Method and system for producing synthesis gas from various sources of carbon and hydrogen by oxygen flame

Abstract

A method for producing a synthesis gas comprising carbon monoxide (CO) and hydrogen (H2), comprising the steps of: supplying an oxidizing stream comprising O2 and a first reducing stream comprising H2 to a first zone of a reactor, wherein the oxidizing stream and / or the first reducing stream comprises CO2; generating an oxygen flame in the first zone by reaction of O2 with H2; and contacting the oxidizing stream and the first reducing stream with the oxygen flame to produce CO2H2O 蒸気 supplying to the reactor a second reduced stream comprising a second carbon source comprising a hydrocarbon; and generating in a second reaction zone of the reactor a second gas comprising synthesis gas from the first gas from the first reaction zone and the second reduced stream by a reaction involving a hydrocarbon.

Description

[Technical field]

[0001] Technical Field This application relates to a method and system for producing a synthesis or reduction gas comprising carbon monoxide (CO) and hydrogen (H2) from various sources of carbon and hydrogen (H2). More particularly, the method for producing a synthesis or reduction gas uses at least one first carbon source that is CO2 and at least one second carbon source comprising a hydrocarbon. [Background technology]

[0002] Latest Technology Carbon monoxide and hydrogen based gas mixtures, commonly known as synthesis or reducing gas, are used to produce a wide range of base products, such as synthetic liquid hydrocarbons and alcohols. In addition, they can be used to produce reducing gas in the metallurgical industry (e.g., direct reduction of iron oxide). To produce such gases, including carbon monoxide (CO), a carbon source is required to feed the process. The carbon source can be derived from fossil resources, such as natural gas or coal. A carbon source and steam can be used to produce a mixture of carbon monoxide and hydrogen. Well-known approaches to achieve this include natural gas reforming techniques and steam gasification of coal.

[0003] The fight against climate change must involve, among other things, a significant reduction in greenhouse gas (GHG) emissions, especially CO2 and methane emissions. Currently, great efforts are being made to minimize the consumption of fossil resources as energy sources and also as the basic raw materials for many chemical syntheses. The use of CO2 as a carbon source in the production of syngas is one approach being explored to reduce these GHG emissions.

[0004] CO2 is found in ambient air as well as in air emissions from industrial processes that emit CO2 (e.g., cement plants, aluminum plants, steel mills, etc.). The process of capturing CO2 from ambient air, from biogenic sources, or from industrial processes and recycling it for later use is also known as "carbon capture and utilization" (CCU). CO2 captured in this way can be used as a carbon source to generate synthesis gas for the production of a wide range of products with improved carbon neutrality, i.e., lower net GHG emissions associated with the production and use cycle of the products when the CO2 comes from biogenic sources or ambient air. It is therefore possible to generate carbon synthetic fuels that are more carbon neutral and can be used in existing infrastructure. It is also possible to generate synthesis gas that can be used to formulate reducing gases for the metallurgical industry (e.g., for the direct reduction of metal oxides).

[0005] There are several methods that use CO2 as the base reagent to provide carbon for the production of synthesis gas. The most practical method consists of converting CO2 to carbon monoxide (CO) according to reaction (A) called "reverse water gas shift" or RWGS. (A) CO2+H2→CO+H2O(steam)

[0006] Hydrogen and CO based mixtures can be produced by reacting CO2 with excess hydrogen (H2).

[0007] To carry out the RWGS reaction (A), catalytic bed reactors are commonly used. However, the use of conventional catalysts to carry out reaction (A) is not without certain limitations in relation to the desired conversion of CO2. Indeed, high temperatures (e.g., above 1200°C) are required to obtain high conversions, and the use of conventional catalysts at high temperature levels is problematic.

[0008] Another method for producing synthesis gas is based on the combustion of hydrogen and pure oxygen in the presence of an oxygen flame, which generates heat and water vapor according to reaction (B). (B) H2+1 / 2O2 → H2O(steam) + heat

[0009] Water vapor generated during the production of syngas by the oxygen flame according to reaction (B) and also by the RWGS reaction (A) can be considered a "loss" of hydrogen and can impact operating costs. It would be desirable to have a method that could utilize the generated water vapor and use it to generate syngas. Summary of the Invention [Means for solving the problem]

[0010] overview According to a first aspect, the present technology provides a method for producing synthesis gas comprising carbon monoxide (CO) and hydrogen (H2), comprising: supplying an oxidizing stream comprising oxygen (O2) and a first reducing stream comprising hydrogen (H2) to at least a first zone of at least one reactor, wherein the oxidizing stream and / or the first reducing stream further comprises a first carbon source which is CO2; generating an oxygen flame in a first zone by reaction of oxygen from the oxidizing stream with hydrogen from the first reducing stream and contacting the oxidizing stream and the first reducing stream with the oxygen flame to produce a first gas comprising at least carbon monoxide (CO) and water vapor (HO); providing a second reduction stream to the reactor comprising a second carbon source comprising at least one hydrocarbon; generating a second gas, comprising synthesis gas, from the first gas from the first reaction zone and the second reduction stream by a reaction involving a hydrocarbon in a second reaction zone of the reactor; The present invention relates to a method comprising the steps of:

[0011] According to one embodiment, in the first zone, the generation of a first gas comprising at least carbon monoxide (CO) and water vapor (H2O) is carried out at a temperature of at least 1000°C and at most 2400°C.

[0012] According to another embodiment, in the first zone, the generation of the first gas comprising at least carbon monoxide (CO) and water vapor (H2O) is carried out at a temperature between about 1000°C and about 1900°C.

[0013] According to another embodiment, the step of generating synthesis gas in the second zone is carried out at a temperature of at least 700°C and at most 1500°C.

[0014] According to another embodiment, the step of generating synthesis gas in the second zone occurs at a temperature between about 700°C and about 1000°C.

[0015] According to another embodiment, the step of generating synthesis gas in the second zone is carried out at a temperature lower than the temperature of the first zone.

[0016] According to another embodiment, the oxidizing stream is fed to a central portion of the lower portion of the first zone, and the first reducing stream is fed to the lower portion of the first zone at the periphery of the oxidizing stream.

[0017] According to another embodiment, the second gas generated in the second zone comprises synthesis gas and residual CO2, and the method further comprises recycling a portion of the second gas to the first zone.

[0018] According to another embodiment, a portion of the second gas is recycled to the first reduced stream.

[0019] According to another embodiment, the method further comprises cooling a portion of the recycled second gas prior to recycling.

[0020] According to another embodiment, the method is carried out in multiple reactors in parallel, each reactor having a first zone receiving the oxidizing stream and the first reducing stream and where a first gas is produced, and a second zone receiving the second reducing stream and where a second gas is generated.

[0021] According to a further embodiment, the reactor comprises a plurality of first zones and a shared second zone, providing an oxidizing stream and a first reducing stream to each first zone of the plurality of first zones to generate a first gas in each first zone; A second return stream is supplied to a shared second zone that receives the first gas produced in each of the first zones, and a second gas is generated in the shared second zone.

[0022] According to another aspect, the present technology provides a system for producing a synthesis gas comprising carbon monoxide (CO) and hydrogen (H2), the system comprising at least one reactor, the reactor comprising at least one first reaction zone and at least one second reaction zone; a first reaction zone is provided with an oxidizing stream comprising oxygen (O2) and a first reducing stream comprising hydrogen (H2), the oxidizing stream and / or the first reducing stream further comprising a first carbon source being CO2, an oxygen flame is generated in the first zone by reaction of the oxygen of the oxidizing stream with the hydrogen of the first reducing stream, and a first gas comprising at least carbon monoxide (CO) and water vapor (HO) is produced by contacting the oxidizing stream and the first reducing stream with the oxygen flame; The system relates to a second reaction zone, wherein a second reduction stream containing a second carbon source containing at least one hydrocarbon is supplied to the second reaction zone, and a second gas containing synthesis gas is generated in the second reaction zone from the first gas from the first reaction zone and the second reduction stream by a reaction involving hydrocarbons.

[0023] According to one embodiment, the first zone is at a temperature of at least 1000° C. and up to 2400° C. during the production of a first gas comprising at least carbon monoxide (CO) and water vapor (H 2 O).

[0024] According to another embodiment, the first zone is at a temperature between about 1000° C. and about 1900° C. during production of a first gas comprising at least carbon monoxide (CO) and water vapor (H 2 O).

[0025] According to another embodiment, the second zone is at a temperature of at least 700° C. and at most 1500° C. during the production of synthesis gas.

[0026] According to another embodiment, the second zone is at a temperature between about 700° C. and about 1000° C. during production of synthesis gas.

[0027] According to another embodiment, the step of generating synthesis gas in the second zone is carried out at a temperature lower than the temperature of the first zone.

[0028] According to another embodiment, the second gas generated in the second zone comprises synthesis gas and residual CO2, and the system further comprises means for recycling a portion of the second gas to the first zone.

[0029] According to another embodiment, the means for recycling include a duct conveying a portion of the second gas mixed with the first return stream.

[0030] According to another embodiment, the system further comprises an apparatus for cooling a portion of the recycled second gas before it is recycled.

[0031] According to another embodiment, the first zone and the second zone are each cylindrical in shape.

[0032] According to another embodiment, the system includes first means for supplying an oxidizing stream to a central portion of a lower portion of the first zone, and second means for supplying a first reducing stream to the lower portion of the first zone at a periphery of the oxidizing stream.

[0033] According to another embodiment, the first means comprises a first central tube and the second means comprises an annular space extending vertically between an outer wall of the central tube and an inner wall of the first zone.

[0034] According to another embodiment, the system includes a third means for providing a second recirculating stream to the second zone.

[0035] According to another embodiment, the first zone and the second zone are each cylindrical in shape and the third means consists of an opening, optionally in an upper region of the first zone and in a lower region of the second zone, formed by an annular space extending between an outer wall of the first zone and an inner wall of the second zone.

[0036] According to another embodiment, the system includes multiple reactors in parallel, each reactor having a first zone receiving the oxidizing stream and the first reducing stream and where a first gas is produced, and a second zone receiving the second reducing stream and where a second gas is generated.

[0037] According to another embodiment, the reactor comprises a plurality of first zones and a shared second zone, Each first zone of the plurality of first zones is supplied with an oxidizing stream and a first reducing stream to generate a first gas in each first zone; The shared second zone is fed with a second return stream to receive the first gas produced in each of the first zones and generate a second gas in the shared second zone.

[0038] According to some aspects, methods and / or systems according to the present technology may include the following embodiments.

[0039] According to one embodiment, the oxidizing stream comprises oxygen and CO2.

[0040] According to another embodiment, the first reduction stream comprises hydrogen (H2) and CO2, and optionally water vapor, in a ratio of H2O / H2 between 0 and 1, preferably a ratio of H2O / H2 between 0 and 0.5.

[0041] According to another embodiment, the oxidizing stream and the first reducing stream each comprise CO2.

[0042] According to another embodiment, only the oxidation stream contains CO2.

[0043] According to alternative embodiments, the CO2 is derived from industrial waste, biogenic CO2 from biogas, CO2 captured directly from ambient air, or a mixture thereof.

[0044] According to another embodiment, the hydrogen present in the first reduced stream originates from the electrolysis reaction of water.

[0045] According to another embodiment, the hydrogen present in the first reduced stream originates from a water electrolysis reaction in an electrolyzer powered by electricity generated from a renewable source (e.g., generated from solar energy, wind energy, hydroelectric energy, biomass, or geothermal energy) or nuclear energy.

[0046] According to another embodiment, the hydrogen present in the first reduced stream originates from a steam reforming reaction of natural gas or methane in a process in which the generated CO2 is at least partially captured and sequestered.

[0047] According to another embodiment, the hydrogen present in the first reduced stream includes hydrogen originating from a water electrolysis reaction in an electrolyzer powered by electricity generated from renewable sources (e.g., solar, wind, hydroelectric, biomass, or geothermal energy) or nuclear energy, as well as hydrogen originating from a natural gas or methane steam reforming reaction in a process in which the evolved CO2 is at least partially captured and sequestered.

[0048] According to another embodiment, the hydrogen present in the first reduced stream further comprises hydrogen resulting from a methane pyrolysis reaction.

[0049] According to another embodiment, hydrogen, oxygen, and CO2 are fed to the first zone in a molar ratio of H2 / O2 of at least 2 and a molar ratio of H2 / CO2 of at least 1.8.

[0050] According to another embodiment, hydrogen, oxygen, and CO2 are fed to the first zone in a molar ratio of H2 / O2 between 2 and 10 and a molar ratio of H2 / CO2 between 1.8 and 9.

[0051] According to another embodiment, oxygen and CO2 are supplied to the first zone in a molar ratio of O2 / CO2 of at least 0.5.

[0052] According to another embodiment, oxygen and CO2 are fed to the first zone in a molar ratio of O2 / CO2 between 0.5 and 6.

[0053] According to another embodiment, the generation of synthesis gas comprises steam reforming of hydrocarbons using steam contained in the first gas.

[0054] According to another embodiment, the second reduced stream further comprises steam, and the generation of synthesis gas comprises steam reforming of hydrocarbons using the steam contained in the first gas and the steam contained in the second reduced stream.

[0055] According to another embodiment, the second carbon source comprises fossil or renewable hydrocarbons.

[0056] According to another embodiment, the second carbon source comprises fossil or renewable natural gas.

[0057] According to another embodiment, the second carbon source comprises methane.

[0058] According to another embodiment, the second carbon source comprises methane from biogas.

[0059] According to another embodiment, the second reduced stream further comprises biomass-derived organic compounds.

[0060] According to another embodiment, the second reduction stream is represented by the formula C, where α varies from 1 to 5, β varies from 2 to 10, and γ varies from 1 to 4. α H β O γ The compound further includes the compound of the formula:

[0061] According to another embodiment, the second reduction stream comprises methane (CH4) and optionally hydrogen (H2), in a molar ratio of H2 / CH4 between 0 and 2.5.

[0062] According to another embodiment, the second reduction stream comprises methane (CH4) and optionally hydrogen (H2), the molar ratio of the CH4 fed to the total amount of H2 fed to the two zones being between 0.1 and 1.

[0063] According to another embodiment, the second reduced stream further comprises hydrogen (H2).

[0064] According to another embodiment, the hydrogen present in the second reduced stream originates from a steam reforming reaction of natural gas or methane in a process in which the generated CO2 is at least partially captured and sequestered.

[0065] According to another embodiment, the second reducing stream comprises hydrogen in an amount to balance the molar composition of the synthesis gas such that H2 / CO>2 and (H2-CO2) / (CO+CO2)>2.

[0066] According to another embodiment, the second reduction stream comprises methane (CH4) and optionally water vapor (H2O), the molar ratio of water vapor (H2O) to CH4 being between 0 and 2.

[0067] According to another embodiment, the second reduced stream further comprises water vapor.

[0068] According to a further embodiment, the production of carbon monoxide and water vapor in the first zone is carried out in the absence of a catalyst.

[0069] According to another embodiment, the generation of the second gas, including synthesis gas, in the second zone of the reactor is carried out in the absence of a catalyst.

[0070] According to another embodiment, the oxygen (O2) present in the oxidizing stream originates from the electrolysis reaction of water.

[0071] According to another embodiment, the oxygen (O2) present in the oxidation stream comes from an air separation unit (ASU).

[0072] According to a further aspect, the present technology relates to the use of the synthesis gas produced by the methods defined herein or the systems defined herein for the production of chemical products or fuels.

[0073] According to one embodiment, the use allows for the production of synthetic hydrocarbons.

[0074] According to yet another aspect, the present technology relates to the use of synthesis gas produced by a method as defined herein or a system as defined herein as a reducing agent in the metallurgical industry.

[0075] According to yet another aspect, the present technology relates to the use of the system defined herein for the treatment of gaseous industrial emissions containing CO2. [Brief description of the drawings]

[0076] [Figure 1] FIG. 1 shows a schematic vertical cross-sectional view of a reactor that can be used to carry out a method according to one embodiment.

[0077] [Diagram 2] FIG. 2 shows a schematic vertical cross-sectional view of a reactor that can be used to carry out a method according to one embodiment, in which the oxygen flame extends towards the second zone.

[0078] [Diagram 3] FIG. 3 shows a schematic vertical cross-sectional view of a reactor that can be used to carry out a method according to another embodiment.

[0079] [Figure 4] FIG. 4 shows a schematic vertical cross-sectional view of a system including several parallel reactors that can be used to carry out a method according to another embodiment.

[0080] [Diagram 5] FIG. 5 shows a schematic vertical cross-sectional view of a reactor containing multiple first reaction zones and a shared second zone that can be used to carry out a process according to yet another embodiment.

[0081] [Figure 6] FIG. 6 shows a bottom view of the reactor of FIG.

[0082] [Figure 7] 7 shows a schematic vertical cross-section of a reactor that can be used to carry out the process of the invention and that is used in the examples. The figure shows the general arrangement of the tubes in this reactor. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS

[0083] Detailed Description All technical and scientific terms and expressions used herein have the same meaning as commonly understood by one of ordinary skill in the art. However, definitions of certain terms and expressions used are provided below.

[0084] As used in this document, the term "about" means approximately, within the region of, and around. When the term "about" is used in connection with a numerical value, the term modifies the numerical value above and below, for example, with a variance of 10% compared to the nominal value. The term can also take into account, for example, experimental error of a measuring device or rounding of values.

[0085] Whenever an interval of values ​​is mentioned in this application, the lower and upper limits of the interval are always included in the definition, unless otherwise stated.

[0086] As used herein, the terms "synthesis gas," "reducing gas," and "syngas" are used interchangeably to identify a gas mixture that includes at least carbon monoxide (CO) and hydrogen (H2). In some embodiments, synthesis gas, reducing gas, or syngas may include CO2.

[0087] The term "stream" is used to describe the different gas streams involved in the production of synthesis gas in different zones within the reactor.

[0088] The term "carbon source" refers to a chemical compound used to provide carbon that leads to the synthesis gas produced. Thus, the carbon source provides at least the carbon that leads to the carbon monoxide (CO) that is produced. Various chemical compounds can be used as carbon sources. In the method of the present invention, at least CO2 and at least one hydrocarbon (i.e., a compound essentially based on carbon and hydrogen) are used as carbon sources to produce the synthesis gas. According to some embodiments, the hydrocarbon used as one of the carbon sources is methane (CH4) or fossil or renewable natural gas (RNG). According to some embodiments, other carbon sources may be used, such as organic compounds containing carbon, hydrogen, and oxygen, as described below.

[0089] The phrase "electricity from renewable sources" or "electricity generated from renewable sources" refers to electricity generated from solar energy, wind energy, hydroelectric energy, biomass, or geothermal energy.

[0090] As used herein, the expression "fossil natural gas" refers to a mixture of gaseous hydrocarbons (essentially methane) resulting from the natural transformation of organic matter from underground deposits.

[0091] As used herein, the term "renewable natural gas" (RNG) refers to a gaseous fuel also known as biomethane or first generation RNG, which may contain 55-99% methane, typically produced from biogas resulting from the anaerobic digestion of organic matter.

[0092] Thus, this document presents an innovative method for producing synthesis gas using at least CO2 as a carbon source and with an oxygen flame generated by the reaction of oxygen with hydrogen. More specifically, the method for producing synthesis gas includes the steps of: feeding an oxidizing stream containing oxygen (O2) and a first reducing stream containing hydrogen to at least a first reaction zone of at least one reactor, where the oxidizing stream and / or the first reducing stream further comprises a first carbon source, which is CO2; generating an oxygen flame in the first zone by reaction of the oxygen of the oxidizing stream with the hydrogen of the first reducing stream and contacting the oxidizing stream and the first reducing stream with the oxygen flame to produce a first gas containing at least carbon monoxide (CO) and water vapor (H2O); feeding a second reducing stream to the reactor, which contains a second carbon source containing at least one hydrocarbon; generating a second gas, including synthesis gas, from the first gas coming from the first zone and the second reducing stream by a reaction involving a hydrocarbon in the second zone of the reactor.

[0093] As described above, the method uses at least CO2 as a carbon source to produce syngas. The CO2 can have a variety of origins. Thus, the method may use CO2 from industrial waste, biogenic CO2 from biogas, or CO2 captured directly from ambient air, for example by a direct air capture (DAC) process. In some embodiments, the carbon source includes CO2 captured from ambient air or CO2 from biomass, in which case the carbon is referred to as "carbon neutral" or "biogenic."

[0094] FIG. 1 shows the general principle of the operation of the method. Thus, according to some embodiments, the method can be carried out in at least one reactor 10 having two reaction zones 12 and 14. In some embodiments, the reactor is provided with insulation (not shown in the drawing). The second reaction zone can be described as a "downstream" zone of the first reaction zone, since products from the reaction involving the first zone can serve as input for the reaction occurring in the second reaction zone. As will be explained in more detail below, the reaction occurring in the second reaction zone is different from the reaction occurring in the first reaction zone. In the first zone, the reaction involves at least CO2 as a first carbon source, and in the second zone, a second carbon source comprising a hydrocarbon. Several sources and types of carbon and / or hydrogen can be used at strategic locations in the reactor. According to some embodiments, the selection of the carbon and / or hydrogen sources and the locations at which these gases are fed to the reactor can reduce operating costs. According to some embodiments, the method may be carried out in at least one reactor comprising two reaction zones 12 and 14, an inlet zone 20, and an outlet zone 28. At least two gas streams are fed to the first reaction zone 12. The stream 16 fed to the first reaction zone 12 is an oxidation stream comprising at least oxygen (O2). The gas stream 18 fed to the first reaction zone 12 is a first reduction stream comprising at least hydrogen (H2). According to the method of the present invention, at least one of the oxidation stream 16 and the first reduction stream 18 further comprises a first carbon source which is CO2.

[0095] In the first reaction zone 12, an oxygen flame 22 is generated by the combustion of hydrogen (H2) from the first reducing stream 18 in the presence of oxygen (O2) from the oxidizing stream 16 according to the aforementioned reaction (B). This flame is bright and radiating and provides the heat necessary to sustain the reaction that produces a first gas comprising carbon monoxide (CO) produced from a first carbon source comprising at least CO2, and also comprising water vapor, according to reaction (A) of the RWGS. Thus, the first gas comprising at least carbon monoxide (CO) and water vapor (H2O) is obtained by "contacting" the oxidizing stream and the first reducing stream with the oxygen flame. The expression "contacting" according to the method of the invention is understood to mean a distance "d" between the oxidizing stream and the reducing stream that may range from 0 to 50 mm, preferably from 0 to 30 mm. The distance "d" between the oxidizing and reducing streams can be 0 mm, 5 mm, 10 mm, 15 mm, 20 mm, 25 mm, 30 mm, 35 mm, 40 mm, 45 mm, 50 mm, or any value therebetween. For example, the distance "d" can be 0-50 mm, 0-40 mm, 0-30 mm, 0-20 mm, or 0-10 mm. In addition, the oxygen flame can generate ionic species and free radicals that can promote the conversion of the carbon source to CO. It should also be noted that the generation of carbon monoxide and water vapor in the first reaction zone 12 can thus be achieved in the absence of a catalyst, such as a conventionally used solid catalyst. The combustion of hydrogen (H2) in the presence of oxygen (O2) to generate the oxygen flame can be initiated by an ignition device. According to some embodiments, the oxygen flame can enable a temperature of at least 600°C to be reached in the first reaction zone. According to other embodiments, the temperature reached in the first zone 12 is at least 1000° C. and up to 2400° C. According to some embodiments, the reactor may be equipped with insulation around the reaction zone to minimize heat loss and thus maintain a temperature within the reactor high enough to support the reaction.According to some embodiments, the generation of the first gas comprising at least carbon monoxide (CO) and water vapor (HO) in the first zone 12 may be carried out at a temperature of about 1000° C. to about 2300° C., or about 1000° C. to about 2200° C., or about 1000° C. to about 2100° C., or about 1000° C. to about 2000° C., or about 1000° C. to about 1900° C. The temperature in the first zone 12 may also vary from about 1000° C. to about 1800° C., from about 1000° C. to about 1700° C., from about 1000° C. to about 1600° C., or from about 1000° C. to about 1500° C. In some embodiments, the oxygen flame generated in the first zone 12 may extend to the second zone 14 of the reactor, as shown in FIG. 2. 1 and 2 generally show the reactor with the reaction zones 12 and 14 displayed one on top of the other (serial zones), but other configurations are envisioned. Thus, according to some embodiments, the two reaction zones 12 and 14 may be at least partially adjacent to each other (parallel zones). In one embodiment, the oxygen (O2) used in the oxidation stream is pure oxygen. By "pure" oxygen, it is understood that this does not necessarily mean 100% purity, but rather that the oxygen-based mixture may substantially comprise O2, with certain impurities, such as N2, H2O, etc. According to some embodiments, the oxygen present in the oxidation stream 16 originates from the electrolysis reaction of water. According to certain other embodiments, the oxygen (O2) present in the oxidation stream 16 may come from an air separation unit (ASU). It would also be possible to use oxygen that is a mixture of oxygen originating from the electrolysis reaction of water and oxygen originating from an air separation unit.

[0096] In some embodiments, the first carbon source comprising CO2 is fed to the first zone of the reactor together with oxygen from the oxidation stream. In another embodiment, the first carbon source comprising CO2 is fed to the first zone of the reactor together with hydrogen from the first reduction stream. In some cases, a portion of the first carbon source comprising CO2 is fed to the first zone of the reactor together with oxygen from the oxidation stream, and another portion of the first carbon source is fed to the first zone of the reactor together with hydrogen from the first reduction stream. In a preferred embodiment, the first carbon source comprising CO2 is fed to the first zone together with only oxygen from the oxidation stream.

[0097] As mentioned above, the CO2 may come from a variety of sources. In some embodiments, the CO2 comes from industrial waste, is biogenic CO2 from biogas, or is CO2 captured directly from ambient air. In some preferred embodiments, the CO2 used as the first carbon source is biogenic CO2 from biogas.

[0098] According to one embodiment, the hydrogen required in the method of the invention may be hydrogen certified as low carbon footprint hydrogen. According to one embodiment, the hydrogen required to generate the oxygen flame in the first zone in the method of the invention, i.e. the hydrogen present in the first return stream 18, may originate at least in part from the electrolysis reaction of water. This hydrogen is called "green hydrogen" if the electrolyzer in which the electrolysis of water is carried out is powered by electricity generated from renewable sources, such as solar energy, wind energy, hydroelectric energy, biomass or geothermal energy. In some embodiments, the electricity used for the electrolysis of water may come from nuclear energy, a source of energy that does not emit greenhouse gases, and this hydrogen may also be called "pink hydrogen" in the context of the present technology.

[0099] According to another embodiment, the hydrogen present in the first reduced stream 18 feeding the first zone of the reactor may be “blue hydrogen”, i.e. hydrogen resulting from a steam reforming reaction of natural gas or methane in a process in which the evolved CO2 is at least partially captured and sequestered.

[0100] According to yet another embodiment, the hydrogen present in the first reduced stream 18 fed to the first zone of the reactor may be "turquoise hydrogen", i.e., hydrogen resulting from a methane pyrolysis reaction.

[0101] According to yet another embodiment, the hydrogen present in the first reduced stream 18 feeding the first zone of the reactor may be “pink hydrogen”, i.e., hydrogen resulting from a nuclear-powered water electrolysis reaction.

[0102] A mixture of hydrogen from various sources may also be used to supply the first zone to generate an oxygen flame and form a first gas including carbon monoxide (CO) and water vapor (H2O). Thus, in some embodiments, the first reduced stream 18 may include a mixture of green hydrogen and blue hydrogen, or a mixture of green hydrogen and turquoise hydrogen, a mixture of blue hydrogen and turquoise hydrogen, or a mixture of green hydrogen, blue hydrogen and turquoise hydrogen.

[0103] In some embodiments, the amount of hydrogen (e.g., green, blue, pink, and / or turquoise hydrogen) supplied to first zone 12 is metered to minimize operating costs while ensuring that the molar composition of the synthesis gas at the reactor outlet satisfies equations (C) and (D) below. (C) H2 / CO≧2 (D) (H2-CO2) / (CO+CO2)≧2

[0104] These equations also take into account the fact that additional hydrogen can be introduced via stream 24 into the second zone 14 of the reactor to balance the composition of the syngas, as discussed below.

[0105] In certain embodiments, hydrogen, oxygen, and CO2 are fed to the first zone 12 at a molar ratio of H2 / O2 of at least 2 and a molar ratio of H2 / CO2 of at least 1.8. According to another embodiment, hydrogen, oxygen, and CO2 may be fed to the first zone at a molar ratio of H2 / O2 of 2 to 10 and a molar ratio of H2 / CO2 of 1.8 to 9. Thus, hydrogen and oxygen can be fed to the first zone 12 at a molar ratio of H2 / O2 of about 2, about 3, about 4, about 5, about 6, about 7, about 8, about 9, or about 10, or any value therebetween. Additionally, the amount of hydrogen and the amount of CO2 fed to the first zone can be adjusted to provide a molar ratio of H2 / CO2 of about 1.8, or about 2, or about 3, or about 4, or about 5, or about 6, or about 7, or about 8, or about 9, or any value therebetween. According to some embodiments, oxygen and CO2 can be fed to the first zone at a molar ratio of O2 / CO2 of at least 0.5. For example, oxygen and CO2 can be fed to the first zone at a molar ratio of O2 / CO2 between 0.5 and 6. Thus, the amount of oxygen and the amount of CO2 fed to the first zone can be adjusted to provide a molar ratio of O2 / CO2 of about 0.5, or about 1, or about 2, or about 3, or about 4, or about 6, or any value between these values. The molar ratios of H2 / O2, H2 / O2, and O2 / CO2 may be adjusted depending on the amount of other gases, if any, fed to the reactor and the desired ratio of CO to H2 in the final synthesis gas.

[0106] It should be noted that in some embodiments, the oxidized stream 16 and / or the reduced stream 18 may contain, in addition to the above inputs, certain amounts of impurities and water vapor. According to some embodiments, the reduced stream 18 may contain water vapor with a molar ratio of HO / H of up to 0.5.

[0107] Referring again to Figures 1 and 2, the reactor 10 includes a second reaction zone 14 configured generally in series with the first zone 12. In some embodiments, as described above and particularly shown in Figure 2, the oxygen flame 22 generated in the first zone may extend to the second zone 14. In this manner, the two zones 12 and 14 may also be at least partially parallel to each other. In Figures 1 and 2, the streams are fed substantially parallel to each reaction zone. Thus, the first and second reduction streams are substantially parallel in the reactor. However, in other embodiments, it may be contemplated to have "angled" feeds of the streams, i.e., the first and second reduction streams may be fed at an angle to each other. In some embodiments, the first and second reduction streams may be fed at a substantially perpendicular angle to each other.

[0108] The second reaction zone receives the gas formed in the first reaction zone, which contains at least CO and water vapor generated by reactions (A) and (B), and may contain some residual CO2 and / or hydrogen H2. This second reaction zone 14 is further fed with a second reduction stream 24 containing a second carbon source comprising at least one hydrocarbon. In addition, the reduction stream 24 may contain water vapor. After reaction of the second reduction stream with the first gas in the second reaction zone of the reactor, a second gas 26 comprising synthesis gas is recovered at the outlet 28 of the reactor.

[0109] The second reduced stream 24 contains at least one hydrocarbon as a second carbon source, and the generation of synthesis gas in the second reaction zone 14 is performed in part by steam reforming the hydrocarbon with steam contained in the first gas and / or any steam present in the reduced stream 24 as described above. The carbon source can be a fossil or renewable hydrocarbon, preferably methane or fossil or renewable natural gas (RNG). In some embodiments, the second carbon source is methane from biogas. When using a hydrocarbon that is methane, reaction (E) and reaction (F) in the presence of residual CO2 take place in the second zone 14. (E) CH4+H2O→CO+3H2 (F) CH4+CO2→2CO+2H2

[0110] Steam reforming of the hydrocarbons fed to the second zone can result in synthesis gas that meets the criteria set forth in equations (C) and (D).

[0111] As explained above, hydrogen may also be fed to the second zone 14 to produce synthesis gas. If additional hydrogen is fed to zone 14 by the reduction stream 24, on the one hand the composition of the synthesis gas can be balanced to comply with the above equations (C) and (D) and on the other hand water vapor and residual CO2 can be reduced in this zone.

[0112] Additionally, the molar ratio of CO to H2 in the syngas can be varied by feeding both one or more hydrocarbons and hydrogen to the second zone 14.

[0113] According to some embodiments, the hydrogen supplied to the second zone 14 via the second reduced stream 24 may be blue hydrogen as described above, i.e. hydrogen resulting from a steam reforming reaction of natural gas or methane in a process in which the evolved CO2 is at least partially captured and sequestered.

[0114] According to some embodiments, the second reduced stream 24 may comprise methane (CH4) and optionally hydrogen (H2), in a molar ratio of H2 / CH4 between 0 and 2.5.

[0115] According to another embodiment, a second reduction stream 24 comprising methane (CH4) and optionally hydrogen (H2) can be fed to the second zone such that the molar ratio between the CH4 fed and the total amount of H2 fed to the two zones is between 0.1 and 1.

[0116] It should be noted that in some embodiments, the second reduced stream 24 may contain water vapor and small amounts of impurities in addition to the above inputs.

[0117] According to some embodiments, the reduced stream 24 fed to the second zone 14 may include methane (CH4) and optionally water steam (H2O), with the molar ratio of water steam (H2O) to CH4 ranging from 0 to 2.

[0118] According to some embodiments, the reduced stream 24 feeding the second zone 14 may further comprise organic compounds derived from biomass, i.e., containing biogenic carbon. These organic compounds containing biogenic carbon are represented by the formula C, where α varies from 1 to 5, β varies from 2 to 10, and γ varies from 1 to 4. α H β O γ may have the following structure:

[0119] According to some embodiments, the reaction in the second zone 14 of the reactor is carried out at a lower temperature than the temperature in the first zone 12. In some embodiments, the synthesis gas can be generated in the second zone 12 at a temperature of at least 700° C. and up to 1500° C. In some cases, the temperature in the second reaction zone can be from about 700° C. to about 1000° C. Thus, the temperature in the second reaction zone can be from about 700° C. to about 1400° C., from about 700° C. to about 1300° C., from about 700° C. to about 1200° C., from about 700° C. to about 1100° C., from about 700° C. to about 1000° C., from about 700° C. to about 900° C., or from about 700° C. to about 800° C. Lower temperatures in the second zone 14 can be achieved in a variety of ways, for example, by adjusting the insulation and / or heating or cooling system of the reactor. In some embodiments, the desired temperature can be achieved in the second reaction zone 14, for example, by using walls that are less well insulated than the reactor walls of the first zone. In some cases, a cooling system can also be used to achieve the desired temperature in the second zone of the reactor.

[0120] According to some embodiments, the production of synthesis gas in the second zone 14 of the reactor can be carried out in the absence of a catalyst, such as a conventionally used solid catalyst (eg, a metal catalyst).

[0121] The use of the second reaction zone 14 substantially reduces the amount of water vapor resulting from the reaction occurring in the first zone 12 and optionally present in the stream 24 feeding this second zone. This is an important advantage. In addition, in some embodiments, if CO2 remains in the zone 14 as a result of the reaction occurring in the zone 14 and it is preferred to further reduce it, a return loop 30 as shown in FIG. 3 can be operated to return a portion of the gas generated in the second zone 14 to the first zone 12 of the reactor. According to some embodiments, the recycled portion of the second gas may be mixed with the first reduction stream 18 before feeding it to the first zone 12. In addition, the recycled portion of the second gas may be cooled at the reactor outlet 28 before returning it to the first zone. According to some embodiments, the cooling must be possible using a fan to overpressurize the gas at the outlet 28.

[0122] According to certain embodiments, the production of synthesis gas by the method of the present invention may include supplying a first zone 12 with an oxidation stream 16 comprising oxygen and a renewable carbon source and a first reduction stream 18 comprising green hydrogen, and supplying a second zone 14 with blue hydrogen and a fossil carbon source. When the renewable carbon source is CO2 and the fossil carbon source is methane, the reactions involved may allow for efficient and low-cost production of synthesis gas. The following equation (G) shows a typical overall reaction scheme that can be achieved. (G) 1 / 2O2+H2(green)+CO2(renewable)+2CH4(fossil)+H2(blue)→3(CO+2H2)

[0123] The method can use fossil carbon sources as inputs, but considering that it also uses CO2 as an input, the net GHG emissions from the reactor can be zero or very close to zero, and the method can be considered as a Carbon Capture and Utilization (CCU) method.

[0124] Schematic diagrams of reactors that can be used to carry out the method of the invention are shown in Figures 1 to 3. However, the design of the reactor may vary and / or a system comprising several reactors may be used. Further examples of designs are shown in Figures 4 to 7, which are discussed below. However, the design of the reactor or system is not limited to the diagrams of Figures 1 to 7, and the design can be adjusted as long as it allows the reactions involved in the production of synthesis gas to take place within the parameters mentioned above.

[0125] In some embodiments, a cylindrical reactor containing two reaction zones as described above may be used, in some embodiments, each of the two zones may itself be cylindrical.

[0126] The reactor 10 may include a first means for feeding the oxidized stream 16 to a central portion of the lower portion of the first zone 12 and a second means for feeding the first reduced stream 18 to the lower portion of the first zone at the periphery of the oxidized stream. In some embodiments, the reactor may include a first central tube through which the oxidized stream 16 is fed to the first zone 12 and an annular space extending vertically between an outer wall of the central tube and an inner wall of the first zone 12 for feeding the first reduced stream 18. In addition, the reactor may include a third means for feeding the second reduced stream 24 to the second zone 14. In some embodiments, this third means may consist of an opening formed by an annular space extending between an outer wall of the first zone 12 and an inner wall of the second zone 14. According to some embodiments, the annular space through which the second reduction stream 24 is fed to the reactor may extend between the outer wall of the first zone 12 and the inner wall of the second zone 14 at an upper region of the first zone and a lower region of the second zone. In some embodiments, the inlets of each of the streams 16, 18, and 24 may be in the same horizontal plane, as shown, for example, in FIG. 7. The reactor may also include an outlet 28 at the top of the second zone 14 to recover gases, including synthesis gas, formed in the second zone. Additionally, as discussed above, the reactor may include a return loop 30 (FIG. 3) for returning a portion of the gases formed in the second zone 14 as needed.

[0127] According to another embodiment, the production of synthesis gas can be carried out using multiple reactors located in parallel, as shown in Figure 4. Each of the reactors can correspond, for example, to one of the reactors shown in Figures 1 to 3. However, the reactors in Figure 4 can have different designs, as long as each reactor has a first zone to which the oxidizing stream and the first reducing stream are fed to produce a first gas, and a second zone to which the second reducing stream is fed to generate a second gas, including synthesis gas, according to the parameters and conditions described above.

[0128] According to yet another embodiment, the synthesis gas production can be carried out using a reactor including a plurality of first zones 12 and a shared second zone 14 (FIGS. 5 and 6). More specifically, in this embodiment, each first zone 12 of the reactor is fed with an oxidizing stream and a first reducing stream to produce a first gas in each first zone, and the shared second zone 14 is fed with a second reducing stream 24 to receive the first gas produced in each first zone and generate a second gas in the shared second zone. In this method, the first zones 12 operate in parallel, each including an oxygen flame. According to some embodiments, the second reducing stream 24 may be fed to the shared second zone 14 via at least one inlet, which may be located in a peripheral zone of the second zone. However, multiple inlets may be provided for feeding the second reducing stream 24 to the second zone. For example, the inlets may be provided in several positions in the peripheral zone of the second zone near the bottom of its inner wall.

[0129] The synthesis gas obtained from the reactor outlet is generally cooled and then used for subsequent chemical synthesis. The method described herein makes it possible to generate a synthesis gas based on balanced CO and H2, i.e. with a suitable ratio of CO and H2, which then allows the production of a variety of products by conventional chemical synthesis. Thus, by controlling the nature and amount of the reagents used (e.g. the flow rates of the gas streams), it is possible to generate a synthesis gas with an adapted ratio of CO and H2 so that the mixture can be used for subsequent chemical synthesis. By controlling the temperature and finally the pressure of each reaction zone of the reactor, it is also possible to influence the ratio of CO and H2 in the synthesis gas. This pressure is generally around atmospheric pressure and can vary typically between 1 and 5 bar (absolute) for each zone. According to some embodiments, the absolute pressure of the first zone may be in the range of 1 to 5 bar, or 1 to 4 bar, or 1 to 3 bar, or 1 to 2 bar. The absolute pressure in the first zone may be about 1 bar, about 2 bar, about 3 bar, about 4 bar, about 5 bar, or any pressure value between these values. According to some embodiments, the absolute pressure in the second zone may be 1-5 bar, or 1-4 bar, or 1-3 bar, or 1-2 bar. The absolute pressure in the second zone may be about 1 bar, about 2 bar, about 3 bar, about 4 bar, about 5 bar, or any pressure value between these values. In some embodiments, the pressure in the first zone and the pressure in the second zone are very close or even the same.

[0130] In some embodiments, the synthesis gas produced by the methods of the present invention can be used to produce many basic chemical products and fuels. These products include methanol and hydrocarbons such as those found in motor gasoline, diesel, and kerosene, to name a few. In some embodiments, the synthesis gas produced by the methods of the present invention is used as a reducing agent for the metallurgical industry, especially for the direct reduction of metal oxides, especially iron oxide.

[0131] Thus, there are several advantages to the above-described method for producing synthesis gas and the reactor that can be used to carry out the method. The reagents are readily available and can come from renewable sources, making the method simple to implement. There is no need to use solid catalysts. It is possible to use hydrogen from a variety of sources, and therefore it is possible to reduce costs by using hydrogen produced at a lower cost. It is possible to use hydrogen with a lower carbon footprint (e.g., green, blue, turquoise, and / or pink hydrogen). Thus, for example, if green hydrogen is produced at a higher cost than blue hydrogen, the amount of green hydrogen used in the method can be reduced by using blue hydrogen in addition to green hydrogen, or simply using blue hydrogen only. The method also takes advantage of the water vapor generated during the CO2 reduction and uses this to produce synthesis gas. This avoids the need to condense large amounts of water as is the case in other known methods, and avoids the indirect loss of hydrogen due to water vapor. The method has a beneficial effect on the environment by recycling CO2 while allowing the efficient conversion of other carbon sources, e.g., fossil hydrocarbons such as methane. Finally, the method provides significant overall conversion of carbon entering the reactor to CO, while allowing flexibility in the relative and in situ conversion of CO2 and hydrocarbons. EXAMPLES

[0132] As examples, laboratory tests were carried out to demonstrate the concepts proposed in this application. These examples are based on a setup similar to that shown in Figure 7. The inputs of each of the streams 16, 18, and 24 are in the same physical horizontal plane. Streams 16 and 18 define a first reaction zone, and stream 24 defines a second reaction zone, the latter at the periphery of the first reaction zone.

[0133] The reactor consisted of an alumina outer tube (99.8% Al2O3) with an inner diameter of 13.54 mm and an outer diameter of 19.05 mm over a length of 212 mm. The reaction volume was 33 cm 3The gas enters through three spaces, a central space and two annular spaces, defined by the ends of two concentric alumina tubes, a central tube and an inner tube, each having the following dimensions: inner diameter 6.31 mm, outer diameter 4.11 mm for the central tube, and inner diameter 8.48 mm, outer diameter 12.34 mm for the inner tube. The ends of the central tube define the flow path of the oxidation stream 16 of the first zone of the reactor, and the annular space between the outer diameter of the central tube and the inner diameter of the inner tube defines the flow path of the reduction stream 18 of the first reaction zone. Finally, the annular space between the inner diameter of the outer tube and the outer diameter of the inner tube defines the flow path of the second reduction stream of the second reaction zone 24.

[0134] The alumina outer tube defining the wall of the reaction chamber is surrounded along the entire length of the reactor by a cylindrical calcium silicate-based thermal insulation jacket (thermal conductivity 0.3 W / mK, density 1.36 g / cm) with an outer diameter of 132 mm and an inner diameter of 20 mm. 3 ) which is itself surrounded by an insulating jacket (not shown in FIG. 7). The purpose of the insulating jacket is to provide some insulation to the reactor to minimize heat loss.

[0135] In each of these embodiments, oxygen is mixed with CO2, and this mixture forms the oxidation stream 16 of the first reaction zone. In the embodiments, hydrogen is fed to form the reduction stream 18 of the first zone. In the first and third embodiments, methane is fed to form the reduction stream 24 of the second zone, and in the second embodiment, a mixture of methane and steam forms the reduction stream 24 of the second zone. The methane-steam mixture is produced by an apparatus for high temperature saturation of a methane stream in the presence of a controlled water flow.

[0136] The examples are shown in Table 1, where for each gas supplied the number of the gas stream in question (16, 18 or 24) is given in brackets, along with the volumetric flow rate of that gas (sL / min, i.e. flow rate at 25° C. and 1 atm). A sample of the gas leaving the reactor is dried by rapid cooling (to −1° C.) and then sent to the mass spectrometry system. Gas analysis is therefore performed on a dry basis.

[0137] The table shows the analysis of the gases leaving the reactor determined by mass spectrometry. From the volumetric composition of the gases, the ratio S is calculated, which is equal to (H2-CO2) / (CO+CO2), based on the respective volume fractions of each of the gases H2, CO2 and CO in the dry gas obtained. The conversion rates of methane and CO2 are calculated from the atomic balance and the composition of the gases (dry basis) obtained from the gas analysis by mass spectrometry. The table also shows the conversion rates to CO of the total carbon entering the reactor, i.e. the carbon contained in the CO2 feed and the carbon contained in the CH4 feed.

[0138] The table also shows the temperatures measured using a thermocouple located 25 mm from the reactor outlet 28. The measured temperature values ​​are used to calculate the average residence time of the reactants (i.e. all fed gases) in the reactor based on the reaction volumes above and taking into account that the reactor is operating at atmospheric pressure.

[0139] It should be noted that after the test, no measurable amount of carbon was observed in the reactor.

[0140] Table 1 shows the results obtained for each of the two examples. [Table 1]

[0141] The results of Examples 1, 2 and 3 shown in Table 1 demonstrate the flexibility of the method and system according to the present invention, which is essentially due to the geometrical differentiation of the reaction zones in the reactor. In particular, the configuration used in these examples (see FIG. 7) offers the advantage of obtaining a fairly wide and flexible range of relative and in situ conversion of CH4 and CO2, while ensuring a significant overall conversion (at least 70%) of the carbon entering the reactor.

[0142] The results of Examples 1 and 2 show that the supply of water steam is not crucial to achieve high methane conversion. In fact, the addition of water to the second zone only slightly increases the conversion of methane (from 79% to 83%) (by reaction (E)), but leads to a decrease in the conversion of CO2, probably by promoting the reverse reaction of reaction (A). The results of Example 3 show that high equivalent conversions of CH4 and CO2 can be achieved by adding a certain amount of excess hydrogen to the first zone (9 vs. 6 sL / min). Indeed, this excess hydrogen seems to help to convert CO2 more efficiently in the first zone by reaction (A). In this same Example 3, it is observed that the conversion of CH4 is not significantly affected by the increase in the conversion of CO2, due to the fact that this CH4 is fed separately to the second zone.

[0143] Although some embodiments of the technology have been described above, the technology is not limited to these only embodiments. Some modifications can be made to any of the above embodiments without departing from the intended scope of the technology.

Claims

1. Carbon monoxide (CO) and hydrogen (H ２ A method for producing synthesis gas containing ), wherein the method is Oxygen (O ２ Oxidizing fluid containing ) and hydrogen (H ２ A step of supplying a first reducing flow containing ) to at least a first reaction zone of at least one reactor, wherein the oxidizing flow and / or the first reducing flow contains CO ２ The process further includes a first carbon source, The reaction between the oxygen in the oxidation stream and the hydrogen in the first reduction stream generates an oxygen flame in the first zone, and by bringing the oxidation stream and the first reduction stream into contact with the oxygen flame, at least carbon monoxide (CO) and water vapor (H) are produced. ２ A step of generating a first gas containing O), A step of supplying the reactor with a second reducing stream containing a second carbon source containing at least one hydrocarbon, A step in which, in the second reaction zone of the reactor, a second gas containing the synthesis gas is generated from the first gas coming from the first reaction zone and the second reducing flow by a reaction involving at least one hydrocarbon. A method that includes this.

2. i) The oxidation flow is oxygen and CO ２ The method according to claim 1, comprising, or ii) the first reducing stream comprising hydrogen (H₂) and CO₂, and optionally water vapor, in an H₂O / H₂ ratio of 0 to 1, or iii) the oxidizing stream and the first reducing stream each comprising CO₂, or iv) the oxidizing stream alone comprising CO₂.

3. The CO ２ is derived from industrial waste, biologically originated CO from biogas ２ or CO directly collected from ambient air ２ or a mixture thereof, the method according to claim 1.

4. The hydrogen present in the first reducing stream i) Produced from the electrolysis of water, or ii) In an electrolytic cell powered by electricity generated from renewable sources or nuclear energy, the electrolysis reaction of water produces, or iii) In a process in which the generated CO2 is at least partially captured and sequestrated, it is produced from a steam reforming reaction of natural gas or methane, iv) containing hydrogen produced from the thermal decomposition reaction of methane, v) Hydrogen produced from the electrolysis of water in an electrolytic cell powered by electricity generated from renewable sources or nuclear energy, and hydrogen produced from the steam reforming of natural gas or methane in a process in which the generated CO2 is at least partially captured and sequestered, The combination of vi) ii) and iv), the combination of iii) and iv), or the combination of iv) and v), The method according to claim 1.

5. i) the hydrogen, oxygen, and CO ２ However, at least 2 H ２ / O ２ The molar ratio and at least 1.8 H ２ / CO ２ The first zone is supplied with the following molar ratio, ii) The oxygen and CO2 are supplied to the first zone in a molar ratio of at least 0.5 O2 / CO2. The method according to claim 1.

6. The method according to any one of claims 1 to 5, wherein the generation of the synthesis gas comprises steam reforming the hydrocarbon using the water vapor contained in the first gas, and / or the second reducing stream further contains water vapor, and the generation of the synthesis gas comprises steam reforming the hydrocarbon using the water vapor contained in the first gas and the water vapor contained in the second reducing stream.

7. The method according to any one of claims 1 to 5, wherein the second carbon source comprises methane.

8. The second reduction stream contains methane (CH4). ４ ) and hydrogen (H) if necessary ２ ) to H 0 to 2.5 ２ / CH ４ The method according to any one of claims 1 to 5, wherein the second reducing stream contains methane (CH4) and optionally hydrogen (H2), and the molar ratio of the supplied CH4 to the total amount of H2 supplied to the two zones is 0.1 to 1.

9. The second reducing flow is when the molar composition of the synthesis gas is H ２ / CO≧2 and (H ２ -CO ２ ) / (CO+CO ２ The method according to any one of claims 1 to 5, further comprising hydrogen (H₂) in an amount that balances such that ) ≥ 2, and / or the second reducing stream comprising methane (CH₄) and optionally water vapor (H₂O), wherein the molar ratio of water vapor (H₂O) to CH₄ is ​​0 to 2.

10. In the first zone, at least carbon monoxide (CO) and water vapor (H ２ The method according to any one of claims 1 to 5, wherein the generation of the first gas containing O) is carried out at a temperature of at least 1000°C and up to 2400°C, and the step of generating the synthesis gas in the second zone is carried out at a temperature of at least 700°C and up to 1500°C.

11. The method according to any one of claims 1 to 5, wherein the step of generating the synthesis gas in the second zone is performed at a temperature lower than the temperature of the first zone.

12. The method according to any one of claims 1 to 5, wherein the generation of carbon monoxide and water vapor in the first zone and the generation of the second gas, including the synthesis gas, in the second zone are carried out in the absence of a catalyst.

13. The second gas generated in the second zone is used as synthesis gas and residual CO ２ The method according to any one of claims 1 to 5, further comprising, and further comprising recycling a portion of the second gas in the first reducing flow, and further optionally comprising, cooling the portion of the second gas to be recycled before recycling.

14. Carbon monoxide (CO) and hydrogen (H ２ A system for producing synthesis gas comprising, wherein the system comprises at least one reactor, the reactor comprising at least one first reaction zone and at least one second reaction zone, In the first reaction zone, oxygen (O ２ Oxidizing fluid containing ) and hydrogen (H ２ A first reducing flow containing ) is supplied, and the oxidizing flow and / or the first reducing flow is CO ２ The system further comprises a first carbon source, wherein the reaction between the oxygen in the oxidation flow and the hydrogen in the first reduction flow generates an oxygen flame in the first zone, and by bringing the oxidation flow and the first reduction flow into contact with the oxygen flame, at least carbon monoxide (CO) and water vapor (H) are produced. ２ A first gas containing O) is produced, A system in which a second reducing stream containing a second carbon source containing at least one hydrocarbon is supplied to the second reaction zone, and a second gas containing the synthesis gas is generated in the second reaction zone by a reaction involving the at least one hydrocarbon from the first gas coming from the first reaction zone and the second reducing stream.

15. i) The oxidation flow is oxygen and CO ２ The system according to claim 14, comprising, or ii) the first reducing stream comprising hydrogen (H₂) and CO₂, and optionally water vapor, in an H₂O / H₂ ratio of 0 to 1, or iii) the oxidizing stream and the first reducing stream each comprising CO₂, or iv) the oxidizing stream alone comprising CO₂.

16. The hydrogen present in the first reducing stream i) Produced from the electrolysis of water, or ii) In an electrolytic cell powered by electricity generated from renewable sources or nuclear energy, the electrolysis reaction of water produces, or iii) In a process in which the generated CO2 is at least partially captured and sequestrated, it is produced from a steam reforming reaction of natural gas or methane, iv) containing hydrogen produced from the thermal decomposition reaction of methane, v) Hydrogen produced from the electrolysis of water in an electrolytic cell powered by electricity generated from renewable sources or nuclear energy, and hydrogen produced from the steam reforming of natural gas or methane in a process in which the generated CO2 is at least partially captured and sequestered, The combination of vi) ii) and iv), the combination of iii) and iv), or the combination of iv) and v), The system according to claim 14.

17. i) the hydrogen, oxygen, and CO ２ However, at least 2 H ２ / O ２ The molar ratio and at least 1.8 H ２ / CO ２ The system according to claim 14, wherein oxygen and CO2 are supplied to the first zone in a molar ratio of O2 / CO2, or ii) the oxygen and CO2 are supplied to the first zone in a molar ratio of at least 0.5 O2 / CO2.

18. The system according to any one of claims 14 to 17, wherein the generation of the synthesis gas comprises steam reforming the hydrocarbon using the water vapor contained in the first gas, and / or the second reducing stream further contains water vapor, and the generation of the synthesis gas comprises steam reforming the hydrocarbon using the water vapor contained in the first gas and the water vapor contained in the second reducing stream.

19. The system according to any one of claims 14 to 17, wherein the second carbon source comprises methane.

20. At least carbon monoxide (CO) and water vapor (H ２ The system according to any one of claims 14 to 17, wherein during the generation of the first gas containing O), the first zone is at a temperature of at least 1000°C and up to 2400°C, and during the generation of the synthesis gas, the second zone is at a temperature of at least 700°C and up to 1500°C, and the generation of the synthesis gas in the second zone is performed at a temperature lower than that of the first zone.

21. The system according to any one of claims 14 to 17, wherein the generation of carbon monoxide and water vapor in the first zone and the generation of the second gas, including the synthesis gas, in the second zone of the reactor are carried out in the absence of a catalyst.

22. The system according to any one of claims 14 to 17, wherein the first zone and the second zone are each cylindrical in shape, and the system includes a first means for supplying the oxidation flow to the lower central part of the first zone and a second means for supplying the first reduction flow to the lower part of the first zone at the periphery of the oxidation flow.

23. The system according to any one of claims 14 to 17, comprising a third means for supplying the second reducing flow to the second zone, wherein the first zone and the second zone are each cylindrical in shape, and the third means optionally comprises an opening formed by an annular space extending between the outer wall of the first zone and the inner wall of the second zone, in the upper region of the first zone and the lower region of the second zone.

24. Use of synthesis gas produced by the method according to any one of claims 1 to 5 or by the system according to any one of claims 14 to 17, i) for the production of chemical products or fuels, ii) for the production of synthetic hydrocarbons, or iii) for use as a reducing agent in the metallurgical industry.

25. CO ２ Use of the system according to any one of claims 14 to 17 for the treatment of gaseous industrial emissions containing

Images