provides a method for generating and storing energy, generating carbon monoxide and ultra-pure oxygen, and further utilizing carbon dioxide to generate liquid carbon dioxide.

[0023] In certain embodiments, the method of the present invention enables the management (peak shaving) of energy peaks and shortages. BRIEF DESCRIPTION OF THE DRAWINGS

[0024]

Figure 1

Figure 2

Figure 3

Figure 4

Figure 5

[0025] For the purposes of the present invention, the heat exchange performed in the exchangers (E1, E2, E3, E4, En) is performed by an external fluid (preferably air, water, etc.).

[0026] In contrast, the heat exchangers (designated by the reference numeral "EXn") involve two flows within the circuit described in the present invention.

[0027] According to a first object of the present invention, there is provided a method for generating and storing energy, generating carbon monoxide and ultra-pure oxygen, and further utilizing carbon dioxide.

[0028] The carbon dioxide can be generated, for example, by an industrial process or a purification process, or by an environmental process, and the emission of carbon dioxide into the atmosphere can be avoided.

[0029] According to the method of the present invention, it is also possible to manage the peak and shortage (peak shaving) of energy.

[0030] In particular, the energy storage is obtained by storing at least partially liquefied carbon monoxide and oxygen and a cooled fluid.

[0031] In particular, such a method of the present invention comprises a storage step (A) and a generation step (B).

[0032] For the purpose of the present invention, the storage step (A) is a step that enables the generation of a flow of carbon monoxide (CO) and oxygen and, optionally, also a flow of a cooled fluid.

[0033] In particular, in the storage step (A), carbon monoxide (CO) and oxygen are generated by the electrolysis of carbon dioxide.

[0034] More specifically, such a storage step (A) is performed using the surplus current available in the network.

[0035] The term "available surplus" as used herein means an amount of electricity that is more than the required amount.

[0036] According to one aspect of the present invention, carbon monoxide and oxygen may be stored in at least partially liquefied form.

[0037] For the purposes of the present invention, referring to the method shown in FIG. 2, the accumulation step (A) comprises the following sub-steps. (A1) Electrolyzing a stream 3 of appropriately heated carbon dioxide to obtain an initial carbon monoxide stream c1 and an initial oxygen stream o1 (electrolysis step). (A2) Obtaining a stream c17 of at least partially liquefied carbon monoxide from the initial carbon monoxide stream c1. (A3) Obtaining a stream o10 of at least partially liquefied oxygen from the initial oxygen stream o1.

[0038] Step (A1) (electrolysis step) is carried out in an electrolyzer (electrolysis cell) EL from a stream 3 of appropriately heated carbon dioxide. The stream 3 of appropriately heated carbon dioxide is obtained from liquid carbon dioxide and, optionally, also from gaseous carbon dioxide (carbonic acid gas).

[0039] Specifically, in step (A0a), an initial liquid carbon dioxide stream 1 is drawn from a liquid carbon dioxide tank TCO2l and heated by heat exchange in a first section (first sector) EX1a of a first heat exchanger to obtain a heated carbon dioxide stream 2. In step (A0b), the heated carbon dioxide stream 2 is further heated by heat exchange in a second heat exchanger EX2 to obtain a stream 3 of appropriately heated carbon dioxide.

[0040] According to one aspect of the present invention, step (A0a') may be carried out. In step (A0a'), a second initial liquid carbon dioxide stream 1'' is fed into a pump P to obtain a second fed liquid carbon dioxide stream 2''. The fed liquid carbon dioxide stream 2'' is subsequently heated by heat exchange in a first section (first sector) EX1a of a first heat exchanger. Thereby, a second heated carbon dioxide stream 3'' is obtained. The second heated carbon dioxide stream 3'' can be stored in a special storage well.

[0041] According to one aspect of the present invention, step (A0b') may be performed. In step (A0b'), the flow 1' of initial gaseous carbon dioxide (initial carbon dioxide gas) is heated in the second heat exchanger EX2 to obtain a heated gaseous carbon dioxide (carbon dioxide gas) flow 2'. The heated gaseous carbon dioxide (carbon dioxide gas) flow 2' is merged into the appropriately heated carbon dioxide flow 3.

[0042] According to one aspect of the present invention, the electrolytic cell (electrolysis cell) EL is preferably a solid oxide electrolysis cell (SOEC).

[0043] As described above, the following two flows are obtained from step (A1). (1) A flow containing carbon monoxide and carbon dioxide (hereinafter referred to as "initial carbon monoxide flow c1") (2) A flow containing 99.9% pure oxygen (hereinafter referred to as "initial oxygen flow o1")

[0044] According to a specific embodiment of the present invention, step (A1) may include a step of generating electric power by utilizing heat generated by the Joule effect from the electrolytic cell (electrolysis cell) EL, as described later.

[0045] The step (A2) of obtaining a carbon monoxide flow c17 that is at least partially liquefied from the initial carbon monoxide flow c1 includes the following further sub-steps. (A2a) A step of obtaining a carbon monoxide flow c6 to be purified. (A2b) A step of obtaining a flow c12 mainly composed of carbon monoxide and steam, a recycled carbon monoxide flow c11, and a recycled gas flow cr. (A2c) A step of obtaining a dehydrated carbon monoxide flow c13. (A2d) A step of obtaining a carbon monoxide flow c17 that is at least partially liquefied.

[0046] In particular, step (A2a) includes the following further sub-steps. (A2a1) Obtaining a first portion c2 of the initial carbon monoxide stream and a second portion c2' of the initial carbon monoxide stream. (A2a2) Obtaining a cooled first portion c3 of the initial carbon monoxide stream by cooling the first portion c2 of the initial carbon monoxide stream in a third heat exchanger EX3a. (A2a3) Obtaining a cooled second portion c3' of the initial carbon monoxide stream by cooling the second portion c2' of the initial carbon monoxide stream in another third heat exchanger EX3b. (A2a4) Obtaining a cooled and merged carbon monoxide stream c4 by merging the cooled first portion c3 of the initial carbon monoxide stream and the cooled second portion c3' of the initial carbon monoxide stream. (A2a5) In a first compressor cC1, compressing the cooled and merged carbon monoxide stream c4 to obtain a compressed carbon monoxide stream c5, and in a first exchanger cE1, cooling the cooled and merged carbon monoxide stream c4 to obtain a carbon monoxide stream c6 to be purified.

[0047] For the purpose of the present invention, step (A2a5) may be repeated, if necessary, until the conditions required for the next step (A3) are achieved.

[0048] Advantageously, step (A2a5) makes it easier to separate carbon monoxide from carbon dioxide, and the heat exchange profile (heat exchange performance) in the carbon monoxide liquefaction process can be improved.

[0049] In one embodiment of the present invention, the initial carbon monoxide stream c1 is sent exclusively to the third heat exchanger EX3 without being separated.

[0050] For the purpose of the present invention, sub-step (A2b) comprises the following further sub-steps. (A2b1) In the first purification column (the first column CL1), perform the first purification on the flow c6 of carbon monoxide to be purified, to obtain a partially purified carbon monoxide flow c7, a carbon monoxide flow c8 from which the physical solvent is separated (released), and a recycled carbon monoxide flow c11. (A2b2) In the second purification column (the second column CL2), perform the second purification on the partially purified carbon monoxide flow c7, to obtain a flow c12 mainly composed of carbon monoxide and steam, a flow m2 to be regenerated, and a recycled gas flow cr.

[0051] For the purpose of the present invention, the flow c12 mainly composed of carbon monoxide and steam has a carbon dioxide concentration of less than 500 ppm (mol / mol), preferably less than 50 ppm (mol / mol).

[0052] More specifically, the step (A2b1) comprises the following steps. (p1) A step of washing with a physical solvent. (p2) By separation from the physical solvent, obtain a regenerated physical solvent flow s9 and a carbon monoxide flow c8 from which the physical solvent is separated. (p3) By compression and cooling, obtain a flow c9 in which the physical solvent is separated and compressed, and a flow c10 in which the physical solvent is separated and compressed and cooled. (p4) By dehydration in the first dehydration unit cDU1, obtain a recycled carbon monoxide flow c11.

[0053] For the purpose of the present invention, the recycled flow of the recycled carbon monoxide flow c11 contains both carbon monoxide and carbon dioxide (for the electrolytic cell (electrolytic cell) EL). The recycled carbon monoxide flow c11 is combined with a suitably heated carbon dioxide flow 3, thereby generating a further suitably heated carbon dioxide flow 3'. The further suitably heated carbon dioxide flow 3' is sent to the above step (A1) and used as the suitably heated carbon dioxide flow 3 in step (A1).

[0054] More specifically, the step (A2b2) comprises the following steps. (p1’) Expanding the flow m2 of the object to be recycled in the expander mEK of the flow of the reaction product of the object to be recycled to obtain the expanded flow m3 of the reaction product of the object to be recycled, optionally generating electric power while doing so. (p2’) Heating the expanded flow m3 of the reaction product of the object to be recycled in the heat exchanger mEX1 of the flow of the reaction product of the object to be recycled to obtain the expanded and heated flow m4 of the reaction product of the object to be recycled and sending it to the regeneration column (third column) CL3. (p3’) Obtaining a flow m5 of the basic aqueous solution from the bottom of the regeneration column CL3, obtaining a flow h1 of carbon dioxide and water, and obtaining a gas flow for forming a recycle gas flow cr from the flow h1 of carbon dioxide and water.

[0055] For the purpose of the present invention, the recycle gas flow cr merges with the carbon monoxide flow c8 from which the physical solvent has been separated (released).

[0056] Also, by step (p3’), a flow m8 to be heated may also be obtained, which is directed towards the reboiler vEX1 of the regeneration column (third column) CL3. The heated flow m9 discharged from the reboiler vEX1 of the regeneration column (third column) CL3 is sent back to the regeneration column (third column) CL3.

[0057] According to an embodiment of the present invention, the reboiler vEX1 of the regeneration column (third column) CL3 is arranged within a Rankine cycle as described below.

[0058] For the purpose of the present invention, the step (A2c) comprises performing a dehydration step on the flow c12 mainly composed of carbon monoxide and steam in the second dehydration unit cDU2 to obtain a dehydrated carbon monoxide flow c13.

[0059] The second dehydration unit cDU2 preferably operates by means of a molecular sieve.

[0060] For the purposes of the present invention, step (A2d) comprises the following further sub-steps. (A2d1) Performing a first cooling step on the stream c13 of dehydrated carbon monoxide to obtain a stream c14 of partially cooled and dehydrated carbon monoxide. (A2d2) Performing a second cooling step on the stream c14 of partially cooled and dehydrated carbon monoxide to obtain a stream c15 of cooled and dehydrated carbon monoxide. (A2d3) Performing a third cooling step on the stream c15 of cooled and dehydrated carbon monoxide to obtain a stream c16 of further cooled and dehydrated carbon monoxide. (A2d4) By expanding in a first expander cEK1, expanding the stream c16 of further cooled and dehydrated carbon monoxide, optionally while generating electric power, to obtain a stream c17 of at least partially liquefied carbon monoxide, wherein the stream c17 of at least partially liquefied carbon monoxide can be stored in a liquid carbon monoxide tank TCOl.

[0061] For the purposes of the present invention, the first cooling step in step (A2d1) is performed in a first section EX1a of a first heat exchanger.

[0062] For the purposes of the present invention, the second cooling step in step (A2d2) is performed in a second section EX1b of the first heat exchanger.

[0063] For the purposes of the present invention, the third cooling step in step (A2d3) is performed in a third section EX1c of the first heat exchanger.

[0064] The heat exchange in step (A2d) is also effected, as will be described hereinafter, by heat exchange with a refrigerant circulating in a refrigerant circuit.

[0065] As described above, from the electrolysis step (A1), a flow o1 of initial oxygen is also obtained. From the flow o1 of initial oxygen, a flow o10 of at least partially liquefied oxygen is obtained according to step (A3).

[0066] For the purposes of the present invention, the step (A3) comprises the following further sub-steps. (A3a) Obtaining a first part o2 of the flow of initial oxygen and a second part o2' of the flow of initial oxygen. (A3b) Cooling the first part o2 of the flow of initial oxygen in a third heat exchanger EX3a to obtain a cooled first part o3 of the flow of initial oxygen. (A3c) Cooling the second part o2' of the flow of initial oxygen in another third heat exchanger EX3b to obtain a cooled second part o3' of the flow of initial oxygen. (A3d) Combining the cooled first part o3 of the flow of initial oxygen and the cooled second part o3' of the flow of initial oxygen to obtain a cooled and combined flow o4 of oxygen. (A3e) Compressing the cooled and combined flow o4 of oxygen with an oxygen compressor oC1 to obtain a compressed flow o5 of oxygen, and cooling the compressed flow o5 of oxygen in an oxygen exchanger oE (oE1) to obtain a compressed and cooled flow o6 of oxygen. (A3f) Cooling the compressed and cooled flow o6 of oxygen to obtain a flow o10 of at least partially liquefied oxygen, and enabling the flow o10 of at least partially liquefied oxygen to be stored in a liquid oxygen tank TO2l.

[0067] For the purposes of the present invention, the step (A3f) further comprises the following steps. (A3f1) Performing a first cooling step on the compressed and cooled flow o6 of oxygen to obtain a flow o7 of oxygen at a further first cooling level. (A3f2) Performing a second cooling step on the flow o7 of oxygen at the further first cooling level to obtain a flow o8 of oxygen at a further second cooling level. Step of obtaining a further third cooling level oxygen stream o9 by performing a third cooling process on the oxygen stream o8 at the further second cooling level. (A3f4) In the first oxygen expander oEK1, while generating power, for example, expanding the oxygen stream o9 at the further third cooling level to obtain an at least partially liquefied oxygen stream o10 and storing it in the liquid oxygen tank TO2l.

[0068] In one embodiment of the present invention, the initial oxygen stream o1 is sent exclusively to the third heat exchanger EX3 without being separated.

[0069] For the purpose of the present invention, step (A3e) may be repeated as necessary until the conditions required for the next step (A3f) are obtained.

[0070] For the purpose of the present invention, the first cooling process in step (A3f1) is performed in the first section EX1a of the first heat exchanger.

[0071] For the purpose of the present invention, the second cooling process in step (A3f2) is performed in the second section EX1b of the first heat exchanger.

[0072] For the purpose of the present invention, the third cooling process in step (A3f3) is performed in the third section EX1c of the first heat exchanger.

[0073] The heat exchange between step (A3b) and step (A3c) is also performed by heat exchange with a refrigerant fluid outside the process (for example, air or water).

[0074] According to a preferred embodiment, the heat exchange between step (A3b) and step (A3c) is performed by heat exchange with a flow that operates in a Rankine cycle as described below.

[0075] The heat exchange in step (A3f) is also performed by heat exchange with a refrigerant fluid circulating in a refrigerant fluid cycle, as described later.

[0076] According to one aspect of the present invention, the refrigerant fluid may be hydrogen, helium, or nitrogen.

[0077] In particular, the circuit of the refrigerant fluid includes a first refrigerant fluid flow f1. The first refrigerant fluid flow f1 is further subjected to the following steps. (I) A step of obtaining a second refrigerant fluid flow f2 by cooling the first refrigerant fluid flow f1. (II) A step of obtaining a third refrigerant fluid flow f3 by further cooling the second refrigerant fluid flow f2 in the first refrigerant fluid exchanger fE1. (III) A step of obtaining a fourth refrigerant fluid flow f4 by cooling the third refrigerant fluid flow f3 in the first heat exchange step. (IV) A step of obtaining a fifth refrigerant fluid flow f5 by cooling the fourth refrigerant fluid flow f4 in the second heat exchange step. (V) A step of obtaining a sixth refrigerant fluid flow f6 by cooling the fifth refrigerant fluid flow f5 in the third heat exchange step. (VI) A step of obtaining a seventh refrigerant fluid flow f7 by expanding the sixth refrigerant fluid flow f6 with the first refrigerant fluid expander fEK1, for example, while generating electric power. (VII) A step of obtaining an eighth refrigerant fluid flow f8 by heating the seventh refrigerant fluid flow f7 in the first heat exchange step. (VIII) A step of obtaining a ninth refrigerant fluid flow f9 by heating the eighth refrigerant fluid flow f8 in the second heat exchange step. (IX) A step of obtaining a tenth refrigerant fluid flow f10 by heating the ninth refrigerant fluid flow f9 in the third heat exchange step. (X) A step of obtaining an eleventh refrigerant fluid flow f11 by compressing the tenth refrigerant fluid flow f10, and obtaining a twelfth refrigerant fluid flow f12 by cooling the eleventh refrigerant fluid flow f11 with the first refrigerant fluid exchanger fE1. (XI) Obtaining the flow f1 of the first refrigerant fluid by compressing the flow f12 of the twelfth refrigerant fluid by the second compression fC2 of the refrigerant fluid.

[0078] For the purpose of the present invention, step (X) may be repeated one or more times as necessary.

[0079] According to an embodiment of the present invention, a further fourth flow f4' is obtained as a flow portion of the refrigerant fluid from the flow f4 of the fourth refrigerant fluid. The further fourth flow f4' is expanded by the second refrigerant fluid expander fEK2 to obtain a further fifth flow f5'. The further fifth flow f5' is subjected to a heat exchange process in step (VIII*) similar to step (VIII) described above to obtain a further sixth flow f6'. The further sixth flow f6' is further heated in a heat exchange process in step (IX*) similar to step (IX) described above to obtain a further seventh flow f7'. The further seventh flow f7' merges with the flow f10 of the tenth refrigerant fluid.

[0080] For the purpose of the present invention, the cooling in step (I) is performed by heat exchange in the second heat exchanger EX2.

[0081] For the purpose of the present invention, the cooling in step (III), the heating in step (IX), and the heating in step (IX*) are performed by heat exchange in the first section EX1a of the first heat exchanger.

[0082] For the purpose of the present invention, the cooling in step (IV), step (VIII), and step (VIII*) are performed by heat exchange in the second section EX1b of the first heat exchanger.

[0083] For the purpose of the present invention, the cooling in step (V) and the heating in step (VII) are performed by heat exchange in the third section EX1c of the first heat exchanger.

[0084] As described above, in a specific embodiment of the present invention, step (A1) may include step (A1') of generating electric power by using heat generated by the Joule effect from an electrolytic cell (electrolytic cell).

[0085] More specifically, the step (A1') includes heating a fluid by heat exchange with the flow c1 of initial carbon monoxide or a part thereof (first part c2, second part c2'), and / or by heat exchange with the flow o1 of initial oxygen or a part thereof (first part o2, second part o2').

[0086] After each heating step, the heated fluid is subjected to expansion with electric power generation.

[0087] For the purpose of the present invention, the step (A1') may be a step within a Rankine cycle.

[0088] In one embodiment of the present invention, the Rankine cycle is a steam cycle.

[0089] In a specific embodiment of the present invention, the Rankine cycle includes subjecting a first steam flow v1 to the following steps. (R1) A step of obtaining a second steam flow v2 by heating the first steam flow v1. (R2) A step of obtaining a third steam flow v3 while generating electric power by expanding the second steam flow v2 in a first expander vEK1 of the Rankine cycle. (R3) A step of obtaining a fourth steam flow v4 by further heating the third steam flow v3. (R4) A step of obtaining a fifth steam flow v5 by further expanding the fourth steam flow v4 in a second expander of the Rankine cycle. (R5) A step of obtaining a condensed sixth steam flow v6 by cooling the fifth steam flow v5 in a first exchanger vE1 of the Rankine cycle. Step of obtaining a condensed seventh vapor flow v7 by feeding a sixth vapor flow v6 into a first pump vP1 of a Rankine cycle. (R7) Step of obtaining the first vapor flow v1 by feeding the seventh vapor flow v7 into a second pump vP2 of the Rankine cycle.

[0090] For the purpose of the present invention, a further fifth vapor flow v5' is obtained from a second expander vEK2 of the Rankine cycle. The further fifth vapor flow v5' is cooled in a specific heat exchanger (reboiler vEX1) of the Rankine cycle, whereby a further sixth vapor flow v6' (actually, a condensed vapor flow) is obtained. The further sixth vapor flow v6' is further cooled in a second exchanger vE2 of the Rankine cycle, whereby a condensed further seventh vapor flow v7' is obtained. The further seventh vapor flow v7' is combined with the seventh vapor flow v7 and then sent to the second pump vP2.

[0091] For the purpose of the present invention, step (R1) is performed by heat exchange with a second portion o2' of the initial oxygen flow and heat exchange with a second portion c2' of the initial carbon monoxide flow in another third heat exchanger EX3b.

[0092] For the purpose of the present invention, step (R3) is performed by heat exchange with a first portion o2 of the initial oxygen flow and heat exchange with a first portion of the flow in which the initial carbon dioxide and the initial carbon monoxide are mixed (a first portion c2 of the initial carbon monoxide flow) in a third heat exchanger EX3a.

[0093] Regarding a specific exchanger (reboiler vEX1) of the Rankine cycle, it is a boiler (vE1) of a regeneration column (third column) CL3, and as described above, it heats a flow m8 to be heated and partially vaporizes it.

[0094] Next, a specific embodiment of step (A2b1) will be described. In step (A2b1), a stream c7 of partially purified carbon monoxide, a stream c8 of carbon monoxide from which the physical solvent has been separated (released), and a recycled stream c11 of carbon monoxide are obtained.

[0095] Specifically, inside the first column CL1, a stream s1 of the initial physical solvent comes into countercurrent contact with a stream c6 of carbon monoxide to be purified, whereby a stream c7 of partially purified carbon monoxide is obtained from the head portion of the first column CL1.

[0096] From the bottom of the first column CL1, a stream s2 of a physical solvent and carbon dioxide containing a certain amount of carbon monoxide is obtained. The stream s2 of the physical solvent and carbon dioxide is expanded in the first physical solvent expander sEK1, for example, with power generation. Thereby, an expanded stream s3 of the physical solvent, carbon monoxide, and carbon dioxide is obtained.

[0097] The expanded stream s3 of the physical solvent, carbon monoxide, and carbon dioxide releases a part of carbon monoxide and carbon dioxide by the regenerated physical solvent washing stream s12 in the solvent separator sS and in the solvent column sC. Thereby, a separated stream s7 (liquid) of the physical solvent and a stream s4 (gas) mainly composed of carbon monoxide are obtained.

[0098] The stream s4 mainly composed of carbon monoxide is compressed by the first compressed solvent sC1, whereby a stream s5 mainly composed of compressed carbon monoxide is obtained. The stream s5 mainly composed of compressed carbon monoxide is cooled in the first solvent exchanger sE1, whereby a stream s6 mainly composed of carbon monoxide returning to the first column CL1 is obtained.

[0099] The separated stream s7 of the physical solvent is expanded in the second solvent expander sEK2, whereby a separated stream s8 of the physical solvent is obtained. The separated stream s8 of the physical solvent is sent to the first separator S1, and from the first separator S1, a stream c8 of carbon monoxide from which the aforementioned physical solvent has been separated (released) and a partially regenerated stream s9 of the physical solvent are obtained.

[0100] The flow s9 of the partially regenerated physical solvent is fed by the first solvent pump sP1, whereby a flow s10 of the solvent that is partially regenerated and fed is obtained. The flow s10 of the solvent that is partially regenerated and fed is heated in the first solvent exchanger sE1, whereby a flow s11 of the regenerated physical solvent at room temperature is obtained. The first portion s12 of the flow of the regenerated physical solvent is sent to the solvent column sC as the regenerated physical solvent, and the second portion s13 of the flow of the regenerated physical solvent is fed by the second solvent pump sP2, whereby a flow s1 of the initial physical solvent is obtained.

[0101] For the purpose of the present invention, examples of the physical solvent involved in the purification process in the first column CL1 include Selectisol, Rectisol, methanol, and the like.

[0102] Next, a specific embodiment of step (A2b2) will be described. By step (A2b2), a flow c12 mainly composed of carbon monoxide and steam, a flow m2 to be regenerated, and a flow cr of recycled gas are obtained.

[0103] In particular, a flow c7 (gaseous) of partially purified carbon monoxide obtained from the head portion of the first column CL1 comes into countercurrent contact with a flow m1 (liquid) of a basic solution in the second column CL2.

[0104] For the purpose of the present invention, the basic solution may be an aqueous amine solution (for example, methyl ethyl amine (MEA) or a sodium bicarbonate solution).

[0105] As a result, a flow m2 of the reaction product solution is obtained from the bottom of the second column CL2. The flow m2 of the reaction product solution is expanded by an expander mEK of the flow of the reaction product to be regenerated, whereby an expanded flow m3 of the reaction product solution to be regenerated is obtained. Next, the expanded flow m3 of the reaction product solution to be regenerated is heated by heat exchange in a heat exchanger mEX1 (basic solution heat exchanger), whereby an expanded and heated flow m4 of the reaction product to be regenerated is obtained.

[0106] The expanded and heated flow m4 of the reaction product to be regenerated is sent to a regeneration column CL3, and from the regeneration column CL3, a flow m5 of the basic solution on the bottom side and a flow h1 of carbon dioxide and water on the head part side are obtained.

[0107] The flow m5 of the basic solution on the bottom side is cooled by heat exchange in a heat exchanger mEX1 (basic solution heat exchanger), whereby a cooled flow m6 of the basic solution on the bottom side is obtained. The cooled flow m6 of the basic solution on the bottom side is sent by a pump mP of the flow of the basic solution on the bottom side, whereby a cooled and sent flow m7 of the basic solution on the bottom side is obtained. The cooled and sent flow m7 of the basic solution on the bottom side is further cooled by a basic solution exchanger mE, whereby a flow m1 of the liquid basic solution is obtained.

[0108] The flow h1 of carbon dioxide and water on the head part side is cooled by a regeneration column exchanger hE, whereby a flow h2 of carbon dioxide and partially condensed water is obtained. From the flow h2 of carbon dioxide and partially condensed water, a flow h3 of the liquid on the bottom side is obtained in a regeneration column separator hS.

[0109] After the flow h3 of the liquid on the bottom side is replenished with a flow of water (make-up water in the illustrated example), it is sent by a regeneration column pump hP, and the sent reflux flow h4 is sent to the head part of the regeneration column CL3.

[0110] Instead, a recycle gas stream cr is obtained from the head portion of the regeneration column separator hS. The recycle gas stream cr merges with the carbon monoxide stream c8 from which the physical solvent has been separated (released), as described above.

[0111] According to an alternative embodiment of the present invention shown in FIG. 3, for example, after a carbon monoxide stream c17 that has been at least partially liquefied in step (A2d4) is obtained, the at least partially liquefied carbon monoxide stream c17 is subjected to the following steps.

[0112] In particular, in the first separator cS1, a first bottom-side liquid stream c18 and a first head-side gaseous stream c24 are separated from the at least partially liquefied carbon monoxide stream c17.

[0113] The first bottom-side liquid stream c18 is expanded by an expansion valve cV, thereby generating a first bottom-side expanded gaseous stream c19. From the first bottom-side expanded gaseous stream c19, a second bottom-side liquid stream c20 stored in the liquid carbon monoxide tank cTCOl and a second head-side gaseous stream c21 are separated in the second separator cS2.

[0114] The second head-side gaseous stream c21 is compressed by a third carbon monoxide compressor cC3 to obtain a second head-side compressed gaseous stream c22. The second head-side compressed gaseous stream c22 is cooled in a third carbon monoxide exchanger cE3, thereby obtaining a second head-side cooled and compressed stream c23. The second head-side cooled and compressed stream c23 merges with the dehydrated carbon monoxide stream c13.

[0115] In particular, the above compression and cooling can be repeated one or more times as necessary.

[0116] The first head-side gaseous stream c24 is subjected to a heating step (A2e). The heating step (A2e) comprises the following further sub-steps. (A2e1) Performing the first heating to obtain a gaseous flow c25 on the first head portion side at the first heating level. (A2e2) Performing the second heating to obtain a gaseous flow c26 on the second head portion side at the second heating level. (A2e3) Performing the third heating to obtain a gaseous flow c27 on the third head portion side at the third heating level, and the gaseous flow c27 on the third head portion side merges with the gaseous flow c21 on the second head portion side.

[0117] For the purpose of the present invention, step (A2e1) is performed in the third section EX1c of the first heat exchanger.

[0118] For the purpose of the present invention, step (A2e2) is performed in the second section EX1b of the first heat exchanger.

[0119] For the purpose of the present invention, step (A2e3) is performed in the first section EX1a of the first heat exchanger.

[0120] According to another embodiment of the present invention, after a flow o10 of oxygen that is at least partially liquefied is obtained in step (A3f), the flow o10 of oxygen that is at least partially liquefied is subjected to the following further steps.

[0121] In particular, in the first separator oS1, a first bottom-side liquid flow o11 and a first head-side gaseous flow o17 are separated from the flow o10 of oxygen that is at least partially liquefied.

[0122] The first bottom-side liquid flow o11 is expanded by an expansion valve oV, thereby generating a first bottom-side expanded gaseous flow o12. From the first bottom-side expanded gaseous flow o12, a second bottom-side liquid flow o13 stored in a liquid oxygen tank cTO2l and a second head-side gaseous flow o14 are separated in a second separator oS2.

[0123] The gaseous flow o14 on the second head portion side is compressed by the second oxygen compressor oC2, thereby obtaining a compressed gaseous flow o15 on the second head portion side. The compressed gaseous flow o15 on the second head portion side is cooled by the second oxygen exchanger oE2, thereby obtaining a compressed and cooled flow o16 on the second head portion side. The compressed and cooled flow o16 on the second head portion side is merged into the compressed and cooled oxygen flow o6.

[0124] In particular, the above compression and cooling may be repeated one or more times as necessary.

[0125] The gaseous flow o17 on the first head portion side is subjected to a heating step (A3g). The heating step (A3g) includes the following further sub-steps. (A3g1) A step of obtaining a gaseous flow o18 on the first head portion side at a first heating level by performing a first heating. (A3g2) A step of obtaining a gaseous flow o19 on the first head portion side at a second heating level by performing a second heating. (A3g3) A step of obtaining a gaseous flow o20 on the first head portion side at a third heating level by performing a third heating, and the gaseous flow o20 on the first head portion side is merged into the gaseous flow o14 on the second head portion side.

[0126] For the purpose of the present invention, step (A3g1) is performed in the third section EX1c of the first heat exchanger.

[0127] For the purpose of the present invention, step (A3g2) is performed in the second section EX1b of the first heat exchanger.

[0128] For the purpose of the present invention, step (A3g3) is performed in the first section EX1a of the first heat exchanger.

[0129] In particular, the heat exchanges in steps (A2e) and (A3g) are also carried out by heat exchange with a refrigerant fluid circulating in another refrigerant fluid circuit, as described below.

[0130] In particular, the other refrigerant fluid circuit includes a flow f'1 of another first refrigerant fluid. The flow f'1 of the other first refrigerant fluid is subjected to the following steps. (I') Obtaining a flow f'2 of another second refrigerant fluid by cooling the flow f'1 of the other first refrigerant fluid. (II') Obtaining a flow f'3 of another third refrigerant fluid by further cooling the flow f'2 of the other second refrigerant fluid in another first refrigerant fluid exchanger f'E1. (III') Obtaining a flow f'4 of another fourth refrigerant fluid by cooling the flow f'3 of the other third refrigerant fluid in a first heat exchange step. (IV') Obtaining a flow f'5 of another fifth refrigerant fluid by cooling the flow f'4 of the other fourth refrigerant fluid in a second heat exchange step. (V') Obtaining a flow f'6 of another sixth refrigerant fluid by cooling the flow f'5 of the other fifth refrigerant fluid in a third heat exchange step. (VI') Obtaining a flow f'7 of another seventh refrigerant fluid, for example with power generation, by expanding the flow f'6 of the other sixth refrigerant fluid in another first refrigerant fluid expander f'EK1. (VII') Obtaining a flow f'8 of another eighth refrigerant fluid by heating the flow f'7 of the other seventh refrigerant fluid in a first heat exchange step. (VIII') Obtaining a flow f'9 of another ninth refrigerant fluid by heating the flow f'8 of the other eighth refrigerant fluid in a second heat exchange step. (IX') Obtaining a flow f'10 of another tenth refrigerant fluid by heating the flow f'9 of the other ninth refrigerant fluid in a third heat exchange step. (X’) By compressing the flow f’10 of the other tenth refrigerant fluid, a flow f’11 of another eleventh refrigerant fluid is obtained, and by cooling the flow f’11 of the another eleventh refrigerant fluid in the first refrigerant fluid exchanger f’E1, a flow f’12 of another twelfth refrigerant fluid is obtained. (XI’) By compressing the flow f’12 of the another twelfth refrigerant fluid by another second compressor of the refrigerant fluid f’C2, a flow f’1 of the another first refrigerant fluid is obtained.

[0131] For the purpose of the present invention, step (X’) may be repeated one or more times as necessary.

[0132] According to an embodiment of the present invention, from a flow f’4 of another fourth refrigerant fluid, another further fourth flow f’4’ is obtained as a flow portion of the refrigerant fluid. The another further fourth flow f’4’ is expanded by another second refrigerant fluid expander f’EK2 to obtain another further fifth flow f’5’. The another further fifth flow f’5’ is subjected to a heat exchange process of step (VIII*’) similar to step (VIII’) described above to obtain another further sixth flow f’6’. The another further sixth flow f’6’ is further heated in a heat exchange process of step (IX*’) similar to step (IX’) described above to obtain another further seventh flow f’7’. The another further seventh flow f’7’ merges with a flow f9’ of another ninth refrigerant fluid.

[0133] For the purpose of the present invention, the cooling in step (I’) is performed by heat exchange in the second heat exchanger EX2.

[0134] For the purpose of the present invention, the cooling in step (III’), the heating in step (IX’), and the heating in step (IX*’) are performed by heat exchange in the first section EX1a of the first heat exchanger.

[0135] For the purposes of the present invention, the cooling in step (IV’), the heating in step (VIII’), and the heating in step (VIII*’) are carried out by heat exchange in the second section EX1b of the first heat exchanger.

[0136] For the purposes of the present invention, the cooling in step (V’) and the heating in step (VII’) are carried out by heat exchange in the third section EX1c of the first heat exchanger.

[0137] According to a second object of the present invention, a method for generating electric power is provided.

[0138] For the purposes of the present invention, the said generating step (energy generating step) (B) comprises the following sub-steps. (B1) Obtaining a flow e1 of combustion gas from a flow a4 of gaseous oxygen sent to a combustor and a flow b4 of gaseous carbon monoxide sent to the combustor. (B2) Obtaining a flow e2 of expanded combustion gas by expanding the flow e1 of combustion gas while generating electric power in a combustion gas expander eEK1. (B3) Obtaining a flow e3 of expanded and cooled combustion gas by cooling the flow e2 of expanded combustion gas. (B4) Obtaining a flow e5 of dehydrated combustion gas by dehydrating the flow e3 of expanded and cooled combustion gas. (B5) Separating a first portion e5’ of the flow of dehydrated combustion gas and obtaining a further cooled first portion e5’’ of the flow of dehydrated combustion gas and feeding it into a liquid carbon dioxide tank aTCO2l. (B6) Obtaining a flow e6 of liquid dehydrated and cooled combustion gas by cooling the remaining portion in the flow e5 of dehydrated combustion gas. (B7) Obtaining a flow e7 of condensed and pumped combustion gas by feeding the condensed flow e6 of dehydrated and cooled combustion gas into a combustion gas pump eP. Step of obtaining a flow e8 of the combustion gas that has been pumped and heated by heating a flow e7 of the condensed and pumped combustion gas, and sending it to the combustor for step (B1).

[0139] For the purposes of the present invention, a flow a4 of gaseous oxygen sent to the combustor is obtained from a flow a1 of liquid oxygen drawn from a liquid oxygen tank aTO2l. The flow a1 of liquid oxygen is subjected to the following steps. (B0a) Step of obtaining a flow a2 of the liquid oxygen that has been sent by pumping the flow a1 of liquid oxygen with a liquid oxygen pump aP. (B0b) Step of obtaining a flow a3 of oxygen that has been partially heated by performing a first heating on the sent flow a2 of liquid oxygen. (B0c) Step of obtaining a flow a4 of vaporized oxygen by performing a second heating on the partially heated flow a3 of oxygen, and sending the flow a4 of vaporized oxygen to the combustor CC for step (B1).

[0140] For the purposes of the present invention, a flow b4 of gaseous carbon monoxide sent to the combustor is obtained from a flow b1 of liquid carbon monoxide drawn from a carbon monoxide tank aTCOl. The flow b1 of liquid carbon monoxide is subjected to the following steps. (B0’a) Step of obtaining a flow b2 of the liquid carbon monoxide that has been sent by pumping the flow b1 of liquid carbon monoxide with a liquid carbon monoxide pump bP. (B0’b) Step of obtaining a flow b3 of carbon monoxide that has been partially heated by performing a first heating on the sent flow b2 of liquid carbon monoxide. (B0’c) Step of obtaining a flow b4 of vaporized carbon monoxide by performing a second heating on the partially heated flow b3 of carbon monoxide, and sending the flow b4 of vaporized carbon monoxide to the combustor CC for step (B1).

[0141] In particular, steps (B0b) and (B0’b) are performed by heat exchange in a first oxygen and carbon monoxide heat exchanger eEX1.

[0142] In particular, the steps (B0c) and (B0'c) are carried out by heat exchange in the second oxygen and carbon monoxide heat exchanger eEX2.

[0143] For the purpose of the present invention, from the flow e6 of the dehydrated and cooled combustion gas obtained from the step (B6), a part (e6') of the flow of the dehydrated and cooled combustion gas is separated and sent to the liquid carbon dioxide tank aTCO2l.

[0144] For the purpose of the present invention, the step (B4) comprises the following further sub-steps. (B4a) Separating a first water portion eW1 in the combustion gas separator eS1 to obtain a flow e4 of a partially dehydrated combustion gas. (B4b) Dehydrating the flow e4 of the partially dehydrated combustion gas in the combustion gas dehydration unit eDU to obtain a flow e5 of a dehydrated combustion gas.

[0145] For the purpose of the present invention, the cooling in the step (B5) is carried out by heat exchange in the first oxygen and carbon monoxide heat exchanger eEX1.

[0146] For the purpose of the present invention, the above step (B3) and the step (B8) are carried out by heat exchange in the second oxygen and carbon monoxide heat exchanger eEX2.

[0147] The step (B6) is carried out in the refrigerant fluid heat exchanger EXfr.

[0148] In particular, a flow arf1 of a first refrigerant fluid is drawn from the refrigerant fluid tank aTrf1 and heated by heat exchange with the flow e5 of the dehydrated combustion gas. Thereby, a flow arf2 of a second refrigerant fluid is obtained and stored in the second refrigerant fluid tank aTrf2.

[0149] For the purposes of the present invention, the refrigerant fluid used in step (B6) is a stored refrigerant fluid and may be, for example, glycol or an aqueous glycol solution.

[0150] According to a particular embodiment of the present invention, an additional flow F may be further sent to step (B1). The additional flow F may be composed of carbon dioxide and hydrocarbons (e.g., methane), or alternatively, may be composed of carbon monoxide produced, for example, by the gasification of coal or produced as a residue of an oil refinery.

[0151] According to an alternative embodiment of the present invention, as shown, for example, in FIG. 5, in said step (B2), the combustion gas flow e1 is expanded in a two-stage expander. Thereby, after obtaining the combustion gas flow e2 expanded in the first stage, the flow e2 of the first stage is subjected to the further steps described above.

[0152] Instead, from the second stage of expansion, a fully expanded combustion gas flow (the combustion gas flow expanded in the second stage) e12 is obtained. The fully expanded combustion gas flow e12 is further subjected to the following steps. (B9) Obtaining a second cooled and expanded combustion gas flow e13 by cooling the combustion gas flow e12 expanded in the second stage. (B10) Obtaining a second further cooled and expanded combustion gas flow e14 by cooling the second cooled and expanded combustion gas flow e13 in a fourth heat exchanger EX4. (B11) Obtaining a second dehydrated combustion gas flow e15 by separating a second water portion eW2. (B12) Obtaining a second compressed combustion gas flow e16 by compressing the second dehydrated combustion gas flow e15 with a combustion gas compressor eC. (B13) Obtaining a second compressed and heated combustion gas flow e17 by heating the second compressed combustion gas flow e16. Step of obtaining a flow e18 of a second compressed and further heated combustion gas by further heating a flow e17 of a second compressed and heated combustion gas.

[0153] For the purposes of the present invention, both step (B9) and step (B13) are carried out by countercurrent heat exchange between a flow e12 of a fully expanded combustion gas and a flow e16 of a second compressed combustion gas in a third heat exchanger EX3.

[0154] Step (B10) is instead carried out in a fourth heat exchanger EX4 as described below.

[0155] For the purposes of the present invention, from a flow e7 of a condensed and pumped combustion gas obtained in step (B7), a partial flow e9 (a flow of a second condensed and pumped combustion gas) is separated. The partial flow e9 is subjected to the following further steps. (B15) Step of obtaining a flow e10 of a second condensed and pumped and heated combustion gas by heating a partial flow e9. (B16) Step of obtaining a flow e11 of a second condensed and pumped and further heated combustion gas by further heating a flow e10 of a second condensed and pumped and heated combustion gas.

[0156] For the purposes of the present invention, step (B15) is carried out in a fourth heat exchanger EX4 by heat exchange with a flow e13 of a second cooled and expanded combustion gas.

[0157] For the purposes of the present invention, step B16 is carried out in a second oxygen and carbon monoxide heat exchanger eEX2.

[0158] According to the present embodiment, the following three flows merge into one flow e19 and are returned to the combustor for step (B1). (1) A flow e8 of a pumped and heated combustion gas. (2) The second condensation, pump delivery, and the flow e11 of the further heated combustion gas. (3) The second compression and the flow e18 of the further heated combustion gas.

[0159] For the purposes of the present invention, the flow b1 of liquid carbon monoxide and the flow a1 of liquid oxygen used in the production step (energy production step) (B) are obtained from the carbon monoxide tank aTCOl and the liquid oxygen tank aTO2l, and the flow c20 of liquid carbon monoxide and the flow o13 of liquid oxygen obtained according to the method of the storage step (A) of the present invention are stored in the liquid carbon monoxide tank cTCOl and the liquid oxygen tank cTO2l, respectively, as described above.

[0160] According to another object, the present invention provides a method for generating and storing energy, generating carbon monoxide and ultra-pure oxygen, and generating liquid carbon dioxide using carbon dioxide.

[0161] In a particular embodiment, the method of the present invention enables the management (peak shaving) of energy peaks and shortages.

[0162] Therefore, the present invention generally presents the following items.

[0163] [Item 1] A method for producing and storing energy, generating carbon monoxide and oxygen, and utilizing carbon dioxide, comprising a storage step (A) and an energy production step (B), wherein the storage step (A) enables the generation of a flow of carbon monoxide (CO), a flow of oxygen, and optionally also a flow of a refrigerant fluid (cooling fluid).

[0164] [Item 2] In the method according to the above item (Item 1), the storage step (A) includes, as sub-steps, electrolyzing a flow (3) of appropriately heated carbon dioxide to obtain an initial flow (c1) of carbon monoxide and an initial flow (o1) of oxygen (step A1), Step (A2) of obtaining a flow (c17) of carbon monoxide that is at least partially liquefied from the flow (c1) of the initial carbon monoxide Step (A3) of obtaining a flow (o10) of oxygen that is at least partially liquefied from the flow (o1) of the initial oxygen, and a method comprising the same

[0165] [Item 3] In the method according to the above item (Item 2), step (A2) further comprises, as further sub-steps Step (A2a) of obtaining a flow (c6) of carbon monoxide to be purified Step (A2b) of obtaining a flow (c12) mainly composed of carbon monoxide and steam, a recycled flow (c11) of carbon monoxide, and a flow (cr) of recycled gas Step (A2c) of obtaining a dehydrated flow (c13) of carbon monoxide Step (A2d) of obtaining a flow (c17) of carbon monoxide that is at least partially liquefied, and a method comprising the same

[0166] [Item 4] In the method according to the above item (Item 3), step (A2a) further comprises, as further sub-steps Step (A2a1) of obtaining a first portion (c2) of the flow of the initial carbon monoxide and a second portion (c2’) of the flow of the initial carbon monoxide Step (A2a2) of cooling the first portion (c2) of the flow of the initial carbon monoxide in a third heat exchanger (EX3a) to obtain a cooled first portion (c3) of the flow of the initial carbon monoxide Step (A2a3) of cooling the second portion (c2’) of the flow of the initial carbon monoxide in another third heat exchanger (EX3b) to obtain a cooled second portion (c3’) of the flow of the initial carbon monoxide Step (A2a4) of combining the cooled first portion (c3) of the flow of the initial carbon monoxide and the cooled second portion (c3’) of the flow of the initial carbon monoxide to obtain a cooled and combined flow (c4) of carbon monoxide In the first compressor (cC1), by compressing the cooled and combined carbon monoxide stream (c4), a compressed carbon monoxide stream (c5) is obtained, and in the first exchanger (cE1), by cooling the cooled and combined carbon monoxide stream (c4), a carbon monoxide stream (c6) to be purified is obtained (step A2a5).

[0167] [Item 5] In the method according to the above item (item 4), the heat exchange in step (A2a2) and the heat exchange in step (A2a3) are performed by heat exchange with a stream that circulates and operates in a Rankine cycle.

[0168] [Item 6] In the method according to the above item (item 3), step (A2b) further includes, as additional sub-steps In the first purification column (CL1), performing a first purification on the carbon monoxide stream (c6) to be purified to obtain a partially purified carbon monoxide stream (c7), a carbon monoxide stream (c8) from which the physical solvent has been separated (released), and the recycled carbon monoxide stream (c11) (step A2b1); In the second purification column (CL2), performing a second purification on the partially purified carbon monoxide stream (c7) to obtain a stream (c12) mainly composed of carbon monoxide and steam, a stream (m2) to be regenerated, and the recycled gas stream (cr) (step A2b2).

[0169] [Item 7] In the method according to the above item (item 6), step (A2b1) includes a step (p1) of washing with a physical solvent; a step (p2) of obtaining a regenerated physical solvent stream (s9) and a carbon monoxide stream (c8) from which the physical solvent has been separated by separation from the physical solvent. Step (p3) of obtaining, by compression and cooling, a physically separated and compressed stream (c9) of the physical solvent and a physically separated, compressed and cooled stream (c10) of the physical solvent. Step (p4) of obtaining the recycled carbon monoxide stream (c11) by dehydration in a first dehydration unit (cDU1). A method comprising this step.

[0170] [Item 8] In the method according to the above item (Item 7), a method in which the recycled carbon monoxide stream (c11) is merged into the appropriately heated carbon dioxide stream (3) so as to generate a more appropriately heated carbon dioxide stream (3’).

[0171] [Item 9] In the method according to the above Item 6, the step (A2b2) Step (p1’) of obtaining an expanded stream (m3) of the reaction product to be regenerated by expanding the stream (m2) to be regenerated in an expander (mEK) of the reaction product stream to be regenerated, optionally generating electric power in the process. Step (p2’) of heating the expanded stream (m3) of the reaction product to be regenerated in a heat exchanger (mEX1) of the reaction product stream to be regenerated to obtain an expanded and heated stream (m4) of the reaction product to be regenerated and sending it to a regeneration column (CL3). Step (p3’) of obtaining a stream (m5) of basic aqueous solution from the bottom of the regeneration column (CL3), obtaining a stream (h1) of carbon dioxide and water from the head of the regeneration column (CL3), and obtaining a gas stream that forms the recycled gas stream (cr) from the stream (h1) of carbon dioxide and water. A method comprising these steps.

[0172] [Item 10] In the method according to the above item (Item 9), a method in which the recycled gas stream (cr) is merged into the carbon monoxide stream (c8) from which the physical solvent has been separated (released).

[0173] [Item 11] In the method according to the above item 9, in the step (p3’), a flow (m8) that is heated and directed from the regeneration column (third column) (CL3) to the reboiler (vEX1) of the regeneration column (third column) (CL3) may be obtained, whereby a heated flow (m9) exiting from the reboiler (vEX1) is generated and returned to the regeneration column (CL3).

[0174] [Item 12] In the method according to the above item 3, the step (A2d) further includes, as additional sub-steps performing a first cooling step on the dehydrated carbon monoxide stream (c13) to obtain a partially cooled and dehydrated carbon monoxide stream (c14) (step (A2d1)); performing a second cooling step on the partially cooled and dehydrated carbon monoxide stream (c14) to obtain a cooled and dehydrated carbon monoxide stream (c15) (step (A2d2)); performing a third cooling step on the cooled and dehydrated carbon monoxide stream (c15) to obtain a further cooled and dehydrated carbon monoxide stream (c16) (step (A2d3)); expanding the further cooled and dehydrated carbon monoxide stream (c16) by expansion in a first expander (cEK1), optionally while generating power (in a power-generable state), to obtain a at least partially liquefied carbon monoxide stream (c17) such that the at least partially liquefied carbon monoxide stream (c17) can be stored in a liquid carbon monoxide tank (TCOl) (step (A2d4)).

[0175] [Item 13] In the method according to the above item 3, the step (A2d) is also performed by heat exchange with a refrigerant circulating in a refrigerant circuit.

[0176] [Item 14] In the method according to the second item above, the step (A3) further includes, as further sub-steps, a step (A3a) of obtaining a first portion (o2) of the initial oxygen flow and a second portion (o2') of the initial oxygen flow; a step (A3b) of cooling the first portion (o2) of the initial oxygen flow in a third heat exchanger (EX3a) to obtain a cooled first portion (o3) of the initial oxygen flow; a step (A3c) of cooling the second portion (o2') of the initial oxygen flow in another third heat exchanger (EX3b) to obtain a cooled second portion (o3') of the initial oxygen flow; a step (A3d) of combining the cooled first portion (o3) of the initial oxygen flow and the cooled second portion (o3') of the initial oxygen flow to obtain a cooled and combined oxygen flow (o4); a step (A3e) of compressing the cooled and combined oxygen flow (o4) with an oxygen compressor (oC1) to obtain a compressed oxygen flow (o5), and cooling the compressed oxygen flow (o5) with an oxygen exchanger (oE1) to obtain a compressed and cooled oxygen flow (o6); a step (A3f) of cooling the compressed and cooled oxygen flow (o6) to obtain at least partially liquefied oxygen flow (o10), and enabling the at least partially liquefied oxygen flow (o10) to be stored in a liquid oxygen tank (TO21).

[0177] [Item 15] In the method according to the above item (Item 14), the heat exchange between the step (A3b) and the step (A3c) is performed by heat exchange with a flow that circulates in a Rankine cycle.

[0178] [Item 16] In the method according to the above item, the heat exchange in the step (A3f) is performed by heat exchange with a refrigerant fluid that circulates in a refrigerant fluid cycle.

[0179] [Item 17] In the method according to the above item, the refrigerant fluid is hydrogen, helium, or nitrogen.

[0180] [Item 18] In the method according to the above item 9, the flow (cr) of the recycle gas merges with the flow (c8) of carbon monoxide from which the physical solvent has been separated (released).

[0181] [Item 19] In the method according to any one of the above items, the step (A) is performed using surplus current available in the network.

[0182] [Item 20] In the method according to any one of the above items, the energy generation step (B) includes, as sub-steps, Step (B1) of obtaining a flow (e1) of combustion gas from a flow (a4) of gaseous oxygen sent to the combustor and a flow (b4) of gaseous carbon monoxide sent to the combustor; Step (B2) of expanding the flow (e1) of combustion gas while generating electricity in a combustion gas expander (eEK1) to obtain an expanded flow (e2) of combustion gas; Step (B3) of cooling the expanded flow (e2) of combustion gas to obtain an expanded and cooled flow (e3) of combustion gas; Step (B4) of dehydrating the expanded and cooled flow (e3) of combustion gas to obtain a dehydrated flow (e5) of combustion gas; Step (B5) of separating a first portion (e5’) of the dehydrated flow of combustion gas and obtaining a further cooled first portion (e5’’) of the dehydrated flow of combustion gas and sending it to a liquid carbon dioxide tank (aTCO2l); Step (B6) of cooling the remaining portion of the dehydrated flow (e5) of combustion gas to obtain a liquid dehydrated and cooled flow (e6) of combustion gas; Step (B7) of obtaining a condensed and pumped combustion gas stream (e7) by feeding the condensed, dehydrated, and cooled combustion gas stream (e6) into a combustion gas pump (eP); Step (B8) of heating the condensed and pumped combustion gas stream (e7) to obtain a pumped and heated combustion gas stream (e8) and sending it to the combustor for step (B1). A method comprising these steps.

[0183] [Item 21] In the method according to the above item (Item 20), in step (B6), a part (e6') of the dehydrated and cooled combustion gas stream is separated and sent to the liquid carbon dioxide tank (aTCO2l). A method.

[0184] [Item 22] In the method according to the above Item 20 or 21, step (B4) further includes, as additional sub-steps: Step (B4a) of obtaining a partially dehydrated combustion gas stream (e4) by separating a first water portion (eW1) in a combustion gas separator (eS1); Step (B4b) of obtaining the dehydrated combustion gas stream (e5) by dehydrating the partially dehydrated combustion gas stream (e4) in a combustion gas dehydration unit (eDU). A method comprising these steps.

[0185] [Item 23] In the method according to the above item (Item 22), the cooling in step (B5) is performed by heat exchange in a first oxygen and carbon monoxide heat exchanger (eEX1). A method.

[0186] [Item 24] In the method according to any one of the above Items 20 to 23, steps (B3) and (B8) are performed by heat exchange in a second oxygen and carbon monoxide heat exchanger (eEX2). A method.

[0187] [Item 25] In the method according to the above item, the step (B6) is performed in a refrigerant fluid heat exchanger (EXfr).

[0188] [Item 26] In the method according to any one of the above Items 20 to 25, an additional stream (F) consisting of carbon dioxide and hydrocarbon may be further sent in the step (B1).

[0189] [Item 27] In the method according to any one of the above Items 20 to 26, in the step (B2), the flow (e1) of the combustion gas is expanded in one or two expansion stages to obtain a flow (e2) of the combustion gas expanded in the first stage, and it is also possible to obtain a flow (e12) of the completely expanded combustion gas. The energy generation step (B) includes, as a further step in which the flow (e12) of the completely expanded combustion gas is exposed, Step (B9) of obtaining a flow (e13) of the second cooled and expanded combustion gas by cooling; Step (B10) of obtaining a flow (e14) of the second further cooled and expanded combustion gas by cooling; Step (B11) of obtaining a flow (e15) of the second dehydrated combustion gas by separating a second water portion (eW2); Step (B12) of obtaining a flow (e16) of the second compressed combustion gas by compressing the flow (e15) of the second dehydrated combustion gas with a combustion gas compressor (eC); Step (B13) of obtaining a flow (e17) of the second compressed and heated combustion gas by heating the flow (e16) of the second compressed combustion gas; Step (B14) of obtaining a flow (e18) of the second compressed and further heated combustion gas by further heating the flow (e17) of the second compressed and heated combustion gas.

[0190] [Item 28] In the method according to the above item (item 27), the step (B9) and the step (B13) are performed in a third heat exchanger (EX3) for countercurrent heat exchange between the flow (e12) of the fully expanded combustion gas and the flow (e16) of the second compressed combustion gas.

[0191] [Item 29] In the method according to the above item 27 or 28, the step (B10) is performed in a fourth heat exchanger (EX4).

[0192] [Item 30] In the method according to the above item 20, a part of the flow (e9) is separated from the flow (e7) of the condensed and pumped combustion gas obtained in the step (B7). The energy generation step (B) includes, as a further step in which the part of the flow (e9) is exposed, a step (B15) of obtaining a second condensed, pumped, and heated combustion gas flow (e10) by heating, and a step (B16) of obtaining a second condensed, pumped, and further heated combustion gas flow (e11) by further heating.

[0193] [Item 31] In the method according to the above item (item 30), the step (B15) is performed in the fourth heat exchanger (EX4) by heat exchange with the flow (e13) of the second cooled and expanded combustion gas.

[0194] [Item 32] In the method according to the above item, the step (B16) is performed in a second oxygen and carbon monoxide heat exchanger (eEX2).

[0195] [Item 32] In the method according to any one of the above items 20 to 32, the flow of the pumped and heated combustion gas (e8), the flow of the second condensed, pumped and further heated combustion gas (e11), and the flow of the second compressed and further heated combustion gas (e18) are merged into one flow (e19) and returned to the combustor for the step (B1).

[0196] From the above description, the advantages provided by the present invention can be immediately apparent to those skilled in the art.

[0197] In particular, the method described herein solves most of the known technical problems inherent in the oxy-fuel combustion process, such as the need to supply high-purity oxygen by, for example, ASU technology.

[0198] Furthermore, the above-described oxy-fuel cycle utilizes carbon dioxide as the working fluid and, in some cases, combines the Brayton cycle and the Rankine cycle in the presence of a small amount of water (less than 20% (mol / mol)), and is more efficient because it can operate at a higher temperature.

[0199] For example, FIG. 1 shows a thermodynamic cycle composed of a Rankine cycle and a Brayton cycle. In this example, the relative contributions are optimized such that heat is introduced at the highest temperature compatible with the technical constraints of the machine and heat is discharged at the lowest temperature compatible with the availability of the heat sink.

[0200] The system operates very efficiently due to the high energy density of liquid carbon monoxide and oxygen.

[0201] The method of the present invention can generally absorb the available surplus power, store the surplus power in the form of liquefied gas (in particular, carbon monoxide and oxygen), generate energy by oxy-fuel combustion during shortages, and at the same time accumulate liquefied carbon dioxide, thereby stabilizing the electrical network and enabling so-called peak shaving.

[0202] It should be noted that the obtained carbon monoxide is also a useful chemical intermediate and can thus be marketed.

[0203] Finally, the method of the present invention is actually a system that utilizes carbon dioxide generated by industrial processes, purification processes, or even environmental processes, whereby the carbon dioxide is removed and not released into the atmosphere.

[0204] Therefore, the method of the present invention enables the mining of deposits with a high carbon dioxide content.

[0205] To avoid misunderstanding, in the method of the present invention, carbon dioxide is removed and no further carbon dioxide is generated.

[0206] In embodiments that do not contain steam and condensate, the present invention is particularly suitable for offshore applications.

Claims

1. A method for producing and storing energy, generating carbon monoxide and oxygen, and utilizing carbon dioxide, The system comprises an accumulation step (A) and an energy generation step (B), The aforementioned accumulation step (A) is a step in which a flow of carbon monoxide (CO) and a flow of oxygen are generated, and in some cases a flow of refrigerant fluid is generated. method.

2. The aforementioned storage step (A) is a substep, Step (A1) involves electrolyzing a properly heated stream of carbon dioxide (3) to obtain an initial stream of carbon monoxide (c1) and an initial stream of oxygen (o1), Step (A2) is to obtain a flow of carbon monoxide (c17) that is at least partially liquefied from the initial flow of carbon monoxide (c1), The process includes step (A3) of obtaining a flow of oxygen (o10) that is at least partially liquefied from the initial flow of oxygen (o1), The method according to claim 1.

3. Step (A2) above is a further substep, Step (A2a) to obtain the carbon monoxide stream (c6) to be purified, Step (A2b) to obtain a flow (c12) mainly consisting of carbon monoxide and vapor, a flow of recirculated carbon monoxide (c11), and a flow of recirculated gas (cr), Step (A2c) to obtain a flow of dehydrated carbon monoxide (c13), The process comprises the step (A2d) of obtaining a stream of carbon monoxide (c17) that is at least partially liquefied, The method according to claim 2.

4. The above step (A2a) is a further substep, Step (A2a1) to obtain the first portion (c2) of the initial carbon monoxide flow and the second portion (c2') of the initial carbon monoxide flow, Step (A2a2) is to obtain a cooled first portion (c3) of the initial carbon monoxide flow by cooling the first portion (c2) of the initial carbon monoxide flow in the third heat exchanger (EX3a), Step (A2a3) is to obtain a cooled second portion (c3') of the initial carbon monoxide flow by cooling the second portion (c2') of the initial carbon monoxide flow in another third heat exchanger (EX3b), Step (A2a4) is to obtain a cooled and combined carbon monoxide flow (c4) by merging the cooled first portion (c3) of the initial carbon monoxide flow with the cooled second portion (c3') of the initial carbon monoxide flow, The process includes the step (A2a5) of compressing the cooled and combined carbon monoxide flow (c4) in a first compressor (cC1) to obtain a compressed carbon monoxide flow (c5), and cooling the cooled and combined carbon monoxide flow (c4) in a first exchanger (cE1) to obtain the carbon monoxide flow to be purified (c6), The heat exchange in step (A2a2) and the heat exchange in step (A2a3) are carried out by heat exchange with a flow that circulates and operates in a Rankine cycle. The method according to claim 3.

5. The above step (A2b) is a further substep, Step (A2b1) involves performing a first purification on the carbon monoxide stream (c6) to be purified in a first purification column (CL1) to obtain a partially purified carbon monoxide stream (c7), a carbon monoxide stream from which the physical solvent has been separated (c8), and the recycled carbon monoxide stream (c11). The process includes a second purification step (A2b2) in a second purification column (CL2) to obtain a flow (c12) mainly consisting of carbon monoxide and vapor, a flow to be regenerated (m2), and a flow of recirculated gas (cr), by performing a second purification on the partially purified carbon monoxide flow (c7). The method according to claim 3.

6. The aforementioned step (A2b1) is, The step of washing with a physical solvent (p1), The steps include (p2) obtaining a stream of the regenerated physical solvent (s9) and a stream of carbon monoxide (c8) from which the physical solvent has been separated by the separation of the physical solvent, Step (p3) involves obtaining a stream (c9) in which the physical solvent has been separated and compressed by compression and cooling, and a stream (c10) in which the physical solvent has been separated, compressed and cooled. The process includes a step (p4) of obtaining the recirculated carbon monoxide flow (c11) by dewatering in a first dewatering unit (cDU1), In step (A1), the recirculated carbon monoxide flow (c11) is merged with the appropriately heated carbon dioxide flow (3) to generate an even more appropriately heated carbon dioxide flow (3'). The method according to claim 5.

7. The aforementioned step (A2b2) is, Step (p1') is to obtain an expanded flow of reaction products (m3) to be regenerated by expanding the flow of the reaction products to be regenerated (m2) with an expander (mEK) for the flow of reaction products to be regenerated, while optionally generating electricity. The step (p2') is to heat the expanded flow of the reaction product to be regenerated (m3) in a heat exchanger (mEX1) for the flow of the reaction product to be regenerated, thereby obtaining an expanded and heated flow of the reaction product to be regenerated (m4) and sending it to the regeneration column (CL3), The process includes the step (p3') of obtaining a flow of basic aqueous solution (m5) from the bottom of the regenerated column (CL3), obtaining a flow of carbon dioxide and water (h1) from the head of the regenerated column (CL3), obtaining a gas flow from the flow of carbon dioxide and water (h1) to form the recirculated gas flow (cr), and optionally obtaining a flow (m8) from the regenerated column (CL3) that is heated and directed toward the reboiler (vEX1) of the regenerated column (CL3), and providing a heated flow (m9) that exits the reboiler (vEX1) and is sent back to the regenerated column (CL3). The method according to claim 5.

8. The recirculated gas flow (cr) is merged with the carbon monoxide flow (c8) from which the physical solvent has been separated. The method according to claim 7.

9. The aforementioned step (A2d) is a further substep, Step (A2d1) involves performing a first cooling step on the dehydrated carbon monoxide flow (c13) to obtain a partially cooled and dehydrated carbon monoxide flow (c14), Step (A2d2) is to perform a second cooling step on the partially cooled and dehydrated carbon monoxide flow (c14) to obtain a cooled and dehydrated carbon monoxide flow (c15), Step (A2d3) is to perform a third cooling step on the cooled and dehydrated carbon monoxide flow (c15) to obtain a further cooled and dehydrated carbon monoxide flow (c16), The process includes step (A2d4) of expanding the further cooled and dehydrated carbon monoxide flow (c16) by a first expander (cEK1), while potentially generating electricity, to obtain a flow of at least partially liquefied carbon monoxide (c17), which can then be stored in a liquid carbon monoxide tank (TCOL), The first cooling step, the second cooling step, and the third cooling step are performed by heat exchange with the refrigerant fluid circulating within the refrigerant circuit. The method according to claim 3.

10. Step (A3) is a further substep, Step (A3a) to obtain the first part (o2) of the initial oxygen flow and the second part (o2') of the initial oxygen flow, Step (A3b) is to obtain a cooled first portion (o3) of the initial oxygen flow by cooling the first portion (o2) of the initial oxygen flow in a third heat exchanger (EX3a), Step (A3c) is to obtain a cooled second portion (o3') of the initial oxygen flow by cooling the second portion (o2') of the initial oxygen flow in another third heat exchanger (EX3b), Step (A3d) is to combine the cooled first portion (o3) of the initial oxygen flow and the cooled second portion (o3') of the initial oxygen flow to obtain a cooled and combined oxygen flow (o4), Step (A3e): Compressing the cooled and combined oxygen flow (o4) with an oxygen compressor (oC1) to obtain a compressed oxygen flow (o5), and cooling the compressed oxygen flow (o5) with an oxygen exchanger (oE1) to obtain a compressed and cooled oxygen flow (o6), The process includes step (A3f) of cooling the compressed and cooled oxygen flow (o6) to obtain a flow of oxygen (o10) that is at least partially liquefied, and making the flow of oxygen (o10) that is at least partially liquefied ready to be stored in a liquid oxygen tank (TO21), The heat exchange between step (A3b) and step (A3c) is carried out by heat exchange with a flow that circulates and operates in a Rankine cycle. The heat exchange in step (A3f) is carried out by heat exchange with the refrigerant fluid circulating in the refrigerant fluid cycle. The method according to claim 2.

11. The refrigerant fluid is hydrogen, helium, or nitrogen. The method according to claim 9.

12. Step (A) is performed using surplus current available in the network. The method according to any one of claims 1 to 11.

13. The energy generation step (B) is a substep, Step (B1) is to obtain a combustion gas flow (e1) from a flow of gaseous oxygen (a4) sent to the combustor and a flow of gaseous carbon monoxide (b4) sent to the combustor, Step (B2) involves expanding the combustion gas flow (e1) while generating electricity with a combustion gas expander (eEK1) to obtain an expanded combustion gas flow (e2), Step (B3) involves cooling the expanded combustion gas flow (e2) to obtain an expanded and cooled combustion gas flow (e3), Step (B4) is to dehydrate the expanded and cooled combustion gas flow (e3) to obtain a dehydrated combustion gas flow (e5), Step (B5) involves separating the first portion (e5') of the dehydrated combustion gas flow, obtaining a further cooled first portion (e5'') of the dehydrated combustion gas flow, and sending it to a liquid carbon dioxide tank (aTCO2l), Step (B6) involves cooling the remaining portion of the dehydrated combustion gas flow (e5) to obtain a liquid dehydrated and cooled combustion gas flow (e6), Step (B7) involves feeding the condensed, dehydrated, and cooled combustion gas flow (e6) into a combustion gas pump (eP) to obtain a condensed and pumped combustion gas flow (e7), The step (B8) includes heating the condensed and pumped combustion gas flow (e7) to obtain a pumped and heated combustion gas flow (e8) and sending it to the combustor for step (B1), The method according to any one of claims 1 to 11.

14. In step (B6), a portion of the dewatered and cooled combustion gas flow (e6') is separated and sent to the liquid carbon dioxide tank (aTCO2l). The method according to claim 13.

15. Step (B4) is a further substep, Step (B4a) involves separating the first water portion (eW1) in the combustion gas separator (eS1) to obtain a partially dehydrated combustion gas flow (e4), The procedure includes step (B4b) of dewatering the partially dewatered combustion gas flow (e4) in a combustion gas dewatering unit (eDU) to obtain the dewatered combustion gas flow (e5), The cooling in step (B5) is carried out by heat exchange in the first oxygen and carbon monoxide heat exchanger (eEX1). Step (B3) and Step (B8) are carried out by heat exchange in the second oxygen and carbon monoxide heat exchanger (eEX2). The method according to claim 13.

16. The above step (B6) is performed in a refrigerant fluid heat exchanger (EXfr). The method according to claim 15.

17. In step (B2), the combustion gas flow (e1) is expanded in one or two expansion stages, thereby obtaining the combustion gas flow (e2) expanded in the first stage, and also making it possible to obtain a fully expanded combustion gas flow (e12). The energy generation step (B) is a further step to which the fully expanded combustion gas flow (e12) is subjected, The step (B9) is to obtain a second cooled and expanded combustion gas flow (e13) by cooling, The step (B10) is to obtain a second, further cooled and expanded flow of combustion gas (e14) by cooling, Step (B11) involves separating the second water portion (eW2) to obtain a second dehydrated combustion gas flow (e15), Step (B12) is to obtain a second compressed combustion gas flow (e16) by compressing the second dehydrated combustion gas flow (e15) with a combustion gas compressor (eC), Step (B13) is to heat the second compressed combustion gas flow (e16) to obtain a second compressed and heated combustion gas flow (e17), The process includes the step (B14) of further heating the second compressed and heated combustion gas flow (e17) to obtain a second compressed and further heated combustion gas flow (e18), Steps (B9) and (B13) are carried out in a third heat exchanger (EX3) for counterflow heat exchange between the fully expanded combustion gas flow (e12) and the second compressed combustion gas flow (e16). Step (B10) is carried out in a fourth heat exchanger (EX4) for heat exchange with the second cooled and expanded combustion gas flow (e13). The method according to claim 13.

18. In step (B7), a portion of the flow (e9) is separated from the flow (e7) of the condensed and pumped combustion gas obtained, The energy generation step (B) is a further step to which the portion of the flow (e9) is exposed, The steps include heating to obtain a second condensation and pump delivery and heated combustion gas flow (e10), (B15), The process further includes the step (B16) of obtaining a second condensation and pump delivery and a flow of further heated combustion gas (e11) by heating, The aforementioned step (B15) is performed in the fourth heat exchanger (EX4) for heat exchange with the second cooled and expanded combustion gas flow (e13), The aforementioned step (B16) is performed in the second oxygen and carbon monoxide heat exchanger (eEX2). The method according to claim 17.

19. The flow of the pumped and heated combustion gas (e8), The second condensation and pump delivery and further heated combustion gas flow (e11), The second compressed and further heated flow of combustion gas (e18) is merged into one flow (e19) and returned to the combustor for step (B1). The method according to claim 18.

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