PROCESS FOR PRODUCING SUSTAINABLE FUEL USING CARBON MONOXIDE

Description

Field of the invention

[0001] The invention relates to methods for producing sustainable fuel.Background of the invention

[0002] Climate change and the on-going energy transition makes it mandatory to replace fossil-based energy sources. In this context various aspects will be important for society to reach Net Zero by 2050 as currently desired. For example, the valorisation of alternative feedstocks is expected to contribute towards the circular economy and / or reduce the carbon dioxide (CO 2 ) footprint associated with the final product. However, while many alternative fuels and chemicals are sort after, drop in solutions from alternative feedstocks would allow for existing infrastructure to be maintained.

[0003] In this context even the valorisation of CO 2 as a feedstock is considered, sourced from flue gas, bio sources and even direct air capture. Upgrading of CO 2 to chemicals such as methanol has already received some attention to yield sustainable fuel for various applications. However, some applications regularly lead to enhanced requirements for the sustainable fuel. For example, aviation fuel, i.e., fuel to power aircraft, regularly requires to contain larger hydrocarbons and aromatics. This is because larger hydrocarbons and aromatics regularly improve the cold flow properties of the aviation fuel. Such improved cold flow properties prevent fuel freezing at low temperatures of for example -40°C, which are typical for cruising altitudes of the powered aircrafts. In attempts to upgrade CO 2 , larger hydrocarbons and aromatics are however regularly more difficult to achieve.

[0004] In a different approach, bio conversion and syngas upgrading via Fischer-Tropsch (FT) are also considered as an alternative to a fossil fuel feedstock. Such routes may appear attractive for diesel and gasoline production. However, they are not suitable for 100% aviation fuel, as they crucially lack aromatic content and hence are applied as a blend.

[0005] Thus far, there are no established routes of producing a 100% sustainable aviation fuel by bio conversion or syngas upgrading via FT.

[0006] Further in the search for sustainable fuel and in particular in the search for aviation fuel, hydrodeoxygenation of fatty acids / triglycerides, CO 2 - or bio-sourced syngas upgrading, or bio-olefin oligomerisation have been researched at various Technology Readiness Levels (TRLs). However, for each of these routes, the major product is regularly long hydrocarbon chains and is typically only suitable for up to 50% blend to meet requirements for aviation fuel. This is because these routes do regularly not yield aromatics which are however also required to improve the cold flow properties of aviation fuel.

[0007] EP 3 243 891 discloses a method for producing a fuel comprising the steps of converting CO 2 into hydrocarbons via a reverse water gas shift reaction and Fischer-Tropsch reaction. Nezam I et al., Journal of CO2 Utilization, vol. 45, 20 January 2022, pages 1-21, discloses a method for producing a fuel comprising the steps of converting CO 2 into C 1 -C 6 olefins using a bifunctional catalyst and converting C 1 -C 6 hydrocarbons into aromatics. WO 2017 / 074843 discloses a method comprising the steps of converting CO 2 into CO using a reverse water gas shift catalyst at 600°C, optionally separating at least of portion of H 2 O from the product stream by condensation to provide as purified syngas and converting CO into light olefins.

[0008] Overall, there remains a general desire for an improved method for producing sustainable fuel.Problem underlying the invention

[0009] It is an object of the present invention to provide a method for producing sustainable fuel which at least partially overcomes the drawbacks encountered in the art.

[0010] It is in particular an object of the present invention to provide a method for producing sustainable fuel which reduces the CO 2 footprint associated with the produced sustainable fuel.

[0011] It is furthermore an object of the present invention to provide a method for producing sustainable fuel which allows for existing infrastructure to be maintained.

[0012] It is moreover an object of the present invention to provide a method for producing sustainable fuel which has an improved energy efficiency and / or an improved cost efficiency.

[0013] It is also an object of the present invention to provide a method for producing sustainable fuel which has an improved carbon efficiency, i.e., a method which minimizes carbon dioxide equivalents emissions to its output.

[0014] It is additionally an object of the present invention to provide a method for producing sustainable fuel which has an increased aromatics content.

[0015] It is in particular an object of the present invention to provide a method for producing sustainable fuel which meets the requirements for aviation fuel.Disclosure of the invention

[0016] Surprisingly, it has been found that the problem underlying the invention is overcome by methods according to the claims. Further embodiments of the invention are outlined throughout the description.

[0017] Subject of the invention is a method for producing sustainable fuel according to claim 1, comprising the steps: (i) converting CO 2 into CO using a reverse water gas shift catalyst, (ii) converting CO from step (i) into C 1 -C 6 hydrocarbons using a Fischer-Tropsch catalyst, and (iii) converting C 1 -C 6 hydrocarbons from step (ii) into aromatics using a zeolite-based catalyst. further comprising a cooling step in which CO from step (i) is cooled before being converted in step (ii).

[0018] Logically, steps (i), (ii) and (iii) are carried out in the given order, i.e., first step (i), thereafter step (ii) and thereafter step (iii). However, additional steps before or after each of steps (i), (ii) and (iii) may also be comprised by the method according to the present invention.

[0019] In step (i), carbon dioxide (CO 2 ) is converted into carbon monoxide (CO). The conversion occurs in the presence of a reverse water gas shift catalyst. As used herein, a reverse water gas shift catalyst promotes a reverse water gas shift reaction. In other words, the reverse water gas shift catalyst lowers the activation energy of a reverse water gas shift reaction. As used herein, a reverse water gas shift reaction is a reaction which comprises a reaction of CO 2 with hydrogen (H 2 ) to yield CO and water (H 2 O). The reverse water gas shift reaction, and hence step (i), comprises the following reaction: CO 2 + H 2 → CO + H 2 O

[0020] In step (ii), CO is converted into short hydrocarbons, namely C 1 -C 6 hydrocarbons. C 1 -C 6 hydrocarbons are compounds containing at least one and at most six carbon atoms, i.e., 1, 2, 3, 4, 5 or 6 carbon atoms, and additionally hydrogen. The C 1 -C 6 hydrocarbons can be saturated and / or unsaturated hydrocarbons. Saturated C 1 -C 6 hydrocarbons are regularly linear, branched or cyclic alkyls. Unsaturated C 1 -C 6 hydrocarbons, more precisely unsaturated C 2 -C 6 hydrocarbons, are regularly linear, branched or cyclic alkenyls or alkynyls. The C 1 -C 6 hydrocarbons may comprise heteroatoms like oxygen (O), sulfur (S), nitrogen (N) or phosphorous (P). However, according to the present invention, the C 1 -C 6 hydrocarbons are preferably free from heteroatoms like oxygen (O), sulfur (S), nitrogen (N) and phosphorous (P).

[0021] In step (ii), CO is converted using a Fischer-Tropsch catalyst (or FT-catalyst), that is, in the presence of a Fischer-Tropsch catalyst. As used herein, a Fischer-Tropsch catalyst promotes a Fischer-Tropsch reaction. In other words, the Fischer-Tropsch catalyst lowers the activation energy of a Fischer-Tropsch reaction. As used herein, a Fischer-Tropsch reaction is a reaction which comprises a reaction of CO with hydrogen (H 2 ) to yield at least the C 1 -C 6 hydrocarbons. During the reaction, the hydrocarbons regularly grow in a repeated sequence in which hydrogen atoms are added to carbon and oxygen, the C-O bond of CO is split and a new C-C bond is formed. For one -CH 2 - group, the reaction can be given as follows:         CO + 2 H 2 → (CH 2 ) + H 2 O

[0022] Such a Fischer-Tropsch reaction can for example comprise the following reaction steps: associative adsorption of CO by the FT-catalyst; splitting of the C-O bond; dissociative adsorption of 2 H 2 by the FT-catalyst; transfer of 2 H to the oxygen to yield H 2 O; desorption of H 2 O from the FT-catalyst; transfer of 2 H to the carbon to yield CH 2 .

[0023] In step (iii), C 1 -C 6 hydrocarbons from step (ii) are converted into aromatics. As used herein, aromatics are aromatic in the sense of the IUPAC Gold Book. More specifically, aromatics are cyclically conjugated molecular entities with a stability (due to delocalization) significantly greater than that of a hypothetical localized structure (e.g., Kekulé structure). Such cyclically conjugated molecular entities have aromaticity. A method for determining aromaticity can in particular be the observation of diatropicity in the 1< H-NMR spectrum.

[0024] In step (iii), C 1 -C 6 hydrocarbons from step (ii) are converted using a zeolite-based catalyst, that is, in the presence of a zeolite-based catalyst. As used herein, zeolite-based means that the catalyst comprises zeolite. The zeolite-based catalyst is preferably composed of ≥ 50 wt.%, more preferably of ≥ 60 wt.%, still more preferably of ≥ 70 wt.%, even more preferably of ≥ 80 wt.% and in particular preferably of ≥ 90 wt.% of zeolite; the weight percentages are based on the total weight of the zeolite-based catalyst. In a particular case, the zeolite-based catalyst consists of zeolite. As used herein, zeolite is given the same meaning as usual in the art. In particular, a zeolite has an aluminosilicate matrix with a tetrahedral arrangement of silicon (Si 4+< ) and aluminium (Al 3+< ) cations surrounded by four oxygen anions (O 2-< ). This regularly results in a macromolecular three-dimensional structure of SiO 2 and AlO 2 tetrahedral building blocks. As the AlO 2 tetrahedral building blocks are negatively charged, zeolites regularly comprise additional charge-compensating cations, e.g., alkali metal cations, alkaline earth metal cations, protons and / or ammonia cations.

[0025] In steps (i) to (iii), the afore-listed catalysts are used, namely, a reverse water gas shift catalyst, a Fischer-Tropsch catalyst and a zeolite-based catalyst. According to the present invention, all these catalysts are used in solid form. Here, solid form refers to the aggregation state of the respective catalysts, in particular under normal conditions of 298.15 K and 101.3 kPa.

[0026] The method for producing sustainable fuel according to the present invention uses CO 2 as a feedstock, which is at least partially converted and is hence not emitted to the environment. The inventive method can thus help to reduce the CO 2 footprint associated with the produced sustainable fuel. Herein, the CO 2 footprint refers to the amount of carbon dioxide released into the atmosphere.

[0027] The method for producing sustainable fuel according to the present invention can be carried out in one or more reaction vessels, especially reactors, which have previously been used for conversion of fossil feedstock. The inventive method may thus allow for existing infrastructure to be maintained.

[0028] The method for producing sustainable fuel according to the present invention combines ways of producing larger hydrocarbons and aromatics and yields a sustainable fuel comprising such larger hydrocarbons and aromatics in one single continuous reaction sequence. The inventive method can thereby lead to improved energy efficiency and / or improved cost efficiency of the fuel production.

[0029] The method for producing sustainable fuel according to the present invention combines ways of producing larger hydrocarbons and aromatics and regularly yields a sustainable fuel comprising such larger hydrocarbons and aromatics. The inventive method can thereby produce sustainable fuel which meets the requirements for aviation fuel.

[0030] The method according to the present invention further comprises a cooling step in which CO from step (i) is cooled before being converted in step (ii). The cooling step lowers requirements to extract heat from the reaction vessel, like a reactor, in which step (ii) is carried out, without however disadvantageously reducing the conversion rate of CO in step (ii). Preferably, during the cooling step between step (i) and step (ii) liquid water is removed resulting in the water-poor CO stream. The Fischer-Tropsch step (ii) is a highly exothermic reaction step and tends to increase the temperature in the reactor, requiring cooling of the reactor content. Hence it is preferred that the CO stream enters step (ii) cooler than it leaves step (i). Moreover, when significant amounts of water are still present in the CO stream, the Fischer-Tropsch catalyst will perform the water-gas shift reaction (CO + H 2 O → CO 2 + H 2 ), being also exothermic and producing heat. It is preferred that the CO stream is poor in water content. Further, the conversion rate of CO in step (ii) may even increase. The cooling step thus further improves the energy efficiency and / or the cost efficiency of the fuel production. In this context, cooling of the CO naturally means that the temperature of the CO obtained in step (i) is lowered before the CO is used in step (ii) for a conversion into C 1 -C 6 hydrocarbons. Hence, also the notation T (CO , step (i)) > T (CO, step (ii)) can be used to indicate that there is an active cooling of the CO between step (i) and step (ii). Moreover, with a maintained or even increased conversion rate of CO in step (ii) the conversion thereof into aromatics in subsequent step (iii) may also be improved, i.e., the aromatics yield can be increased.

[0031] In the method according to the present invention, the CO from step (i) is cooled (in the cooling step) from a temperature of ≥ 500°C to a temperature of ≤ 350°C before being converted in step (ii), preferably from a temperature of ≥ 500°C to a temperature of ≤ 300°C and more preferably from a temperature of ≥ 500°C to a temperature of ≤ 250°C. An advantageously efficient conversion of CO 2 into CO in the reverse water gas shift reaction in step (i) will regularly lead to a product stream of increased temperature, in particular an increased temperature of ≥ 500°C. It has been found that in order to increase the efficiency of the Fischer-Tropsch reaction and to increase the yield of the C 1 to C 6 hydrocarbons in step (ii), in particular the yield of unsaturated C 2 to C 6 hydrocarbons, it is advantageous to lower the temperature of CO from 500°C or more to 350°C or less, even better to 300°C or less and especially to 250°C or less. A respective lowering of the temperature of the CO can then ultimately also increase the yield of aromatics obtained in step (iii).

[0032] In the context of the cooling step, it is especially preferred that step (i) is carried out in a first reactor and that step (ii) is carried out in a physically separated second reactor, wherein the cooling takes place between the CO leaving the first reactor and the CO entering the second reactor. It is especially preferred that in the cooling step liquid water is removed from the CO stream.

[0033] It is preferred that in a method according to the present invention, in step (i) the CO 2 is at least partially reacted with H 2 , and / or in step (ii) the CO is at least partially reacted with H 2 . A reaction with H 2 in either step can lead to an increased conversion of CO 2 and / or CO, which can further reduce the CO 2 footprint. Additionally, an increased conversion of CO 2 and / or CO can further improve the energy efficiency and / or the cost efficiency of the fuel production.

[0034] It is preferred that in a method according to the present invention, the reverse water gas shift catalyst comprises Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof, preferably in oxidic form (Fe-oxide, Co-oxide, Cu-oxide, Cr-oxide, Ni-oxide, Ir-oxide, Mn-oxide, or mixtures thereof) or in metallic form supported on metal oxide(s) or supported on carbon. It is preferred that the reverse water gas shift catalyst comprises Ni, even more preferably comprises Ni supported on metal oxide, in particular Ni / Al 2 O 3 . It is also preferred that the reverse water gas shift catalyst comprises Fe, even more preferably comprises an Fe-oxide, in particular Fe 2 O 3 or Fe 3 O 4 . The use of a reverse water gas shift catalyst which comprises Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof can lead to an increased conversion of CO 2 in step (i), which can further reduce the CO 2 footprint. Additionally, such a reverse water gas shift catalyst comprising Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof may already be used in existing infrastructure. Hence, such a reverse water gas shift catalyst comprising Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof can help to maintain existing infrastructure. The mentioned effects can be particularly pronounced when the reverse water gas shift catalyst comprises either Ni supported on metal oxide, in particular Ni / Al 2 O 3 , or an Fe-oxide, in particular Fe 2 O 3 or Fe 3 O 4 .

[0035] It is similarly preferred that in a method according to the present invention, the reverse water gas shift catalyst comprises Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof in the form of sulphide(s) or carbide(s).

[0036] It is further preferred that in a method according to the present invention, the reverse water gas shift catalyst comprises Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof, preferably in the form of oxides, sulphides or carbides, or preferably in metallic form supported on metal oxide(s) or supported on carbon, wherein the water gas shift catalyst further comprises a promotor metal species selected from alkali metals and alkaline earth metals.

[0037] It is also preferred that in a method according to the present invention, the reverse water gas shift catalyst is selected from oxide catalysts, preferably selected from CeO 2 , CuO, ZnO, Al 2 O 3 , Fe 2 O 3 , Cr 2 O 3 , In 2 O 3 , and MnO 2 , composite oxides, preferably selected from CuO / ZnO / Al 2 O 3 , NiO / CeO 2 , ZnO / Al 2 O 3 , ZnO / Cr 2 O 3 , CuO x / CeO 2 , and In 2 O 3 -CeO 2 , spinel oxides, preferably selected from ZnAl 2 O 4 , ZnCr 2 O 4 , Cu Al 2 O 4 , and Co Al 2 O 4 , solid solution oxides, preferably selected from Zn x Zr 1-x O 2-y , Ce 0.5 Zr 0.5 O 2 , NixCe 0.75 Zr 0.25-x O 2 , and perovskite-type oxides, preferably selected from BaZr 0.8 Y 0.16 Zn 0.04 O3, La 0.75 Sr 0.25 CoO 3-d , La 0.75 Sr 0.25 FeO 3 , La 0.75 Sr 0.25 Fe 1-Y CuYO 3 , LaNiO 3 , La 0.9 Sr 0.1 NiO 3+d , La 0.9 Sr 0.1 FeO 3-d , La 0.9 Sr 0.1 Ni 0.5 Fe 0.5 O 3-d , La 0.75 Sr 0.25 Cr 0.5 Mn 0.5 O 3-d , and SrCe 0.9 Y 0.1 O 3-d .

[0038] It is also preferred that in a method according to the present invention, the reverse water gas shift catalyst is selected from metals, which metals are preferably selected from Pt, Pd, Au, Rh, Ru, Cu, Ni, Re, Co, Fe, and Mo, which are immobilized on a metal oxide support material, which support material is preferably selected from CeO 2 , TiO 2 , Al 2 O 3 , ZnO, ZrO 2 , and SiO 2 . It is additionally preferred that such a water gas shift catalyst further comprises a promotor metal species selected from alkali metals and alkaline earth metals.

[0039] It is preferred that in a method according to the present invention, the Fischer-Tropsch catalyst comprises Fe and / or Co, preferably Co. It is more preferred that the Fischer-Tropsch catalyst comprises Fe or Co which is supported on an oxide, in particular Co supported on an oxide. The use of a Fischer-Tropsch catalyst which comprises Fe or Co can lead to an increased conversion of CO in step (ii), which can further improve the energy efficiency and / or the cost efficiency of the fuel production. Additionally, such a Fischer-Tropsch catalyst comprising Fe or Co may already be used in existing infrastructure. Hence, such a Fischer-Tropsch catalyst comprising Fe or Co can help to maintain existing infrastructure. The mentioned effects can be particularly pronounced when the Fischer-Tropsch catalyst comprises Co. Optionally, the Fe comprised by the Fischer-Tropsch catalyst is metallic Fe, the Co comprised by the Fischer-Tropsch catalyst is metallic Co, or the Fe comprised by the Fischer-Tropsch catalyst is metallic Fe and the Co comprised by the Fischer-Tropsch catalyst is metallic Co.

[0040] It is preferred that in a method according to the present invention, the zeolite-based catalyst in step (iii) comprises MFI-type zeolite (especially a ZSM-5 zeolite or an HZSM-5 zeolite), a CHA-type zeolite, a BEA-type zeolite, an MOR-type zeolite, an FAU-type zeolite, an MEL-type zeolite, an FER-type zeolite, an MTT-type zeolite, a TON-type zeolite, an ERI-type zeolite, an MTW-type zeolite, an MWW-type zeolite or a mixture thereof. More preferably, the zeolite-based catalyst in step (iii) comprises a ZSM-5 zeolite or an HZSM-5 zeolite, particularly preferable an HZSM-5 zeolite (an HZSM-5 zeolite is a proton-exchanged form of a ZSM-5 zeolite). The listed zeolite types are indicated here by the codes attributed by the International Zeolite Association. The use of a zeolite-based catalyst which comprises a zeolite of the listed types can lead to an increased conversion of C 1 -C 6 hydrocarbons into aromatics in step (iii), which can further improve the energy efficiency and / or the cost efficiency of the fuel production. Additionally, such a zeolite-based catalyst of the listed types may already be used in existing infrastructure. Hence, such a zeolite-based catalyst of the listed types can help to maintain existing infrastructure. The mentioned effects can be particularly pronounced when the zeolite-based catalyst in step (iii) comprises a ZSM-5 zeolite or an HZSM-5 zeolite, in particular an HZSM zeolite. Herein, a ZSM-5 zeolite and an HZSM-5 zeolite may be combinedly referred to as (H)ZSM-5 zeolite.

[0041] It is preferred that in a method according to the present invention, the zeolite-based catalyst in step (iii) comprises a metal-modified zeolite. As used herein, "metal-modified" means that the zeolite contains metal cations different from alkali metal cations and alkaline earth metal cations. Preferred metal cations are Zn-cations, Ga-cations, Ag-cations, Mo-cations and / or Re-cations. Accordingly, it is particularly preferred that the zeolite-based catalyst in step (iii) comprises a Zn-modified zeolite, a Ga-modified zeolite, an Ag-modified zeolite, an Mo-modified zeolite and / or a Re-modified zeolite. The metal-modified zeolite can be an MFI-type zeolite, a CHA-type zeolite, a BEA-type zeolite, an MOR-type zeolite, an FAU-type zeolite, an MEL-type zeolite, an FER-type zeolite, an MTT-type zeolite, a TON-type zeolite, an ERI-type zeolite, an MTW-type zeolite, an MWW-type zeolite or a mixture thereof. The use of a metal-modified zeolite can lead to an increased conversion of C 1 -C 6 hydrocarbons into aromatics in step (iii), which can further improve the energy efficiency and / or the cost efficiency of the fuel production. Additionally, such a metal-modified zeolite may already be used in existing infrastructure. Hence, such a metal-modified zeolite can help to maintain existing infrastructure.

[0042] It is preferred that in a method according to the present invention, another zeolite-based catalyst is present in step (i), more preferably a metal-modified zeolite, still more preferably a zeolite selected from a Zn-modified zeolite, a Ga-modified zeolite, an Ag-modified zeolite, an Mo-modified zeolite and / or a Re-modified zeolite. The "another" zeolite-based catalyst is different from the zeolite-based catalyst used in step (iii), i.e., it is a further zeolite-based catalyst. The presence of such a further zeolite-based catalyst in step (i) may further promote the reverse water gas shift reaction, which is especially the case for a metal-modified zeolite.

[0043] It is preferred that in a method according to the present invention, step (ii) additionally produces saturated C7+ hydrocarbons, preferably saturated C8+ hydrocarbons. Saturated C7+ hydrocarbons are saturated hydrocarbons which contain seven or more (≥7) carbon atoms. Saturated C8+ hydrocarbons are saturated hydrocarbons which contain eight or more (≥8) carbon atoms. Saturated C7+ hydrocarbons are particularly suitable for combustion in aircraft engines. Accordingly, when the saturated hydrocarbons comprise saturated C7+ hydrocarbons, the inventive method can be particularly suitable for producing sustainable fuel which meets the requirements for aviation fuel. The mentioned effect can be particularly pronounced when the saturated hydrocarbons comprise saturated C8+ hydrocarbons.

[0044] In the method according to the present invention, the C 1 -C 6 hydrocarbons comprise ethylene, propylene and / or butylene. When the C 1 -C 6 hydrocarbons produced in step (ii) comprise ethylene, propylene and / or butylene, the subsequent conversion thereof into aromatics in step (iii) can have a higher conversion rate and / or may require less energy. Accordingly, when the C 1 -C 6 hydrocarbons comprise ethylene, propylene and / or butylene, the energy efficiency and / or the cost efficiency of the fuel production can be improved.

[0045] It is preferred that in a method according to the present invention, methane (CH 4 ) is produced in step (i) which is subsequently at least partially converted into aromatics in step (iii). It is known that a conversion of CO 2 into CO over a reverse water gas shift catalyst may yield CH 4 as a by-product. Like the C 1 -C 6 hydrocarbons produced in step (ii), which may also comprise CH 4 , additional CH 4 produced in step (i) can subsequently be at least partially converted into aromatics in step (iii). This additional synthesis of aromatics in the inventive method can improve the aromatics content of the produced sustainable fuel, which can further help to meet the requirements for aviation fuel. Moreover, the by-product CH 4 from step (i) is not lost, but is rather valorised.

[0046] It is preferred that in a method according to the present invention, step (i) is performed at a temperature of 250 to 1000°C, more preferably of 300 to 750°C and still more preferably of 300 to 600°C. An increased temperature of 250 to 1000°C in step (i) can lead to an increased conversion of the CO 2 . This can help to further reduce the CO 2 footprint of the sustainable fuel produced by the inventive method. At the same time, too high temperatures may lead to a reduced energy efficiency and / or cost efficiency of the fuel production. Temperatures of 300 to 750°C and in particular of 300 to 600°C are therefore particularly preferred.

[0047] It is preferred that in a method according to the present invention, step (i) is performed at an absolute pressure of 0.1 to 10 MPa, more preferably of 1 to 4 MPa. An absolute pressure of 0.1 to 10 MPa in step (i) can lead to an increased conversion of the CO 2 . This can help to further reduce the CO 2 footprint of the sustainable fuel produced by the inventive method. At the same time, too high pressures may lead to a reduced energy efficiency and / or cost efficiency of the fuel production. Absolute pressures of 1 to 4 MPa are therefore particularly preferred.

[0048] It is preferred that in a method according to the present invention, a feed is fed in step (i) to the reverse water gas shift catalyst which has a molar ratio of hydrogen to carbon oxides, i.e., a molar ratio H 2 :CO x , of 0.5 to 12, more preferably of 1 to 3, with x being 1 and / or 2, with x preferably being 2. With such a molar ratio of hydrogen to carbon oxides of 0.5 to 12 an increased conversion of CO 2 in step (i) may be achieved which can help to further reduce the CO 2 footprint of the sustainable fuel produced by the inventive method. These effects can be particularly pronounced when the ratio of hydrogen to carbon oxides is 1 to 3.

[0049] It is preferred that in a method according to the present invention, H 2 O is produced in step (i) to yield a mixture comprising CO and H 2 O, wherein the H 2 O is at least partially separated from the CO in the cooling step. The separation of H 2 O can help to maintain or even increase the conversion rate of CO in step (ii). The separation of H 2 O can thus further improve the energy efficiency and / or the cost efficiency of the fuel production.

[0050] It is preferred that in a method according to the present invention, in step (i) a feed comprising the CO 2 is fed to the reverse water gas shift catalyst, wherein the feed is substantially free of CO. When the feed is substantially free of CO, preferably free of CO, the absent CO cannot interfere with the reverse water gas shift reaction. Accordingly, a substantial absence of CO and in particular a complete absence of CO in the feed fed to the reverse water gas shift catalyst can lead to an increased conversion of CO 2 in step (i), which can further reduce the CO 2 footprint.

[0051] In a method according to the present invention, step (ii) is performed at a temperature of 200 to 350°C, preferably of 250 to 350°C. An increased temperature in step (ii) can lead to an increased conversion of the CO. It is preferred that in a method according to the present invention, step (iii) is performed at a temperature of 200 to 500°C, more preferably of 250 to 350°C. An increased temperature of 200 to 500°C in step (iii) can lead to an increased conversion of the C 1 -C 6 hydrocarbons. At the same time, too high temperatures may lead to a reduced energy efficiency and / or cost efficiency of the fuel production. A temperature of 250 to 350°C is therefore respectively preferred.

[0052] It is preferred that in a method according to the present invention, step (ii) and / or (iii) is performed at an absolute pressure of 0.1 to 5 MPa, more preferably of 1 to 3 MPa. An absolute pressure of 0.1 to 5 MPa in step (ii) can lead to an increased conversion of the CO. An absolute pressure of 0.1 to 5 MPa in step (iii) can lead to an increased conversion of the unsaturated hydrocarbons. At the same time, too high pressures may lead to a reduced energy efficiency and / or cost efficiency of the fuel production. Absolute pressures of 1 to 3 MPa are therefore particularly preferred.

[0053] It is preferred that in a method according to the present invention, in step (i) the CO 2 is reacted with H 2 at a temperature of 250 to 1000°C using a reverse water gas shift catalyst which comprises Ni / Al 2 O 3 to yield a mixture comprising CO and H 2 O, the H 2 O is at least partially separated from the CO in a subsequent cooling step before the CO is converted in step (ii), in step (ii) CO from step (i) is reacted with H 2 using a Fischer-Tropsch catalyst which comprises Co to yield saturated C8+ hydrocarbons and unsaturated hydrocarbons which comprise at least one of ethylene, propylene and / or butylene, and in step (iii) the zeolite-based catalyst comprises an MFI-type or a BEA-type zeolite.

[0054] Such a preferred method for producing sustainable fuel according to the present invention can in particular help to reduce the CO 2 footprint associated with the produced sustainable fuel, may allow for existing infrastructure to be maintained, can lead to an improved energy efficiency and / or an improved cost efficiency of the fuel production and can produce sustainable fuel which meets the requirements for aviation fuel.Brief description of the drawings

[0055] Fig. 1 shows an exemplary reactor system in which a method according to the present invention can be carried out.Exemplary embodiment

[0056] The present invention is further described with reference to the accompanying Fig. 1 which shows an exemplary reactor system 10. The reactor system 10 has two reactors, namely a first reactor 1 and a second reactor 2, which are in fluid communication with each other. A first feed 3 is fed to the first reactor 1. Feed 3 comprises CO 2 and H 2 , and depending on the source of the CO 2 potentially minor amounts of CO (typically however 0% CO) and light hydrocarbons. The first reactor 1 contains a first catalyst bed 4 which contains Ni / Al 2 O 3 as a reverse water gas shift catalyst. The first reactor bed 1 is operated at elevated temperatures between 250 and 1000°C and absolute pressures between 0.1 and 10 MPa. The thereby produced CO and H 2 O are contained in a first product 5, together with unreacted H 2 and potentially unreacted CO 2 . Methane (CH 4 ) in low amounts may also be produced in reactor 1, in which case the first product 5 additionally contains CH 4 . The first product 5 is withdrawn from reactor 1 and is sent to reactor 2. In-between reactor 1 and reactor 2, a cooling device 6 may be arranged. The cooling device 6 cools the first product 5 to the reaction temperature of the second reactor 2. The cooling device 6 further separates at least some of the H 2 O produced in the first reactor 1 to give the second feed 7 which is fed to the second reactor 2. The second feed 7 contains CO, H 2 and potentially CO 2 and / or CH 4 . The second reactor 2 contains a second catalyst bed 8 which contains a Co-based Fischer-Tropsch catalyst (metallic Co on support) and an HZSM-5 zeolite catalyst. The second reactor 2 is operated at elevated temperatures between 200 and 500°C and absolute pressures between 0.1 and 5 MPa. In the second reactor 2, unreacted H 2 and CO generated from the first reactor are converted by the Fischer-Tropsch catalyst to C 1 -C 6 hydrocarbons, which contain C 2 -C 4 alkenyls, and additionally to saturated C7+ hydrocarbons. The C 1 -C 6 hydrocarbons are converted to aromatics by the HZSM-5 zeolite catalyst. As a result, a second product 9 is obtained which contains long hydrocarbons and aromatics, and potentially residual CO, H 2 , CO 2 and / or CH 4 . The second product 9 can be withdrawn from the second reactor as the overall product, i.e., as a sustainable (raw) fuel for further use or refinement thereof.List of reference signs

[0057] 1:First reactor 2:Second reactor 3:First feed 4:First catalyst bed 5:First product 6:Cooling device 7:Second feed 8:Second catalyst bed 9:Second product 10:Reactor system

Claims

1. A method for producing sustainable fuel, comprising the steps: (i) converting CO2 into CO using a reverse water gas shift catalyst, (ii) converting CO from step (i) into C1-C6 hydrocarbons using a Fischer-Tropsch catalyst, and (iii) converting C1-C6 hydrocarbons from step (ii) into aromatics using a zeolite-based catalyst, wherein the C1-C6 hydrocarbons comprise ethylene, propylene and / or butylene, further comprising a cooling step in which CO from step (i) is cooled before being converted in step (ii), wherein the CO from step (i) is cooled from a temperature of ≥ 500°C to a temperature of ≤ 350°C before being converted in step (ii), wherein step (ii) is performed at a temperature of 200 to 350°C.

2. The method according to claim 1, wherein step (i) is performed at a temperature of 250 to 1000°C.

3. The method according to claim 1 or 2, wherein H2O is produced in step (i) to yield a mixture comprising CO and H2O, wherein the H2O is at least partially separated from the CO in the cooling step.

4. The method according to any of the preceding claims, wherein the reverse water gas shift catalyst comprises Fe, Co, Cu, Cr, Ni, Ir, Mn or mixtures thereof.

5. The method according to any of the preceding claims, wherein the Fischer-Tropsch catalyst comprises Fe and / or Co, preferably Co.

6. The method according to any of the preceding claims, wherein the zeolite-based catalyst in step (iii) comprises an MFI-type zeolite, a CHA-type zeolite, a BEA-type zeolite, a MOR-type zeolite, an FAU-type zeolite, an MEL-type zeolite, an FER-type zeolite, an MTT-type zeolite, a TON-type zeolite, an ERI-type zeolite, an MTW-type zeolite, an MWW-type zeolite or a mixture thereof.

7. The method according to any of the preceding claims, wherein another metal-modified zeolite-based catalyst is present in step (i).

8. The method according to any of the preceding claims, wherein step (ii) additionally produces saturated C7+ hydrocarbons, preferably saturated C8+ hydrocarbons.

9. The method according to any of the preceding claims, wherein in step (i) a feed comprising the CO2 is fed to the reverse water gas shift catalyst, wherein the feed is substantially free of CO.

10. The method according to any of the preceding claims, wherein in step (i) the CO2 is reacted with H2 at a temperature of 250 to 1000°C using a reverse water gas shift catalyst which comprises Ni / Al2O3 to yield a mixture comprising CO and H2O, wherein the H2O is at least partially separated from the CO in a subsequent cooling step before the CO is converted in step (ii), wherein in step (ii) CO from step (i) is reacted with H2 using a Fischer-Tropsch catalyst which comprises Co to yield saturated C8+ hydrocarbons and unsaturated hydrocarbons which comprise at least one of ethylene, propylene and / or butylene, and wherein in step (iii) the zeolite-based catalyst comprises an MFI-type zeolite or a BEA-type zeolite.