WO2023157835A1 - リアクタモジュール - Google Patents

リアクタモジュール Download PDF

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Publication number
WO2023157835A1
WO2023157835A1 PCT/JP2023/004983 JP2023004983W WO2023157835A1 WO 2023157835 A1 WO2023157835 A1 WO 2023157835A1 JP 2023004983 W JP2023004983 W JP 2023004983W WO 2023157835 A1 WO2023157835 A1 WO 2023157835A1
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Prior art keywords
reactor
membrane
prereactor
raw material
gas
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Ceased
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PCT/JP2023/004983
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English (en)
French (fr)
Japanese (ja)
Inventor
剛佑 中川
和希 飯田
博史 菅
淳史 鳥井
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NGK Insulators Ltd
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NGK Insulators Ltd
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Application filed by NGK Insulators Ltd filed Critical NGK Insulators Ltd
Priority to CN202380019071.3A priority Critical patent/CN118613319A/zh
Priority to EP23756360.6A priority patent/EP4480569A4/en
Priority to AU2023222786A priority patent/AU2023222786B2/en
Priority to JP2024501381A priority patent/JP7637310B2/ja
Publication of WO2023157835A1 publication Critical patent/WO2023157835A1/ja
Priority to US18/679,548 priority patent/US20240316527A1/en
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2475—Membrane reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/58—Multistep processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2445—Stationary reactors without moving elements inside placed in parallel
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/245—Stationary reactors without moving elements inside placed in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B01J8/009—Membranes, e.g. feeding or removing reactants or products to or from the catalyst bed through a membrane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
    • B01J8/0496—Heating or cooling the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
    • C07B61/00—Other general methods
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
    • C07C31/02—Monohydroxylic acyclic alcohols
    • C07C31/04—Methanol
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/24—Stationary reactors without moving elements inside
    • B01J2219/2401—Reactors comprising multiple separate flow channels
    • B01J2219/2402—Monolithic-type reactors
    • B01J2219/2423—Separation means, e.g. membrane inside the reactor

Definitions

  • the present invention relates to reactor modules.
  • membrane reactors have been developed that can improve the conversion efficiency by separating the products in the conversion reaction from raw material gases containing hydrogen and carbon oxides to liquid fuels (methanol, ethanol, etc.).
  • Patent Document 1 discloses a membrane reactor that includes a channel through which a raw material gas flows, a catalyst arranged in the channel, and a separation membrane that allows water vapor, which is one of the products, to pass through.
  • the purpose of the present invention is to provide a reactor module that can improve the cost performance of separation membranes.
  • a reactor module includes a prereactor and a membrane reactor arranged downstream of the prereactor and having a separation membrane.
  • the prereactor produces an intermediate gas containing liquid fuel, water vapor and residual feed gas from a feed gas containing hydrogen and carbon oxides.
  • the membrane reactor produces liquid fuel and steam from the residual feed gas.
  • the separation membrane allows water vapor contained in the intermediate gas and water vapor generated from the residual raw material gas to pass therethrough.
  • FIG. 1 is a schematic diagram showing the configuration of a reactor system 100. As shown in FIG. Reactor system 100 comprises source gas source 10 and reactor module 15 .
  • the reactor module 15 includes a prereactor 20 and a membrane reactor 30.
  • the pre-reactor 20 and the membrane reactor 30 may be housed in separate pressure-resistant containers, or may be collectively housed in one pressure-resistant container. If the prereactor 20 and the membrane reactor 30 are housed in separate pressure-resistant containers, the temperatures of the prereactor 20 and the membrane reactor 30 can be individually controlled, which is more preferable.
  • FIG. 1 cross sections of the prereactor 20 and the membrane reactor 30 are schematically illustrated.
  • the source gas source 10 is arranged upstream of the prereactor 20 .
  • the raw material gas source 10 stores raw material gas.
  • the raw material gas source 10 supplies the raw material gas to the prereactor 20 .
  • the source gas contains at least hydrogen and carbon oxide. At least one of carbon monoxide and carbon dioxide can be used as the carbon oxide.
  • the source gas may be a so-called synthesis gas (Syngas).
  • the prereactor 20 is arranged downstream of the source gas source 10 .
  • the pre-reactor 20 is arranged upstream of the membrane reactor 30 .
  • a raw material gas is supplied to the prereactor 20 from the raw material gas source 10 .
  • the prereactor 20 produces an intermediate gas by performing a conversion reaction from raw material gas to liquid fuel.
  • Pre-reactor 20 supplies intermediate gas to membrane reactor 30 .
  • the liquid fuel is a fuel that is liquid at room temperature and pressure, or a fuel that can be liquefied at room temperature and pressure.
  • fuels in a liquid state at normal temperature and pressure include methanol, ethanol, liquid fuels represented by C n H 2 (m-2n) (m is an integer less than 90, n is an integer less than 30), and these mixtures.
  • the liquid fuel produced in the prereactor 20 is in a gaseous state when it is produced and is maintained in a gaseous state at least until it flows out of the prereactor 20 .
  • Fuels that can be liquefied at room temperature and under pressure include, for example, propane, butane, and mixtures thereof.
  • reaction formula (1) for synthesizing methanol by catalytically hydrogenating a raw material gas containing hydrogen and carbon dioxide in the presence of a catalyst is as follows. CO2 + 3H2 ⁇ CH3OH + H2O (1)
  • the intermediate gas contains the liquid fuel produced by the conversion reaction, steam that is one of the products of the conversion reaction, and residual raw material gas that has not been used in the conversion reaction.
  • the content of water vapor in the intermediate gas can be determined according to the permeation performance of the separation membrane 34 of the membrane reactor 30, which will be described later.
  • the content of residual raw material gas in the intermediate gas can be determined according to the conversion efficiency in membrane reactor 30 .
  • the operating temperature of the prereactor 20 is preferably higher than the operating temperature of the membrane reactor 30. Since the prereactor 20 does not have a separation membrane, the operating temperature can be set to a temperature suitable for the catalytic activity of the first catalyst 23 without considering the heat resistance of the separation membrane.
  • the operating temperature of the prereactor 20 can be, for example, 180° C. or higher and 350° C. or lower.
  • the operating temperature of the prereactor 20 is the intermediate temperature flowing through a portion (hereinafter referred to as “prereactor adjacent portion”) of a connecting pipe (not shown) between the prereactor 20 and the membrane reactor 30 , which is close to the prereactor 20 . means the temperature of the gas.
  • the operating temperature of the prereactor 20 can be measured using a thermocouple, a resistance temperature detector, a thermistor, or the like. If it is difficult to measure the temperature of the intermediate gas flowing in the vicinity of the pre-reactor, a measurement location is provided on the outer surface of the vicinity of the pre-reactor and covered with a heat insulating material to reduce the influence of the outside temperature. The temperature may be measured and the temperature of the intermediate gas flowing therein may be estimated based on the measured temperature.
  • the prereactor 20 includes a reaction tube 21, a first channel 22, and a first catalyst 23. Prereactor 20 does not have a separation membrane.
  • a first channel 22 is formed inside the reaction tube 21 .
  • a raw material gas flows through the first flow path 22 .
  • a first catalyst 23 is arranged in the first flow path 22 .
  • the first catalyst 23 promotes the conversion reaction described above.
  • An intermediate gas produced by the conversion reaction is recovered from the first flow path 22 .
  • the prereactor 20 according to this embodiment has three first flow paths 22, the number of the first flow paths 22 may be one or more.
  • the first catalyst 23 a known catalyst suitable for the conversion reaction to the desired liquid fuel can be used.
  • the first catalyst 23 include metal catalysts (copper, palladium, etc.), oxide catalysts (zinc oxide, zirconia, gallium oxide, etc.), and composite catalysts thereof (copper-zinc oxide, copper-zinc oxide -alumina, copper-zinc oxide-chromium oxide-alumina, copper-cobalt-titania, and catalysts obtained by modifying these with palladium, etc.).
  • the configuration of the prereactor 20 has been described above, the configuration of the prereactor 20 can be changed as appropriate.
  • a well-known reactor without a separation membrane for example, JP-A-2005-298413, JP-A-2010-13422, etc.
  • a membrane reactor 30 is arranged downstream of the pre-reactor 20 .
  • the intermediate gas is supplied from the pre-reactor 20 to the membrane reactor 30 .
  • the membrane reactor 30 converts the residual raw material gas contained in the intermediate gas into a liquid fuel (see the above reaction formula (1)), while the water vapor generated in the prereactor 20 and the water vapor generated in the membrane reactor 30 are Separate from water vapor.
  • the equilibrium shift effect can be utilized to shift the reaction equilibrium of the above formula (1) to the product side.
  • the liquid fuel generated in the membrane reactor 30 is in a gaseous state when it is generated, and is maintained in a gaseous state at least until it flows out of the membrane reactor 30 .
  • the operating temperature of the membrane reactor 30 is set in consideration of the heat resistance of the separation membrane 34.
  • the operating temperature of membrane reactor 30 may be lower than the operating temperature of prereactor 20 .
  • the operating temperature of the membrane reactor 30 can be, for example, 160° C. or higher and 300° C. or lower.
  • the operating temperature of the membrane reactor 30 refers to the inside of a portion of a discharge pipe (not shown) that discharges the liquid fuel from the membrane reactor 30 to the outside and that is close to the membrane reactor 30 (hereinafter referred to as a “membrane reactor-adjacent portion”). means the temperature of the flowing liquid fuel.
  • the operating temperature of membrane reactor 30 can be measured using a thermocouple, a resistance temperature detector, a thermistor, or the like.
  • a measurement location is provided on the outer surface of the membrane reactor vicinity and covered with a heat insulating material to reduce the influence of the outside temperature.
  • the temperature may be measured and the temperature of the liquid fuel flowing therein may be estimated based on the measured temperature.
  • the membrane reactor 30 includes a porous support 31 , a second channel 32 , a second catalyst 33 , a separation membrane 34 and a third channel 35 .
  • the porous support 31 is composed of a porous material.
  • a ceramic material a metal material, a resin material, or the like can be used, and a ceramic material is particularly suitable.
  • aggregates for ceramic materials include alumina (Al 2 O 3 ), titania (TiO 2 ), mullite (Al 2 O 3 SiO 2 ), cerven and cordierite (Mg 2 Al 4 Si 5 O 18 ). At least one of them can be used. At least one of titania, mullite, sinterable alumina, silica, glass frit, clay mineral, and sinterable cordierite can be used as the inorganic binder for the ceramic material.
  • the ceramic material need not contain inorganic binders.
  • the second channel 32 is formed in the porous support 31 .
  • the second channel 32 penetrates the porous support 31 . Therefore, both ends of the second channel 32 are open to the outer surface of the porous support 31 .
  • the second channel 32 is a space on the non-permeate side of the separation membrane 34 .
  • An intermediate gas flows through the second flow path 32 .
  • the intermediate gas contains liquid fuel produced in the prereactor 20 , steam produced in the prereactor 20 , and residual feed gas not used in the conversion reaction in the prereactor 20 .
  • the membrane reactor 30 according to this embodiment has two second flow paths 32, the number of the second flow paths 32 may be one or more.
  • the second catalyst 33 is arranged inside the second flow path 32 .
  • a known catalyst suitable for the conversion reaction to the desired liquid fuel can be used.
  • the second catalyst 33 accelerates the conversion reaction.
  • the second catalyst 33 include metal catalysts (copper, palladium, etc.), oxide catalysts (zinc oxide, zirconia, gallium oxide, etc.), and composite catalysts thereof (copper-zinc oxide, copper-zinc oxide -alumina, copper-zinc oxide-chromium oxide-alumina, copper-cobalt-titania, and catalysts obtained by modifying these with palladium, etc.).
  • the second catalyst 33 is used for the conversion reaction of the residual raw material gas contained in the intermediate gas. Therefore, the load on the second catalyst 33 can be reduced as compared with the case where the second catalyst 33 is directly used for the conversion reaction of all the raw material gases. In this way, by making the first catalyst 23 of the prereactor 20 bear part of the burden necessary for the conversion reaction of the raw material gas, the burden on the second catalyst 33 of the membrane reactor 30 can be reduced. 33 can be extended.
  • the separation membrane 34 is supported by the porous support 31.
  • a separation membrane 34 surrounds the second channel 32 .
  • Separation membrane 34 is arranged between second channel 32 and third channel 35 .
  • the separation membrane 34 is permeable to water vapor. Specifically, the separation membrane 34 permeates the water vapor originally contained in the intermediate gas and the water vapor newly generated from the residual material gas contained in the intermediate gas.
  • the upstream portion of the separation membrane 34 is mainly used for the permeation of water vapor originally contained in the intermediate gas, and the downstream portion of the separation membrane 34 is newly generated from the residual raw material gas. Mainly used for water vapor permeation.
  • the upstream portion of the separation membrane 34 can be utilized by performing the conversion reaction using the intermediate gas containing water vapor, so that the entire separation membrane 34 can be evenly and effectively utilized. Therefore, the cost performance of the separation membrane 34 can be improved.
  • An inorganic membrane can be used as the separation membrane 34 .
  • An inorganic film is preferable because it has heat resistance, pressure resistance, and water vapor resistance.
  • inorganic membranes include zeolite membranes, silica membranes, alumina membranes, and composite membranes thereof.
  • an LTA-type zeolite membrane in which the molar ratio (Si/Al) of silicon element (Si) and aluminum element (Al) is 1.0 or more and 3.0 or less is preferable because it has excellent water vapor permeability. be.
  • the separation membrane 34 preferably has a water vapor permeability coefficient of 100 nmol/(s ⁇ Pa ⁇ m 2 ) or more.
  • the water vapor permeability coefficient can be determined by a known method (see Ind. Eng. Chem. Res., 40, 163-175 (2001)).
  • the separation membrane 34 preferably has a separation factor of 100 or more. The higher the separation factor, the easier it is for water vapor to permeate, and the less it is for components other than water vapor (hydrogen, carbon dioxide, liquid fuel, etc.) to permeate.
  • the separation factor can be determined by a known method (see Fig. 1 of "Separation and Purification Technology 239 (2020) 116533").
  • a third channel 35 is formed in the porous support 31 .
  • a third channel 35 penetrates the porous support 31 . Therefore, both ends of the third channel 35 are open.
  • the second channel 32 is a space on the permeate side of the separation membrane 34 .
  • a sweep gas for sweeping the water vapor that has permeated through the separation membrane 34 is passed through the third channel 35 .
  • An inert gas for example, nitrogen
  • air can be used as the sweep gas.
  • the membrane reactor 30 according to the present embodiment has one third flow path 35, the number of the third flow paths 35 may be one or more. No catalyst is placed in the third flow path 35 .
  • a monolith means a structure having a plurality of holes penetrating in the longitudinal direction, and is a concept including a honeycomb.
  • the reactor module 15 is provided with only one membrane reactor 30 in the above embodiment, it may be provided with a plurality of membrane reactors 30 .
  • each membrane reactor 30 is connected to the pre-reactor 20 .
  • the intermediate gas produced in prereactor 20 is distributed to each membrane reactor 30 .
  • a plurality of membrane reactors 30 can be arranged in series.
  • the most upstream membrane reactor 30 among the plurality of membrane reactors 30 is connected to the pre-reactor 20, and the remaining membrane reactors 30 are connected downstream thereof.
  • the intermediate gas produced in the pre-reactor 20 is supplied to the membrane reactor 30 positioned most upstream.
  • the product gas generated in each membrane reactor 30 is supplied to other membrane reactors 30 located downstream.
  • the product gas includes liquid fuel and residual feed gas.
  • the product gas may contain water vapor.
  • a plurality of membrane reactors 30 may be arranged in a combination of parallel and series.
  • the first catalyst 23 of the pre-reactor 20 bears part of the load required for the conversion reaction of the source gas.
  • the load on the second catalyst 33 of each of the membrane reactors 30 can be reduced.
  • the sweep gas is made to flow through the third flow path 35 , but the sweep gas does not have to flow through the third flow path 35 .
  • the intermediate gas is directly supplied from the pre-reactor 20 to the membrane reactor 30 in the above embodiment, it may be supplied to the membrane reactor 30 after being cooled.
  • a cooling device (radiator or heat exchanger) can be arranged between the pre-reactor 20 and the membrane reactor 30 to cool the intermediate gas in the cooling device.
  • the separation membrane 34 allows the water vapor generated in the pre-reactor 20 and the water vapor generated in the membrane reactor 30 to pass through, but it is not limited to this.
  • the separation membrane 34 may permeate the liquid fuel that is the product in the prereactor 20 and the liquid fuel that is the product in the membrane reactor 30 . Also in this case, the reaction equilibrium of the above formula (1) can be shifted to the product side.
  • the separation membrane 34 is permeable to the liquid fuel, even when the liquid fuel is generated by a reaction that does not generate water vapor (for example, 2H 2 +CO ⁇ CH 3 OH), the reaction equilibrium is shifted to the product side. be able to.
  • a reaction that does not generate water vapor for example, 2H 2 +CO ⁇ CH 3 OH
  • the raw material gas containing hydrogen and carbon oxide is directly supplied to the prereactor 20, but while the raw material gas is generated in the prereactor 20, the generated raw material gas is used to produce liquid fuel. may be generated.
  • reaction formula (2) when ammonia and carbon dioxide are supplied to the prereactor 20, hydrogen, which is a part of the raw material gas, is generated from ammonia according to the following reaction formula (2), and raw material gas (hydrogen and carbon dioxide) to produce methanol.
  • reaction formula (4) summarizes reaction formulas (2) and (3).
  • Source Gas Source 15 Reactor Module 20 Prereactor 21 Reaction Tube 22 First Channel 23 First Catalyst 30 Membrane Reactor 31 Porous Support 32 Second Channel 33 Second Catalyst 34 Separation Membrane 35 Third Channel

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
PCT/JP2023/004983 2022-02-18 2023-02-14 リアクタモジュール Ceased WO2023157835A1 (ja)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CN202380019071.3A CN118613319A (zh) 2022-02-18 2023-02-14 反应器模块
EP23756360.6A EP4480569A4 (en) 2022-02-18 2023-02-14 REACTOR MODULE
AU2023222786A AU2023222786B2 (en) 2022-02-18 2023-02-14 Reactor module
JP2024501381A JP7637310B2 (ja) 2022-02-18 2023-02-14 リアクタモジュール
US18/679,548 US20240316527A1 (en) 2022-02-18 2024-05-31 Reactor module

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JP2022-024238 2022-02-18
JP2022024238 2022-02-18

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US18/679,548 Continuation US20240316527A1 (en) 2022-02-18 2024-05-31 Reactor module

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WO2023157835A1 true WO2023157835A1 (ja) 2023-08-24

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See also references of EP4480569A4

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