EP4240810A1 - Conversion du coen vecteurs d'énergie chimiques et produits - Google Patents

Conversion du coen vecteurs d'énergie chimiques et produits

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Publication number
EP4240810A1
EP4240810A1 EP21791304.5A EP21791304A EP4240810A1 EP 4240810 A1 EP4240810 A1 EP 4240810A1 EP 21791304 A EP21791304 A EP 21791304A EP 4240810 A1 EP4240810 A1 EP 4240810A1
Authority
EP
European Patent Office
Prior art keywords
product
methanation
gas
fischer
synthesis
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
EP21791304.5A
Other languages
German (de)
English (en)
Inventor
Tim BÖLTKEN
Roland Dittmeyer
Peter Pfeifer
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.)
Karlsruher Institut fuer Technologie KIT
Original Assignee
Karlsruher Institut fuer Technologie KIT
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 Karlsruher Institut fuer Technologie KIT filed Critical Karlsruher Institut fuer Technologie KIT
Publication of EP4240810A1 publication Critical patent/EP4240810A1/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
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C10G2/34—Apparatus, reactors
    • 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
    • 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
    • C10G2/50—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon dioxide with hydrogen
    • 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
    • C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
    • C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
    • C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/023—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/02—Hydrogen or oxygen
    • C25B1/04—Hydrogen or oxygen by electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/23—Carbon monoxide or syngas
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B15/00—Operating or servicing cells
    • C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
    • C25B15/081—Supplying products to non-electrochemical reactors that are combined with the electrochemical cell, e.g. Sabatier reactor
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4043—Limiting CO2 emissions
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/42—Hydrogen of special source or of special composition
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/42—Fischer-Tropsch steps
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
    • Y02E60/30—Hydrogen technology
    • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

  • the present invention relates to methods for converting CO2 into chemical energy carriers and products, in particular via methanation of the gas phase fraction from a Fischer-Tropsch synthesis.
  • Fischer-Tropsch synthesis (FTS) process used to produce hydrocarbons has been known for many decades.
  • a synthesis gas which mainly consists of carbon monoxide (CO) and hydrogen (H2), is converted into hydrocarbons by heterogeneous catalysis in a synthesis reactor.
  • CO carbon monoxide
  • H2 hydrogen
  • the outlet stream of Fischer-Tropsch synthesis units in which synthesis gas is synthesized into hydrocarbons according to the Fischer-Tropsch process, four fractions can usually be distinguished:
  • a gas phase consisting of unreacted synthesis gas (mainly CO, H2), short-chain hydrocarbons and volatile components of the by-products and CO2.
  • a waxy phase of long-chain hydrocarbons that is solid at ambient temperature and pressure (wax phase or wax fraction).
  • a hydrophobic phase of shorter-chain hydrocarbons that is liquid at ambient temperature and pressure (oil phase).
  • An aqueous phase consisting of the water of reaction that forms and the organic compounds dissolved in it.
  • a further problem of the prior art is that methanation from a gas phase originating from a Fischer-Tropsch synthesis is not possible satisfactorily if the synthesis gases fed into the Fischer-Tropsch synthesis have a CCh content of more than 50% by volume in relation to the amount of carbon oxides used, i.e. a mixture of CO and CO2. Even at 15 to 50% by volume, the possible degrees of conversion of the carbon contained in the carbon oxides in the Fischer-Tropsch synthesis are limited.
  • the object of the present invention was accordingly to provide methods and devices which no longer have the problems of the prior art, or at least only to a greatly reduced extent, or have new advantageous effects.
  • ambient temperature means a temperature of 20° C. Unless otherwise stated, temperatures are in degrees Celsius (° C.).
  • the reactions or process steps listed are carried out at superatmospheric pressure, i.e. at more than 3 barg, preferably more than 5 barg, particularly preferably at least 19 barg.
  • long-chain hydrocarbons is understood to mean hydrocarbons having at least 25 carbon atoms (C25), preferably up to one hundred carbon atoms (C100).
  • the long-chain hydrocarbons having at least 25 carbon atoms can be linear or branched and partially monounsaturated contain hydrocarbon compounds.
  • short-chain hydrocarbons is understood to mean hydrocarbons having 5 to 24 carbon atoms (C5-C24).
  • the short-chain hydrocarbons having 5 to 24 carbon atoms can be linear or branched and contain partially monounsaturated hydrocarbon compounds.
  • short-chain hydrocarbons is understood to mean hydrocarbons having 1 to 4 carbon atoms (C1-C4).
  • the short-chain hydrocarbons having 4 carbon atoms can be linear or branched and contain partially monounsaturated hydrocarbon compounds.
  • wax phase or “wax fraction” is understood to mean that product fraction of the Fischer-Tropsch synthesis which is characterized by long-chain hydrocarbons.
  • oil phase means that product fraction of the Fischer-Tropsch synthesis that is characterized by shorter-chain hydrocarbons. This fraction is also referred to as the fuel fraction in the context of the present invention. The products of this product fraction are used in the present invention often referred to as fuels.
  • reverse water-gas shift reaction also referred to as “reverse water-gas shift reaction”
  • RWGS reverse water-gas shift reaction
  • a “reactor” can also be referred to as a device or unit.
  • “chemical energy carriers and products” means a synthetic gas that can be fed into a natural gas network, in particular a mixture of at least 80% by volume of methane with a Wobbe index of 37 to 60 MJ/m 3 , preferably 50 to 55 MJ/m 3 and a calorific value of 30 to 47 MJ/m 3 understood.
  • a synthetic gas that can be fed into a natural gas network means a gas that, with regard to calorific value and Wobbe index, complies with the regulations for feeding into the natural gas network without restricting the degree of admixture in accordance with DVG worksheet G260 or DIN EN 16726:2019-11.
  • the present invention relates in particular to a process for converting CO2, in particular into chemical energy carriers and products, comprising the following process steps or consisting of these: a) providing a synthesis gas comprising H 2 , CO and CO2, b) supplying the synthesis gas to a Fischer-Tropsch synthesis, and conversion of the synthesis gas into a Fischer-Tropsch synthesis product comprising at least the following fractions i) fuel fraction, ii) wax fraction, iii) gaseous by-product phase, iv) aqueous phase, cl) optional hydrogenation of the Fischer -Tropsch synthesis product from step b) with metered addition of hydrogen, c2) multi-stage separation of the Fischer-Tropsch synthesis product from step b) or the product from step cl) and separation of fractions i), ii) and iv) , d) methanation of the gaseous by-products in fraction iii) with addition of H 2 , in particular to a synthe
  • the origin of the synthesis gas is not restricted, as long as the synthesis gas has a CCh content of at least 5% by volume.
  • the synthesis gas can be obtained from the gasification of biomass, from synthesis gas production from fossil reactants (natural gas, petroleum, coal), or from electricity-based processes (conversion of electrolytically generated H 2 and CO 2 ).
  • the synthesis gas is formed within the scope of the present invention from H2O and CO2 by means of high-temperature co-electrolysis.
  • the ratio of H 2 O to CO 2 (v/v) is about 2:1 and the electrolysis occurs at 750-850°C, particularly using electricity from renewable sources.
  • a synthesis gas stream is assumed that contains at least 5% by volume of CO2.
  • RWGS reverse water gas shift reaction
  • step a) accordingly comprises the steps al) formation of a synthesis gas by means of high-temperature co-electrolysis of H 2 O and CO2, a2) processing of the synthesis gas obtained in al) by means of CO2 activation by H2 from a H2O electrolysis via, or consists of, the reverse water gas shift reaction RWGS.
  • step c2) it is possible to subject the fractions i) and/or ii) obtained in step c2) to a (further) hydrogenating cleavage. This makes it possible to further adapt the products obtained to desired results.
  • the water formed during the methanation is condensed out and separated off. This is preferably done together with the methanation. This can either be in a single Apparatus part done or by installing a separator downstream of the methanation reactor.
  • the methanation product obtained in the process of the present invention is in most cases a synthetic gas that can be fed directly into a natural gas network.
  • a product is obtained whose calorific value and Wobbe index satisfies the relevant regulations for such a feed.
  • the product does not meet these regulations in individual cases, it is possible to simply work up the product by using combustible substances such as propane or butane or inert gases such as CO, depending on whether the Wobbe index and/or calorific value are too high or too low or CO2 can be added.
  • the methanation product is fed directly into a natural gas grid as a synthetic gas that can be fed into a natural gas grid.
  • the present invention also relates to a plant for converting CO2, in particular into chemical energy carriers and products, comprising the following plant parts or consisting of them
  • CI optionally a single or multi-stage device for the hydro-treating of the Fischer-Tropsch products
  • C2 a multi-stage separation device, preferably composed of several individual separation devices arranged one after the other,
  • the multi-stage separation device C2) preferably comprises a device configured to discharge and transfer the gaseous product fraction into the methanation device D).
  • the device A) is a high-temperature co-electrolysis device configured for a high-temperature co-electrolysis of H2O and CO2 or, in other embodiments, a system as described in WO 2019 048236
  • device B) is a microstructured reactor as described in WO 2017/013003, i.e. a microstructured reactor for carrying out an exothermic reaction between two or more reactants, which are passed in the form of fluids over one or more catalyst(s), comprising at least one stack sequence of a) at least one layer having one or more catalyst(s) for carrying out at least one exothermic reaction, b) at least one layer divided into two or more cooling fields, c) at least one layer having distributor structures with lines for distributing the coolant , having ports for supplying coolant to the ducts of the manifold structure and for connection to the cooling fields, ports for removing the heated coolant from the cooling fields, and ducts and ports for removing the heated coolant from the stack sequence.
  • the devices C2) are preferably separating devices as are known from the prior art, in particular distillation devices.
  • the device D) is in preferred embodiments
  • the device D) can be according to WO 2017/211864.
  • the water separation device can be a (simple) device for condensation and phase separation. In other embodiments, it may be a distillation device.
  • the systems according to the invention are particularly suitable and configured for carrying out the method according to the invention.
  • the present invention relates in particular to the direct combination of Fischer-Tropsch synthesis with subsequent methanation of the gaseous product components or unreacted starting materials when using a CCh-containing synthesis gas as starting material gas with a CCh content of at least 5% by volume.
  • An advantage of the present invention is that, unlike in the prior art, the hydrocarbons with chain lengths of less than 0.4, which are generally regarded as an undesirable by-product in the Fischer-Tropsch synthesis, are put to meaningful use in the context of the present invention.
  • the procedure in the prior art is generally such that the formation of these products is minimized, which makes it necessary, inter alia, to limit the degree of conversion per pass and to recycle the unreacted starting materials.
  • the gases can be used thermally or to generate electricity. For smaller systems, the associated effort is uneconomical. If there is no use for the heat or electricity generated by burning the gaseous fractions, the carbon yield, the overall efficiency and also the economics of the process are reduced.
  • it is an advantage of the present invention that the present invention increases carbon yield, overall efficiency, and economy.
  • An advantage of the present invention is that a feed-ready product gas is obtained as product. As a result, a high carbon yield is achieved in particular even without recirculation.
  • One advantage of the present invention is that a significant improvement in the economics of “power-to-molecules” applications or electricity-based chemical energy carriers, in this case electricity plus CO2 to form methane, could be achieved.
  • the residual gas of the FT synthesis can be used almost completely in embodiments, ie to a proportion of more than 90%, preferably more than 95%, particularly preferably more than 98% and particularly preferably more than 99% Recycling of unreacted synthesis gas be avoided.
  • FIG. 1 shows an example of a method corresponding to a variant of the present invention.
  • Synthesis gas 1 comprising H2, CO and CO2 is introduced into a Fischer-Tropsch reactor D.
  • Pressurized water 5 is also introduced into this Fischer-Tropsch reactor D and pressurized steam 6 is removed from the reactor by indirect heat exchange.
  • This steam 6 can be used for energy recovery, in particular via heat exchangers or turbines, or for supplying heat for reactions (neither of which is shown in the figure).
  • the resulting FT product (comprising four fractions) is then conducted via a first heat exchanger WT to a first separation device A, where the wax fraction ii) is separated off as the bottom.
  • the product is discharged from the methanation reactor E and conducted via a fourth heat exchanger WT to a third separation device C, where the water 3 formed during methanation is condensed and discharged and the remaining product gas 4 is discharged as synthetic gas that can be fed into a natural gas network.
  • the latter can then be fed into a natural gas network (not shown in the figure).
  • FIG. 2 shows the same structure and sequence as FIG. Product is subjected to hydrocleavage, so that compared to Figure 1, a lower proportion of wax fraction ii) and a higher proportion of fuel fraction i) is obtained before the first separation takes place. This is followed by forwarding to a first separation device A and the same process as in FIG. 1.
  • the gas components are similar in both cases.
  • a total of only 19.9 kg/h of FT product (total of oil and wax) and 30.5 kg/h of water (by-product of the synthesis) were obtained as the product of value. This meant that around 50% of the incoming mass flow could not be used and would have had to be recycled, which involved a lot of energy.
  • the composition of the gas was in % by volume: 16.57 CO2 25.33 CO 0.07 H 2 O 50.10 H 2 6.26 CH 4 0.33 C2 0.59 C3 0.42 C4 0.21 C5 0.08 C6 0.02 C7 0.01 C8
  • the composition of the product gas after methanation in % by volume was: CO 0.01 CO 2 2.64 H 2 6.35 H 2 O 0.06 CH 4 85.84 C2 0.79 C3 1.83 C4 1.32 C5 0.78 C6 0.35 C7 0.08 C8 0.02
  • this composition could be fed in directly as synthetic natural gas at 0.282 kg/h, since the Wobbe index in this composition was around 53 MJ/m 3 or 15.3 kWh/m 3 .
  • methane another 0.289 kg/h of water was formed, which was condensed out. The gas quality was very good.
  • process data were determined as follows:
  • the operating parameters were the following:
  • the FT product went directly to a multi-stage separation from which the four fractions were obtained.
  • the product gas had a Wobbe index of 53 MJ/m 3 .
  • the FT product was post-treated by directly subsequent hydrocracking in such a way that the wax content was ultimately less than 5% by weight of the product yield (17.6 kg/h oil, 1.5 kg/h wax).
  • a waste gas composition from the FT synthesis in % by volume was obtained as follows:
  • the operating parameters were the following:
  • the FT product first went to the hydrogenating cleavage and only then to a multi-stage separation, from which the four fractions were obtained in turn.
  • the product gas also had a Wobbe index of 53 MJ/m 3 .
  • the product gas of the methanation had the following composition in % by volume: CO2 1.80
  • Example 1 compared to Example 2, more waxes were obtained.
  • Example 2 in comparison with Example 1, the yield of fuels was maximized and little wax was obtained. In both examples 1 and 2, a feed-ready product gas was obtained.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Metallurgy (AREA)
  • Electrochemistry (AREA)
  • Materials Engineering (AREA)
  • Inorganic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé de conversion du CO2 en vecteurs d'énergie chimiques et produits, en particulier par l'intermédiaire d'une étape de méthanation de la fraction en phase gazeuse à partir d'une synthèse Fischer-Tropsch.
EP21791304.5A 2020-11-03 2021-10-11 Conversion du coen vecteurs d'énergie chimiques et produits Pending EP4240810A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102020128868.9A DE102020128868A1 (de) 2020-11-03 2020-11-03 Umwandlung von CO2 in chemische Energieträger und Produkte
PCT/EP2021/077995 WO2022096229A1 (fr) 2020-11-03 2021-10-11 Conversion du co2 en vecteurs d'énergie chimiques et produits

Publications (1)

Publication Number Publication Date
EP4240810A1 true EP4240810A1 (fr) 2023-09-13

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US (1) US20230399570A1 (fr)
EP (1) EP4240810A1 (fr)
DE (1) DE102020128868A1 (fr)
WO (1) WO2022096229A1 (fr)

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AT525898B1 (de) * 2022-06-23 2023-09-15 Avl List Gmbh Brennstoffzellensystem, Brennstoffzellenanlage und Verfahren zum Erzeugen von Synthesegas
AT526077B1 (de) * 2022-06-23 2023-11-15 Avl List Gmbh Brennstoffzellensystem, Brennstoffzellenanlage und Verfahren zum Erzeugen von Synthesegas
AT525899B1 (de) * 2022-06-23 2023-09-15 Avl List Gmbh Synthesesystem, Brennstoffzellensystem, Brennstoffzellenanlage und Verfahren zum Erzeugen von Synthesegas

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