WO2017074843A1 - Procédés basse température pour hydrogénation de co2 pour la production de compositions de gaz de synthèse à faible rapports h2/co - Google Patents

Procédés basse température pour hydrogénation de co2 pour la production de compositions de gaz de synthèse à faible rapports h2/co Download PDF

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WO2017074843A1
WO2017074843A1 PCT/US2016/058395 US2016058395W WO2017074843A1 WO 2017074843 A1 WO2017074843 A1 WO 2017074843A1 US 2016058395 W US2016058395 W US 2016058395W WO 2017074843 A1 WO2017074843 A1 WO 2017074843A1
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Prior art keywords
reaction
catalyst
syngas
product mixture
certain embodiments
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PCT/US2016/058395
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English (en)
Inventor
Aghaddin Mamedov
Clark Rea
Xiankuan Zhang
Jose Salazar
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Sabic Global Technologies B.V.
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Publication of WO2017074843A1 publication Critical patent/WO2017074843A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/02—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon
    • C07C1/04—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon monoxide with hydrogen
    • C07C1/0485—Set-up of reactors or accessories; Multi-step processes
    • 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
    • C01B3/12—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 water vapour with carbon monoxide
    • C01B3/16—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 water vapour with carbon monoxide using catalysts
    • 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
    • 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
    • C10K3/026—Increasing the carbon monoxide content, e.g. reverse water-gas shift [RWGS]
    • 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
    • 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
    • C01B2203/10—Catalysts for performing the hydrogen forming reactions
    • C01B2203/1041—Composition of the catalyst
    • C01B2203/1047—Group VIII metal catalysts
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/20—C2-C4 olefins
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Definitions

  • the presently disclosed subject matter relates to methods for low temperature conversion of carbon dioxide (C0 2 ) into synthesis gas (syngas) via hydrogenation of C0 2 .
  • Synthesis gas (also known as syngas) is a mixture of carbon monoxide (CO) and hydrogen (H 2 ). Syngas can be prepared by reacting C0 2 with H 2 . This process can be described as a hydrogenation of C0 2 . C0 2 and H 2 can react to form carbon monoxide (CO) and water (H 2 0) through a reverse water gas shift (RWGS) reaction.
  • RWGS reverse water gas shift
  • the RWGS reaction is reversible; the reverse reaction (from CO and H 2 0 to C0 2 and H 2 ) is known as the water gas shift reaction.
  • the RWGS reaction can be conducted under conditions that provide partial conversion of C0 2 and H 2 , thereby creating an overall product mixture that includes C0 2 , H 2 , CO, and H 2 0.
  • C0 2 and H 2 0 can optionally be removed from such a product mixture, thereby providing a purified syngas mixture containing primarily CO and H 2 .
  • Syngas is a versatile mixture that can be used to prepare light olefins, methanol, acetic acid, aldehydes, and many other important industrial chemicals.
  • the efficiency of the preparation of different chemicals, for example, methanol versus light olefins, from syngas can depend on the composition of the syngas.
  • Syngas containing H 2 and CO in a molar ratio (H 2 :CO) of about 2: 1 can be useful for olefin synthesis whereas a molar ratio of more than 4.5: 1 can be useful for methanol synthesis.
  • the molar ratio is preferably about 1 : 1.
  • a disadvantage of many existing methods of preparing syngas is that they tend to produce syngas having a H 2 :CO molar ratio of 3 : 1 or greater.
  • steam reforming of methane tends to generate syngas with a H 2 :CO molar ratio of 3 : 1 or greater.
  • Additional problems encountered during preparation of syngas can include poor catalyst stability under reaction conditions, decomposition of CO to coke fragments, and poor yield.
  • the presently disclosed subject matter provides for a method of preparing syngas that can include providing a reaction chamber that comprises a solid-supported catalyst comprising Cr.
  • the method can further include feeding a reaction mixture comprising H 2 and C0 2 to the reaction chamber.
  • the method can further include contacting H 2 and C0 2 with the catalyst at a reaction temperature of about 600 °C or less to provide a product mixture that comprises H 2 and CO.
  • the catalyst can include one or more solid supports selected from the group consisting of A1 2 0 3 , MgO, Si0 2 , Ti0 2 , and Zr0 2 . In certain embodiments, catalyst includes about 17% Cr by weight.
  • the reaction mixture includes H 2 and C0 2 in a molar ratio (H 2 :C0 2 ) of about 1 :2.
  • the reaction temperature is about 600 °C, about 590 °C, or about 580 °C.
  • the product mixture includes H 2 and CO in a molar ratio
  • the product mixture further includes C0 2 and H 2 0.
  • the method further includes separating at least a portion of
  • the presently disclosed subject matter provides for a method of preparing light olefins, including providing a reaction chamber that comprises a solid-supported catalyst comprising 17% Cr.
  • the method can further include feeding a reaction mixture comprising H 2 and C0 2 to the reaction chamber.
  • the method can further include contacting H 2 and C0 2 with the catalyst at a reaction temperature of about 600 °C or less to provide a product mixture that comprises H 2 , CO, C0 2 , and H 2 0.
  • the method can also include separating at least a portion of C0 2 and H 2 0 from the product mixture to provide purified syngas.
  • the method can also include subjecting purified syngas to a Fischer- Tropsch synthesis (FT) reaction to provide light olefins.
  • FT Fischer- Tropsch synthesis
  • FIG. 1 is a schematic diagram presenting an exemplary process for preparation of syngas.
  • the presently disclosed subject matter provides novel methods of converting C0 2 and H 2 into syngas at low temperatures with low H 2 :CO ratios and improved catalyst stability.
  • the presently disclosed subject matter includes the surprising discovery that solid-supported Catofin® catalysts containing chromium (Cr) can be used to promote hydrogenation of C0 2 at temperatures equal to or less than about 600 °C under atmospheric pressure. Such catalysts can be stable at these temperature and under conditions of low H 2 concentrations to effectively produce syngas with low H 2 :CO ratios and reduce decomposition of CO to coke fragments.
  • the term “about” or “approximately” means within an acceptable error range for the particular value as determined by one of ordinary skill in the art, which will depend in part on how the value is measured or determined, i.e., the limitations of the measurement system. For example, “about” can mean a range of up to 20%, up to 10%, up to 5%), and or up to 1% of a given value.
  • the methods of the present disclosure can involve fixed bed isothermal or adiabatic reactors suitable for reactions of gaseous reactants and reagents catalyzed by solid catalysts.
  • the reactor can be constructed of any suitable materials capable of holding temperatures, for example from about 500°C to about 700°C. Non-limiting examples of such materials can include metals, alloys (including steel), glasses, ceramics or glass lined metals, and coated metals.
  • the reactor can also include a reaction vessel enclosing a reaction chamber.
  • reaction vessel and reaction chamber are variable and can depend on the production capacity, feed volume, and catalyst.
  • the geometries of the reactor can be adjustable in various ways known to one of ordinary skill in the art.
  • reaction conditions within the reaction chamber can be isothermal. That is, hydrogenation of C0 2 can be conducted under isothermal conditions.
  • a temperature gradient can be established within the reaction chamber. For example, hydrogenation of C0 2 can be conducted across a temperature gradient using an adiabatic reactor.
  • the pressure within the reaction chamber can be varied, as is known in the art.
  • the pressure within the reaction chamber can be atmospheric pressure, i.e., about 1 bar.
  • Catalysts suitable for use in conjunction with the presently disclosed matter can be catalysts capable of catalyzing RWGS reactions, i.e., hydrogenation of C0 2 .
  • the catalyst can be a solid catalyst, e.g., a solid-supported catalyst.
  • the catalyst can be a metal oxide or mixed metal oxide.
  • the catalyst can be located in a fixed packed bed, i.e., a catalyst fixed bed.
  • the catalyst can include solid pellets, granules, plates, tablets, or rings.
  • the catalyst can include one or more transition metals.
  • the catalyst can include chromium (Cr).
  • the catalyst can include a solid support. That is, the catalyst can be solid-supported.
  • the solid support can include various metal salts, metalloid oxides, and/or metal oxides, e.g., titania (titanium oxide), zirconia (zirconium oxide), silica (silicon oxide), alumina (aluminum oxide), magnesia (magnesium oxide), and magnesium chloride.
  • the solid support can include alumina (A1 2 0 3 ), silica (Si0 2 ), magnesia (MgO), titania (Ti0 2 ), zirconia (Zr0 2 ), cerium(IV) oxide (Ce0 2 ), or a combination thereof.
  • the amount of the solid support present in the catalyst can be between about 15% and about 95%, by weight, relative to the total weight of the catalyst.
  • the solid support can constitute about 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 55%, 60%, 65%, 70%, 75%, 80%, 85%, 90%, or 95% of the total weight of the catalyst.
  • the catalyst can include about 1% to about 25% Cr, by weight.
  • the catalyst can include about 1%, 2%, 3%, 4%, 5%, 6%, 7%, 8%, 9%, 10%, 11%, 12%, 13%, 14%, 15%, 16%, 17%, 18%, 20%, 22%, or 25% Cr, by weight.
  • the remainder of the catalyst can be solid support (e.g., AI 2 O 3 ).
  • the catalyst includes about 17% Cr supported on AI 2 O 3 .
  • the catalysts of the presently disclosed subject matter can be prepared according to various techniques known in the art.
  • metal oxide catalysts suitable for use in RWGS reactions can be prepared from various metal nitrates, metal halides, metal salts of organic acids, metal hydroxides, metal carbonates, metal oxyhalides, metal sulfates, and the like.
  • a transition metal oxide e.g., a Cr oxide
  • a solid support e.g., AI 2 O 3
  • the presently disclosed subject matter provides methods of converting mixtures of H 2 and C0 2 into syngas via the reverse water gas shift (RWGS) reaction.
  • a mixture of H 2 and C0 2 can be termed a "reaction mixture.”
  • the mixture of H 2 and C0 2 can alternatively be termed a "feed mixture” or "feed gas.”
  • the C0 2 in the reaction mixture can be derived from various sources.
  • the C0 2 can be a waste product from an industrial process.
  • C0 2 that remains unreacted in the RWGS reaction can be recovered and recycled back into the RWGS reaction.
  • Reaction mixtures suitable for use with the presently disclosed methods can include various proportions of H 2 and C0 2 .
  • the reaction mixture can include H 2 and C0 2 in a molar ratio (H 2 :C0 2 ) between about 5:1 and about 1:2, e.g., about 5:1, 4:1, 3:1, 2.8:1, 2.6:1, 2.5:1, 2.4:1, 2.3:1, 2.2:1, 2.1:1, 2:1, 1.9:1, 1.8:1, 1.7:1, 1.6:1, 1.5:1, 1.4:1, 1.3:1, 1.2:1, 1.1:1, 1:1, 1:1.1, 1:1.2, 1:1.3, 1:1.4, 1:1.5, 1:1.6, 1:1.7, 1:1.8, 1:1.9, or 1:2.
  • the reaction mixture can include H 2 and C0 2 in a molar ratio (H 2 :C0 2 ) of about 2: 1 to about 1 : 1. In certain embodiments, the reaction mixture can include H 2 and C0 2 in a molar ratio (H 2 :C0 2 ) of about 1 :2.
  • an exemplary method 100 can include providing a reaction chamber, as described above.
  • the reaction chamber can include a solid-supported catalyst, as described above ⁇ see FIG. 1, 101).
  • the method can further include feeding a reaction mixture, as described above, to the reaction chamber 102.
  • the method can additionally include contacting H 2 and C0 2 (present in the reaction mixture) with the catalyst at a reaction temperature of 600 °C or less, thereby inducing a RWGS reaction to provide a product mixture that includes H 2 and CO 103.
  • the product mixture can further include H 2 0 (a product of the RWGS reaction, as shown in Equation 1) and unreacted C0 2 .
  • the reaction mixture can be fed into the reaction chamber at various flow rates.
  • the flow rate can be varied for each component of the reaction mixture, as is known in the art.
  • the flow rate of each individual component can be about 600 cc/min to about 1300 cc/min.
  • the flow rate can be about 600 cc/min to about 700 cc/min or about 1100 cc/min to about 1300 cc/min.
  • the catalyst is present in amount of from about 1 to about 1000 mL. In certain embodiments, the catalyst is present in amount of from about 250 to about 750 mL. In certain embodiments, the catalyst is present in amount of about 426 mL.
  • the reaction temperature can be understood to be the temperature within the reaction chamber.
  • the reaction temperature can influence the RWGS reaction, including conversion of C0 2 and H 2 , the ratio of H 2 :CO in the product mixture, and the overall yield.
  • the reaction temperature can be greater than 560 °C, e.g., greater than about 570 °C, 580 °C, 590 °C, 600 °C.
  • the reaction temperature can be less than 600 °C, e.g., less than about 610 °C, 600 °C, 590 °C, 580 °C, and 570°C.
  • the reaction temperature can be between about 560 °C and about 800 °C.
  • the reaction temperature can be between about 550 °C and about 600 °C. In certain embodiments, the reaction temperature can be about 600 °C. In certain embodiments, the reaction temperature can be about 590 °C. In certain embodiments, the reaction temperature can be about 580 °C.
  • the RWGS can proceed with partial conversion of C0 2 and H 2 , thus providing a product mixture that includes CO, H 2 0, C0 2 , and H 2 .
  • the RWGS reaction can be performed to about 50% conversion of C0 2 .
  • Adjustment of the degree of conversion of C0 2 and H 2 as well as adjustment of the ratio of C0 2 and H 2 in the reaction mixture can therefore influence the ratio of H 2 and CO in the syngas product formed. For example, use of a higher molar ratio of H 2 :C0 2 in the reaction mixture can increase the molar ratio of H 2 :CO in the product mixture.
  • the product mixture can include H 2 and CO in a molar ratio (H 2 :CO) of about 0.5: 1 to about 5: 1.
  • the product mixture can include H 2 and CO in a molar ratio (H 2 :CO) of about 1 : 1 to about 3 : 1, e.g., about 1 : 1, 1.1 : 1, 1.2: 1, 1.3 : 1, 1.4: 1, 1.5: 1, 1.6: 1, 1.7: 1, 1.8: 1, 1.9: 1, 2: 1, 2.1 : 1, 2.2: 1, 2.3 : 1, 2.4: 1, 2.5: 1, 2.6: 1, 2.7: 1, 2.8: 1, 2.9: 1, or 3 : 1.
  • the product mixture can include H 2 and CO in a molar ratio (H 2 :CO) of about 1.5: 1 to about 3 : 1, about 2: 1 to about 3 : 1, or about 2.5: 1.
  • the molar ratio (H 2 :CO) of the product mixture can be influenced by the molar ratio (H 2 :C0 2 ) of the reaction mixture.
  • the RWGS can be performed to relatively high conversion. That is, the amount of C0 2 present in the product mixture can be relatively low.
  • the product mixture can include less than about 25% C0 2 , by mole or less than about 20% C0 2 , by mole.
  • the product mixture can include about 24%, 23%, 22%, 21%, 20%, 19%, 18%, 17%, 16%, 15%, 14%, 13%, 12%, 11%, 10%, 9%, 8% by mole.
  • the methods of the presently disclosed subject matter can include separating at least a portion of C0 2 and/or H 2 0 from the product mixture, to provide purified syngas.
  • CO 2 and/or H 2 0 can be separated by various techniques known in the art.
  • H 2 0 can be separated by condensation, e.g., by cooling the product mixture
  • CO 2 can be removed from the product mixture and contributed to the reaction mixture, thereby recycling CO 2 through the RWGS reaction and improving overall economy of the process.
  • an exemplary method of preparing light olefins can include conducting a RWGS reaction to convert CO 2 and H 2 into a product mixture that includes H 2 , CO, CO 2 , and H 2 0, as described above.
  • the method can additionally include separating at least a portion of C0 2 and H 2 0 from the product mixture, to provide purified syngas.
  • the method can further include subjecting purified syngas to a Fischer- Tropsch synthesis (FT) reaction to provide light olefins.
  • FT Fischer- Tropsch synthesis
  • the methods of the presently disclosed subject matter can have advantages over other techniques for preparation of syngas and preparation of light olefins.
  • the presently disclosed subject matter includes the surprising discovery that catalysts containing Cr can be used to promote RWGS reactions at temperatures at 600 °C or less without sacrificing product purity or catalyst stability.
  • Additional advantages of the presently disclosed subject matter can include preparation of syngas with improved H 2 :CO ratios.
  • the methods of the presently disclosed subject matter can provide syngas containing H 2 and CO in molar ratios suitable for use in further reactions, e.g., FT reactions.
  • the methods of the presently disclosed subject matter can prepare syngas via hydrogenation of C0 2 with minimal side reactions, good catalyst stability, and good yields of syngas. Additional advantages of the presently disclosed subject matter can include improved energy efficiency and overall economy.
  • a reactor was charged with a 426 mL of a Catofin® catalyst containing 17% Cr, by weight, supported on AI2O3.
  • the catalyst was in pellet form, size 3x7 millimeter.
  • the reactor was heated to 600 °C.
  • a reaction mixture containing H 2 at a flow rate of 603 cc/min and C0 2 at a flow rate of 1206 cc/min was fed into the reactor at atmospheric pressure, thereby contacting the reaction mixture with the catalyst and inducing a RWGS reaction.
  • a product mixture containing H 2 , C0 2 , CO, and H 2 0 was removed from the reactor.
  • Table 1 The composition of the reactants and purified mixture is presented in Table 1.
  • a reactor was charged with a 426 mL of a Catofin® catalyst containing 17% Cr, by weight, supported on A1 2 0 3 .
  • the catalyst was in pellet form, size 3x7 millimeter.
  • the reactor was heated to 590 °C.
  • a reaction mixture containing H 2 at a flow rate of 603 cc/min and C0 2 at a flow rate of 1206 cc/min was fed into the reactor at atmospheric pressure, thereby contacting the reaction mixture with the catalyst and inducing a RWGS reaction.
  • a product mixture containing H 2 , C0 2 , CO, and H 2 0 was removed from the reactor.
  • Table 2 The composition of the reactants and purified mixture is presented in Table 2. Table 2.
  • a reactor was charged with a 426 mL of a Catofin® catalyst containing 17% Cr, by weight, supported on AI2O3.
  • the catalyst was in pellet form, size 3x7 millimeter.
  • the reactor was heated to 580 °C.
  • a reaction mixture containing H 2 at a flow rate of 603 cc/min and C0 2 at a flow rate of 1206 cc/min was fed into the reactor at atmospheric pressure, thereby contacting the reaction mixture with the catalyst and inducing a RWGS reaction.
  • a product mixture containing H 2 , C0 2 , CO, and H 2 0 was removed from the reactor.
  • Table 3 The composition of the reactants and purified mixture is presented in Table 3.

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Abstract

L'invention porte sur des procédés de préparation de gaz de synthèse. Un procédé donné à titre d'exemple peut comprendre l'hydrogénation du dioxyde de carbone (CO2) par conversion du gaz à l'eau (RWGS). Des catalyseurs comprenant du Cr peuvent être utilisés, et la RWGS peut être réalisée à une température de 600 °C ou moins.
PCT/US2016/058395 2015-10-30 2016-10-24 Procédés basse température pour hydrogénation de co2 pour la production de compositions de gaz de synthèse à faible rapports h2/co WO2017074843A1 (fr)

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KR20190136978A (ko) * 2018-05-30 2019-12-10 한국화학연구원 에너지 효율적인 이산화탄소의 전환 시스템 및 방법
CN112169799A (zh) * 2019-07-02 2021-01-05 中国科学院大连化学物理研究所 采用铁基催化剂进行二氧化碳加氢合成低碳烯烃的方法
WO2023222798A1 (fr) * 2022-05-19 2023-11-23 Totalenergies Onetech Procédé de production de combustible durable par l'intermédiaire du monoxyde de carbone
US11827521B2 (en) 2021-12-14 2023-11-28 Industrial Technology Research Institute Method for selectively chemically reducing CO2 to form CO
WO2024000397A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Procédés fischer-tropsch intégrés utilisant des catalyseurs de conversion inverse eau-gaz au nickel

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KR102183215B1 (ko) 2018-05-30 2020-11-25 한국화학연구원 에너지 효율적인 이산화탄소의 전환 시스템 및 방법
CN112169799A (zh) * 2019-07-02 2021-01-05 中国科学院大连化学物理研究所 采用铁基催化剂进行二氧化碳加氢合成低碳烯烃的方法
CN112169799B (zh) * 2019-07-02 2022-04-22 中国科学院大连化学物理研究所 采用铁基催化剂进行二氧化碳加氢合成低碳烯烃的方法
US11827521B2 (en) 2021-12-14 2023-11-28 Industrial Technology Research Institute Method for selectively chemically reducing CO2 to form CO
US11981573B2 (en) 2021-12-14 2024-05-14 Industrial Technology Research Institute Catalyst for selectively chemically reducing CO2 to form CO
WO2023222798A1 (fr) * 2022-05-19 2023-11-23 Totalenergies Onetech Procédé de production de combustible durable par l'intermédiaire du monoxyde de carbone
WO2024000397A1 (fr) * 2022-06-30 2024-01-04 Bp P.L.C. Procédés fischer-tropsch intégrés utilisant des catalyseurs de conversion inverse eau-gaz au nickel

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