EP4313849A1 - Procédé amélioré de redox thermochimique solaire - Google Patents

Procédé amélioré de redox thermochimique solaire

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Publication number
EP4313849A1
EP4313849A1 EP22719518.7A EP22719518A EP4313849A1 EP 4313849 A1 EP4313849 A1 EP 4313849A1 EP 22719518 A EP22719518 A EP 22719518A EP 4313849 A1 EP4313849 A1 EP 4313849A1
Authority
EP
European Patent Office
Prior art keywords
redox material
reduction
redox
synthesis gas
thermochemical
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
EP22719518.7A
Other languages
German (de)
English (en)
Inventor
Philipp HOLZEMER-ZERHUSEN
Andreas ROSENSTIEL
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Deutsches Zentrum fuer Luft und Raumfahrt eV
Original Assignee
Deutsches Zentrum fuer Luft und Raumfahrt eV
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Deutsches Zentrum fuer Luft und Raumfahrt eV filed Critical Deutsches Zentrum fuer Luft und Raumfahrt eV
Publication of EP4313849A1 publication Critical patent/EP4313849A1/fr
Pending legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
    • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
    • C01B3/061—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of metal oxides with water
    • C01B3/063—Cyclic methods
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/062—Hydrocarbon production, e.g. Fischer-Tropsch process

Definitions

  • the present invention relates to a particular solar thermal redox process for the production of organic compounds, in which as by-products resulting short-chain hydrocarbons in the solar thermal chemical process as a reducing agent or as a fuel who is used again.
  • Solar thermochemical cycles are a promising technology for the production of synthesis gas from water and carbon dioxide.
  • the synthesis gas which is a mixture of hydrogen and carbon monoxide, can be used in downstream processes to produce C02-neutral fuels and basic chemicals.
  • thermochemical cycles a redox material is heated. At high temperatures, oxygen is released from the material. This process is called reduction. In the next step, the reduced material is oxidized at lower temperatures by adding CO2 (carbon dioxide) or water. As a result, water and CO2 react to form hydrogen or carbon monoxide (CO). Synthesis gas is thus produced. The cycle process then starts all over again.
  • Various methods can be used to heat the redox material during reduction. A heating up with energy sources by burning them is just as possible as heating with electrical energy, which is provided, for example, by renewable energy sources. Alternatively, concentrated solar radiation can be used for heating. In such a case one speaks of a solar thermochemical cycle. The basic process is with Typical values are shown schematically in FIG. 1, with concentrated solar radiation being mentioned as the heat source by way of example.
  • cerium oxide for example, is deprived of oxygen at temperatures of around 1500 °C. This is usually done at reduced oxygen partial pressure, which is achieved either by one or more vacuum pumps, which reduce the overall pressure in the reduction chamber, or by using a purge gas, which reduces the oxygen concentration in the reduction chamber.
  • thermochemical reduction step can be used, in which a reducing agent is used.
  • a reducing agent is used.
  • Significantly lower oxygen partial pressures can be achieved than when using vacuum pumps or purge gases (Krenzke, P.T., Fosheim, J.R., and Davidson, J.H., Solar fuels via chemical-looping reforming. Solar Energy 2017, 156: p.48-72 ).
  • This allows the process to take place at significantly lower reduction temperatures He, T. et al., A hybrid solar-redox scheme for liquid fuel and hydrogen co-production. Energy & Environmental Science, 2014, 7(6): p. 2033-2042).
  • Methane has proven to be a suitable reducing agent in the process, also known as redox reforming. However, by using methane from natural gas, the reaction is no longer C02 neutral.
  • the reduction in solar thermochemical cycle processes is discontinuous.
  • Suitable solar receiver reactors exist for this purpose, in which the redox material is present as a solid structure (monolith).
  • the reduction phase and synthesis gas generation alternate.
  • the discontinuously generated synthesis gas must be temporarily stored.
  • several reactors can be operated in parallel, so that one by Such arrays enable a quasi-continuous production of synthesis gas. Storage is always necessary if the synthesis gas is to be made available even when there is no solar radiation, for example at night.
  • thermochemical and in particular solar thermal chemical cycle processes there is a large temperature difference between the reaction steps, ie reduction and oxidation of the redox material. After the oxidation has taken place, the redox material must be heated to the temperature at which the reduction takes place.
  • the temperature difference between oxidation and reduction is usually 500 K to 800 K. The amount of heat required for this can account for about 60% of the total energy requirement for synthesis gas production (Marxer, D. et al., Solar thermochemical Splitting of CO2 into separate streams of CO and O2 with high selectivity, stability, conversion, and efficiency Energy & Environmental Science, 2017. 10(5): pp. 1142-1149).
  • High reduction temperatures also generally have a negative effect on the efficiency and cost-effectiveness of a process: On the one hand, high reduction temperatures result in high thermal losses at the receiver, particularly due to radiation. In addition, high temperatures tend to require higher concentration factors of the concentrated solar radiation, which means that radiation losses increase when the concentrated solar radiation is provided, and the efficiency of the solar collectors, e.g. in a heliostat field, decreases. Furthermore, high temperatures lead to high material stress, which is why particularly expensive temperature-resistant materials have to be used.
  • a further disadvantage of the prior art is that in the production of fuels from synthesis gas, for example, using synthesis processes such as the Fischer-Tropsch synthesis, in addition to the desired liquid long-chain hydrocarbon compounds, there is also a significant proportion of gaseous products.
  • the object of the present invention is to improve these disadvantages of the prior art.
  • the main product of the synthesis process ie one or the mixture of two or more organic compounds, can consist of linear, cyclic or branched, substituted or unsubstituted al kanes or alkenes having 5 to 50 carbon atoms per molecule. Longer carbon chains can also form in small proportions.
  • a CH2 group within an alkyl chain or alkylene chain Z to be substituted by a heteroatom, the heteroatom being selected from N, 0, P or S, preferably N or 0, and free valences being compensated by H.
  • organic compounds having 5-50 carbon atoms, in particular linear or branched alkanes or alkenes, one or both, preferably a terminal -CH3 group being replaced by an -OH group or a -COOH or a -C-(0 )0-KW or an -O-KW group can be replaced, where KW is alkyl, aryl, heteroaryl, in particular having 1 to 5 carbon atoms.
  • the organic compounds also include cyclic hydrocarbons, alcohols with one or more OH groups, the -OH groups preferably being present at the ends.
  • the main products are therefore often solid or liquid at room temperature and normal pressure.
  • different products can arise.
  • Fischer-Tropsch process for example, mainly linear alkanes are formed
  • Synol process for example, mainly alcohols are formed, to name just two possible production processes for the production of organic compounds, without the present application being restricted thereto.
  • States of matter of compounds mentioned in the present application always relate to room temperature (25° C.) and normal pressure.
  • thermochemical cycle which is part of the method according to the invention, comprises in particular the following steps: al) providing water and/or carbon dioxide, a2) bringing water vapor and/or carbon dioxide into contact with a redox material, as a result of which the redox material is oxidized and water and /or carbon dioxide are reduced to carbon monoxide and/or hydrogen, a3) separation of the synthesis gas obtained, a4) reduction of the redox material by means of gaseous hydrocarbons CnHm, which are formed as a by-product in the production of the main product, and separation of the oxygen obtained.
  • thermochemical cycle is preferably a solar thermal chemical cycle, i.e. the energy required for the cycle is at least partially, preferably almost completely, in particular completely provided by solar energy in a preferred embodiment.
  • the thermochemical cycle can be in the form of a single reduction reactor, in particular a solar reduction reactor.
  • the short-chain gaseous hydrocarbons can be completely returned to the reactor.
  • the reactor Arrays used, the short-chain gaseous hydrocarbons can be fed to one, a part or all of the reactors.
  • the reduction temperature can be lowered and/or the degree of reduction increased, which reduces the thermal losses and other disadvantages of the prior art.
  • other uses of the by-products are possible that increase the efficiency of the process, as explained further below.
  • thermochemical cycle requires energy, especially in the form of thermal energy. This is needed to heat and reduce the redox material.
  • the heat can be provided in any way, such as by burning fossil fuels, or by electricity obtained by burning fossil fuels, in nuclear power plants, or by wind, water, or solar power.
  • the heat required is preferably obtained from regenerative energies, i.e. from wind, water or solar energy. In this way, electricity can first be generated, which can then be used for heating.
  • solar energy in particular can also be used directly, so that the redox material is immediately heated by means of concentrated solar radiation.
  • thermochemical cycle process is also referred to as a solar thermochemical cycle process.
  • thermochemical cycle With sufficient addition of a reducing agent to the thermochemical cycle, the efficiency of the entire cycle and thus of the method according to the invention can be improved in various ways.
  • reducing the reduction temperature radiation and other heat losses at the receiver are reduced. This is particularly relevant when using concentrated solar radiation. But also with that This factor must be taken into account when using other heat sources.
  • lower concentration factors can be selected at lower reduction temperatures, which reduces radiation losses when providing the concentrated solar radiation and increases the collector efficiency.
  • the CCh neutrality of the entire process is maintained, provided that the redox material is also heated using regenerative energies.
  • short-chain gaseous hydrocarbons as a reducing agent also means that the by-product, i.e. the short-chain gaseous hydrocarbons, remains in the process.
  • these hydrocarbons react again to form synthesis gas, which is fed back to the synthesis process, for example the fuel synthesis.
  • the short-chain gaseous hydrocarbons can also be converted into CO2 and H2O in this step, which are fed to the oxidation step and react there to form synthesis gas, which is then fed back into the fuel synthesis. This increases the yield and carbon utilization of the process.
  • part of the recirculated short-chain hydrocarbons can be thermally utilized, ie burned and the heat released used.
  • the reactor could be solar in the reduction step preheated and then brought to the final reduction temperature using the enthalpy of combustion. Since no open aperture is required for combustion, radiation losses due to high temperatures are reduced. The CO2 and H2O produced during combustion can be returned to the oxidation step, which means that the process remains CO2-neutral.
  • thermochemical cycle process thus enables a thermochemical cycle process to be carried out under optimized conditions.
  • the recirculated short-chain hydrocarbons ie in particular methane, ethane, propane and butane
  • This has the advantages already mentioned and, in a preferred embodiment, makes it possible for a solar cycle process to also be carried out at times when there is reduced solar radiation, such as in the morning or evening hours, i.e. at sunrise or sunset. or during periods of cloud cover.
  • the reduction can take place at temperatures well below the usual temperatures.
  • the temperature of the reduction is preferably 200 K to 700 K, in particular 200 K to 500 K, below the temperature that is required if no reducing agent is used.
  • the redox material in its oxidized form, can be represented generally as Me y Ox-ox, where Me stands for metals, metalloids or metallic compounds.
  • Me stands for metals, metalloids or metallic compounds.
  • the larger Dd öred - d 0c .
  • the larger Dd the more synthesis gas can be produced in the oxidation step with the same amount of redox material. So if the temperature of the reduction step is not lowered when there is intense solar radiation, the presence of the short-chain reducing agents still improves efficiency.
  • the redox material is reduced in step a4) of the method according to the invention in such a way that the redox material is brought from its oxidized state MeOx-doc into its reduced state MeOx-öred, where öred by a factor of 1, 2 to 40, in particular 1.5 to 30, preferably 2 to 20, in particular 3 to 15, particularly preferably 4 to 20 be greater than in a comparable process in which no reducing agent is used.
  • Improving reactivity through improved reduction and lowering the temperature at which reduction occurs can also be combined.
  • the redox material is reduced in step a4) at a temperature of from 750.degree. C. to 1200.degree. C., in particular from 850.degree. C. to 1100.degree.
  • the reduction it is also possible for the reduction to be carried out at higher temperatures of up to 1700° C., in particular of up to 1500° C., as a result of which a higher d value is achieved.
  • the oxidation of the redox material in step a2) of the method according to the invention takes place, for example, at a temperature of 1000° C. or less, in particular in a range from 500° C. to 950° C.
  • Suitable redox materials are basically chemical compounds with redox properties. Chemical compounds with redox properties im The purposes of the invention are those compounds which can be reversibly oxidized and re-duced. These chemical compounds with redox properties are advantageously selected from the group consisting of metal oxides, mixed metal oxides and/or doped metal oxides. Of these reaction partners, metal oxides have proven to be particularly advantageous because they are the most versatile.
  • a multivalent metal oxide is particularly preferably used as the redox material, since this is particularly easy to fix and regenerate.
  • Multivalent within the meaning of the invention is a metal oxide which has several oxidation states next to one another and in particular when the metal is present in an oxidation state greater than +1, in particular greater than +2.
  • the metal oxides of the redox material preferably include ferrites and/or cerium oxide and/or doped cerium oxide and/or zinc oxide and/or manganese oxide and/or lanthanum oxide and/or oxides of the general formula M1 x M2 y Fe3-x- y O4 and/or mixtures of these Oxides, since these can be used particularly efficiently in water splitting, and/or perovskites and brownmillerites of the general chemical composition A m+ B n+ Ox.
  • Ml x M2 y Fe3-x- y 04 are 0 ⁇ x ⁇ 3, 0 ⁇ y ⁇ 3 and 0 ⁇ (x+y) ⁇ 3, and Ml and M2 are each independently selected from the Group consisting of Cr, Mg, Ca, Mn, Co, Ni, Cu, Zn, Sr, Sn, Ba, Cd and Pb.
  • Perovskites and brownmillerites have a general chemical composition A m+ B n+ O x , the cation A m+ having a valency m in the range from 1 to 3, in particular 2, being selected from the group of alkali, alkaline earth or rare earth metals , the cation B n+ with a valency n in the range from 1 to 5, in particular 3 to 4, selected from the group of transition metals and main group metals, and the oxygen stoichiometry x is in the range 2 to 4, in particular in the range 2.5 to 3, and mixtures these oxides.
  • Cerium oxide or doped cerium oxide has proven to be particularly suitable as a redox material. This can be oxidized and reduced particularly well.
  • thermochemical cycle chemical reactions take place in which the individual steps are reversible.
  • Reversible steps within the meaning of the invention are reaction steps in which the chemical equilibrium can be set in such a way that either the “forward” or the “reverse reaction” takes place with preference.
  • the redox material is oxidized, while in the second step, the redox material is reduced.
  • oxidation and reduction can take place in one reactor. Alternatively, reduction and oxidation take place in separate reactors.
  • thermochemical cycle process according to the invention is particularly preferably one in which water or CO2 is split. It is also possible a combination of the two, so that both water and CO2 can be split at the same time. This is preferred in the present case.
  • water vapor in particular can be split thermochemically by concentrated sunlight and hydrogen can be generated as a result. This forms the basis for the development of the method according to the invention, with which hydrogen can be produced by solar thermochemistry.
  • hydrogen is generated from water vapor in a cyclic process, preferably at temperatures in the range from 800 °C to 1200 °C.
  • a metal oxide system is circulated that can separate oxygen from water molecules and bind it reversibly into its crystal structure.
  • the heat, in particular solar heat, which is required for the cyclic process can preferably be provided by concentrated radiation either directly in a receiver reactor or by a heat transfer medium.
  • a directly irradiated receiver reactor is assumed.
  • the short-chain gaseous hydrocarbons can be fully or partially thermally utilized and for the energy thus obtained to be used in the thermochemical cycle process.
  • the hydrocarbons are burned in particular together with air. The heat gained in this way can be used to heat up the reactors.
  • the resulting CO2 can be fed back into the cyclic process for the production of synthesis gas, so that the overall process is CO2-neutral.
  • Suitable reactors in which the cyclic process takes place are described in the prior art. According to the invention, it is possible for several reactors to be operated in parallel in a so-called array. According to the invention, it is possible for the redox material to be present in monolithic form in the reactor or in the reactors. However, it is also possible for the redox material to be present in the reactor in particulate form or in the form of other movable units.
  • FIG. 2 a preferred embodiment of the procedural procedure according to the invention is shown in a device suitable for this purpose.
  • a solar-thermochemical cyclic process uses the raw materials water and CO2 to generate synthesis gas, i.e. a mixture of carbon monoxide (CO) and hydrogen (H2).
  • synthesis gas i.e. a mixture of carbon monoxide (CO) and hydrogen (H2).
  • the high-temperature heat required for this is provided by concentrated solar radiation, here in the example by a heliostat field.
  • a Fischer-Tropsch process in FIG. 2 a mixture of hydrocarbon compounds, the so-called syncrude, is produced from the synthesis gas.
  • gaseous hydrocarbons mainly methane, ethane, propane and butane.
  • these gaseous hydrocarbons are recycled and used as reducing agents in the reduction step of the solar thermochemical reactor. Since gaseous hydrocarbons are continuously produced in the synthesis process, but the thermochemical reactor is only operated when there is sufficient solar radiation, a reducing agent buffer store for the gaseous hydrocarbons is also provided.
  • thermochemical reactor is designed in a discontinuous monolithic concept.
  • the redox material is fixed in the reactors and is cyclically reduced and oxidized.
  • the redox material could also be in mobile form (e.g. particles or mobile elements) and first pass through a reduction and then an oxidation reactor.
  • thermochemical receiver reactors TCR1-TCR5
  • receiver array receives several parallel thermochemical receiver reactors (TCR1-TCR5)
  • the number of reactors being set to 5 as desired.
  • corresponding arrays can have any number of reactors.
  • a receiver array consisting of 19 reactors is considered.
  • more or fewer reactors can also be used in an array - depending on the desired system capacity, the thermal output of an individual reactor and the on-site conditions and the resulting fluctuations in solar radiation.
  • the reduction and oxidation steps can run in parallel. In such monolithic reactors only reduction or oxidation can take place. If the redox material is completely oxidized, it can then be used for reduction. In reactors in which the redox material is present in particulate form or in the form of other mobile elements and is therefore not fixed, the redox material can be exchanged after a certain time and, for example, circulate between reactors or be stored temporarily before it is used in the respective oxidation stage for oxidation or oxidation .reduction is needed.
  • the invention provides that the supply of reducing agent to each reactor can be controlled individually. It is thus possible to run the reduction step with reducing agent in some reactors of the array and purely thermally, i.e. without reducing agent, in others. For example, with relatively little solar radiation due to the reducing agent, the thermochemical reduction, ie the cycle process according to the invention, could still take place in some or all of the reactors.
  • the process according to the invention increases the overall process efficiency in the production of the above-mentioned organic products. Even during the design phase, it is possible, for example, to differentiate between purely thermal and thermochemical reactors with reducing agents within the receiver array.
  • the reactors where that Reducing agent is used can then be performed with cheaper Materia lien, in particular, a cheaper and more readily available redox material than cerium oxide can be used.
  • cerium oxide could be replaced by a doped cerium oxide, a ferrite compound or by similar perovskites. This and the better utilization of the concentrated solar radiation improves the economics of the process. It can also be provided according to the invention that all reactors are designed in such a way that they can be operated both with reducing agents and purely thermally.
  • Fig. 3 shows how the temperature required in the reduction reactor changes when short-chain hydrocarbon compounds are added.
  • methane was chosen as a representative of short-chain hydrocarbon compounds.
  • the splitting of water and CO2 was considered.
  • the calculations are based on a model published in Holzemer-Zerhusen, P., et al., Efficiency assessment of solar redox reforming in comparison to conventional reforming. International Journal of Hydrogen Energy, 2020. 45(7): p. 4137-4151, is described in detail.
  • the graph shows that the required reduction temperature falls as the amount of methane increases. If 0.14 mol/s of methane is added per mol/s of cerium oxide, the reduction temperature is around 1100° C., for example. If you try to achieve the same degree of reduction in the reduction step without adding methane or another reducing agent, eg with a vacuum pump at a pressure of 10 Pa, you would need a temperature of approx. 1900 °C. If a method according to the invention is compared with a method from the prior art, clear improvements result. This is shown below as an example for cerium oxide as the redox material and methane as the reducing agent.
  • the method according to the invention can enable effective degrees of reduction of the redox material at atmospheric pressure. In the state of the art about 4% of the total energy requirement is required for the vacuum pumps, whereas this is not exactly necessary in the method according to the invention.
  • the required temperature can be drastically reduced.
  • the reducing agent is divided between some of the reactors or all of the reactors in such a way that approx. 15% of the synthesis gas produced in the oxidation step is produced in reactors in which the reduction according to the invention using the reducing agent takes place, a reduction temperature of 800 °C is appropriate possible with these reactors.
  • the reducing agent can be continuously divided among so many reactors that they produce 15% of the synthesis gas produced in the oxidation step.
  • the reducing agent can be used temporarily in several or all of the reactors. For this purpose, the reducing agent can be temporarily stored.
  • the amount of heat to be supplied to all reduction reactors and vacuum pumps would be reduced from about 98% to about 84% of the total energy requirement of the prior art. I.e. the total energy requirement in the method according to the invention would be about 14% lower than the total energy requirement of the prior art. Due to the lower temperature, the heliostat field can also be adjusted, which means that an additional increase in efficiency can be expected. c) degree of reduction
  • the degree of reduction d of the redox material can be increased.
  • the amount of reducing agent is sufficient to operate part of the reactors of an array continuously with reducing agent at a temperature of 1520 °C and 1 bar in such a way that that an estimated 33% of the synthesis gas produced in the oxidation step is produced in these reactors.
  • the reducing agent can also be temporarily stored and the reactors are not continuously operated with reducing agent. So can up to 100% of the reactors at times are supplied with reducing agent, so that a total of about 33% of the synthesis gas produced in the oxidation step is also produced in reactors in which the reduction according to the invention by means of reducing agent takes place. Combinations of both approaches are possible.
  • the amount of heat to be supplied to all reduction reactors and vacuum pumps would be reduced from approximately 98% to approximately 68% of the total energy requirement of the prior art. That is, the total energy requirement in the inventive method would be about 30% lower than the total energy requirement of the state of the art.
  • the method according to the invention offers a CO 2 -neutral possibility for the production of liquid hydrocarbons and other organic compounds, the method being more effective than known methods from the prior art.
  • the process according to the invention offers the same advantage in terms of product yield as other conceivable approaches to recycling by-products:
  • the yield increases by up to 58% when the method is applied to a Fischer–Tropsch synthesis process compared to a no-recycle case.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

La présente invention concerne un procédé de production d'un ou plusieurs composés organiques, caractérisé en ce que a) un gaz de synthèse est produit dans un procédé cyclique thermochimique à deux étages à l'aide d'un matériau redox, b) le gaz de synthèse ainsi obtenu est ensuite converti en un produit primaire, consistant en au moins un composé organique, à l'aide d'un procédé de synthèse, des hydrocarbures gazeux CnHm où n = 1 à 4 et m = 4 pour n = 1 et m = 2 à 2n+2 pour n = 2 à 4 étant produits en tant que sous-produit et c) les hydrocarbures gazeux sont utilisés dans le procédé cyclique thermochimique en tant qu'agent réducteur pour le matériau redox, le produit primaire issu du procédé de synthèse étant un composé organique, ou un mélange de deux ou plus de ceux-ci, de formule générale X-(Z)n-Y, Z étant choisi parmi (CH2) et/ou (CH = CH), n valant 2 à 50, en particulier 5 à 50, X et Y étant, indépendamment l'un de l'autre, choisis parmi -CH3, -OH, -COOH, -NH2, -O-KW, KW représentant alkyle, aryle, hétéroaryle, comprenant en particulier 1 à 5 atomes de carbone.
EP22719518.7A 2021-03-31 2022-03-28 Procédé amélioré de redox thermochimique solaire Pending EP4313849A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102021108174.2A DE102021108174A1 (de) 2021-03-31 2021-03-31 Verbessertes solarthermochemisches Redox-Verfahren
PCT/EP2022/058115 WO2022207553A1 (fr) 2021-03-31 2022-03-28 Procédé amélioré de redox thermochimique solaire

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EP4313849A1 true EP4313849A1 (fr) 2024-02-07

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Publication number Priority date Publication date Assignee Title
US9518236B2 (en) * 2009-09-08 2016-12-13 The Ohio State University Research Foundation Synthetic fuels and chemicals production with in-situ CO2 capture
US9212327B2 (en) 2013-07-30 2015-12-15 Advanced Cooling Technologies, Inc. System and process for producing fuel with a methane thermochemical cycle

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