WO2023286803A1 - Dispositif de réaction isotherme - Google Patents

Dispositif de réaction isotherme Download PDF

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Publication number
WO2023286803A1
WO2023286803A1 PCT/JP2022/027552 JP2022027552W WO2023286803A1 WO 2023286803 A1 WO2023286803 A1 WO 2023286803A1 JP 2022027552 W JP2022027552 W JP 2022027552W WO 2023286803 A1 WO2023286803 A1 WO 2023286803A1
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WIPO (PCT)
Prior art keywords
heat transfer
transfer medium
reaction tube
tube
fluid
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PCT/JP2022/027552
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English (en)
Japanese (ja)
Inventor
公一 横山
正志 清澤
郷紀 佐々木
Original Assignee
三菱重工業株式会社
三菱パワー株式会社
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Publication of WO2023286803A1 publication Critical patent/WO2023286803A1/fr

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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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/755—Nickel
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • 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
    • 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
    • C07C1/12—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of a carbon from carbon dioxide with hydrogen
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C9/00—Aliphatic saturated hydrocarbons
    • C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
    • C07C9/04—Methane
    • 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

Definitions

  • the present invention relates to a catalytic reactor. More particularly, the present invention relates to a catalytic reactor for chemically reacting fluid raw materials in the presence of a catalyst to obtain fluid products.
  • Patent Document 1 discloses a catalytic gas-phase reaction catalyst that is used by being filled in a reaction tube, the shape of the catalyst is columnar, the length in the longitudinal direction is longer than the inner diameter of the reaction tube, and , after installing a columnar catalyst for catalytic gas phase reaction characterized by having at least one or more through holes in the longitudinal direction at the inlet end of the catalyst layer in the reaction tube, surrounding and / or behind the catalyst Disclosed is a catalytic gas-phase reaction method characterized in that the reaction is performed by filling a granular catalyst having a shape different from that of the catalyst.
  • Patent Document 2 discloses a catalytic reactor for gas phase reaction containing a cylindrical shaped catalyst reaction tube, wherein the cylindrical shaped catalyst reaction tube has an inlet and an outlet of the raw material gas of the catalytic reactor. discloses a catalytic reactor characterized by a gradient of catalytic activity in the direction of .
  • Patent Document 3 discloses a hybrid porous tubular body characterized by laminating a porous alloy sprayed coating on the inside and a porous ceramic sprayed coating.
  • An object of the present invention is to provide a catalytic reaction that has an excellent heat removal effect without causing an excessive temperature difference in the longitudinal direction and chemically reacts fluid raw materials in the presence of a catalyst to obtain a fluid product.
  • An object is to provide an apparatus and a catalytic reaction method.
  • a reaction tube comprising at least one first reaction tube and at least one second reaction tube; a heat transfer medium tube having a heat transfer medium inlet and a heat transfer medium outlet and having a heat transfer medium tube lumen communicating from the heat transfer medium inlet to the heat transfer medium outlet;
  • the first reaction tube comprises a cylindrical non-porous layer and a cylindrical porous layer laminated inside thereof, has a fluid inlet and a fluid outlet, and has a fluid inlet and a fluid outlet.
  • the second reaction tube is composed of a cylindrical non-porous layer, has a fluid inlet and a fluid outlet, and has a reaction tube lumen communicating from the fluid inlet to the fluid outlet. and a catalyst filled in the reaction tube lumen of the single-layer structure tube, the fluid outlet of the first reaction tube is connected to the fluid inlet of the second reaction tube such that the respective reaction tube lumens are in communication;
  • the fluid raw material flows into the reaction tube lumen at the fluid inlet of the first reaction tube, is brought into contact with the catalyst in the reaction tube lumen and chemically reacts, and reacts at the fluid outlet of the second reaction tube.
  • the first reactor is A reaction tube comprising a cylindrical non-porous layer and a cylindrical porous layer laminated inside thereof, having a fluid inlet and a fluid outlet, and communicating from the fluid inlet to the fluid outlet.
  • a first reaction tube comprising a multi-layer structure tube having cavities and a catalyst supported on the porous layer; a first heat transfer medium tube having a heat transfer medium inlet and a heat transfer medium outlet and having a heat transfer medium tube lumen communicating from the heat transfer medium inlet to the heat transfer medium outlet;
  • the fluid raw material flows into the reaction tube lumen at the fluid inlet of the first reaction tube, the fluid raw material is brought into contact with the catalyst in the reaction tube lumen and chemically reacts, and the reaction occurs at the fluid outlet of the first reaction tube.
  • the heat transfer medium flows into the heat transfer medium tube inner cavity at the heat transfer medium inlet of the first heat transfer medium tube, and the heat transfer medium flows out of the heat transfer medium tube inner cavity at the heat transfer medium outlet of the first heat transfer medium tube.
  • the second reactor is A single-layer structure tube comprising a cylindrical non-porous layer, having a fluid inlet and a fluid outlet, and having a reaction tube lumen communicating from the fluid inlet to the fluid outlet, and a single-layer structure tube.
  • a second reaction tube comprising a catalyst filled in the reaction tube lumen of a second heat transfer medium tube having a heat transfer medium inlet and a heat transfer medium outlet and having a heat transfer medium tube lumen communicating from the heat transfer medium inlet to the heat transfer medium outlet;
  • the fluid mixture a1 flows into the reaction tube lumen at the fluid inlet of the second reaction tube, contacts the catalyst in the reaction tube lumen to cause a chemical reaction, and reacts at the fluid outlet of the second reaction tube.
  • the heat transfer medium flows into the heat transfer medium tube inner cavity at the heat transfer medium inlet of the second heat transfer medium tube, and the heat transfer medium flows from the heat transfer medium tube inner cavity at the heat transfer medium outlet of the second heat transfer medium tube.
  • the second reaction tube is inserted through the heat transfer medium tube lumen of the second heat transfer medium tube, and the heat transfer medium in the heat transfer medium tube lumen flows through the reaction tube wall through the reaction tube lumen having a mechanism for exchanging heat with something inside, the fluid outlet of the first reactor is connected to the fluid inlet of the second reactor such that the respective reaction tube lumens are in communication; Catalytic reactor.
  • the first reaction tube comprises a cylindrical non-porous layer and a cylindrical porous layer laminated inside thereof, has a fluid inlet and a fluid outlet, and has a fluid inlet and a fluid outlet.
  • the second reaction tube is composed of a cylindrical non-porous layer, has a fluid inlet and a fluid outlet, and has a reaction tube lumen communicating from the fluid inlet to the fluid outlet. and a catalyst filled in the reaction tube lumen of the single-layer structure tube, and wherein the fluid outlet of the first reaction tube is connected to the fluid inlet of the second reaction tube in each reaction tube lumen. are communicatively connected to reaction tube.
  • the catalytic reaction apparatus and the catalytic reaction method of the present invention can uniformly control the temperature distribution in the reaction tube within a predetermined range, and can stably chemically react the fluid raw materials in the presence of the catalyst for a long period of time under a desired pressure. to obtain a fluid product.
  • INDUSTRIAL APPLICABILITY The present invention is preferably used in chemical reactions that utilize CO 2 to produce methane gas and water.
  • FIG. 1 is a vertical cross-sectional view showing an example of a reaction tube of the present invention
  • FIG. 2 is a cross-sectional view showing an example of a second reaction tube.
  • FIG. 3 is a vertical cross-sectional view showing another example of the reaction tube of the present invention;
  • It is a cross-sectional view showing another example of the first reaction tube.
  • It is a cross-sectional view showing another example of the first reaction tube.
  • BRIEF DESCRIPTION OF THE DRAWINGS It is a longitudinal cross-sectional view showing an example of a reactor equipped with the reaction tube of the present invention.
  • FIG. 3 is a vertical cross-sectional view showing another example of the reaction tube of the present invention
  • It is a cross-sectional view showing another example of the first reaction tube.
  • BRIEF DESCRIPTION OF THE DRAWINGS It is a longitudinal cross-sectional view showing an example of a reactor equipped
  • FIG. 2 is a perspective view showing an example of the appearance of the interior of the reactor of the present invention (with the end plate removed).
  • Figure 7 is a cross-sectional view of the reactor shown in Figure 6; It is a figure which shows an example of the catalytic reaction apparatus of this invention. It is a figure of the longitudinal section which shows an example of a 1st reaction tube. It is a longitudinal cross-sectional view showing an example of a second reaction tube. It is a figure which shows an example of the catalytic reaction apparatus of this invention.
  • 1 is a vertical cross-sectional view showing an example of a catalyst-filled reactor; FIG.
  • a catalytic reactor 30a of Embodiment 1 according to the present invention comprises a reactor 20 containing reaction tubes and heat transfer medium tubes (see FIG. 11).
  • the reactor 20 used in the present invention preferably has a plurality of reaction tubes.
  • Each reaction tube is preferably arranged such that its longitudinal direction is parallel to the longitudinal direction of the heat transfer medium tube (see FIGS. 8, 9 and 10). Also, each reaction tube may be interconnected with another adjacent reaction tube via plate fins.
  • the plurality of reaction tubes may all be the reaction tubes 10 of the present invention, or some may be the reaction tubes 10 of the present invention, but all are preferably the reaction tubes 10 of the present invention. .
  • the reaction tube 10 of the present invention comprises at least one first reaction tube a and at least one second reaction tube b (Figs. 2 and 4).
  • the first reaction tube a comprises a multi-layer structure tube and a catalyst.
  • the multi-layer structure tube consists of a cylindrical non-porous layer 2 and a cylindrical porous layer 1 laminated inside.
  • the multilayer structure tube has a fluid inlet and a fluid outlet, and has a reaction tube lumen 3 communicating from the fluid inlet to the fluid outlet.
  • a plane (cross section) cut perpendicular to the longitudinal direction of the multi-layer structure pipe can be, for example, circular, oval, elliptical, oval, square with rounded corners, square, or the like. From a point of view, it is preferably circular (see for example FIG. 1).
  • the inner and outer diameters of the multilayer structure tube can be appropriately designed according to the reaction scale, strength, pressure resistance, and the like.
  • the inner diameter and the outer diameter, in a cross section perpendicular to the longitudinal direction are defined as follows: It is a value (equivalent diameter) defined by 4A/L.
  • the fluid is liquid, gas, or gas-liquid mixture, preferably gas.
  • a porous layer is a layer having a structure with a large number of pores.
  • the porous layer preferably has pores (communicating pores) through which fluid can pass from one side to the other.
  • the porous layer does not need to have continuous pores, and may have dead-end pores as long as it has a pore volume into which a fluid can enter.
  • the porous layer serves as a carrier for the catalyst, it can be appropriately selected from metals, ceramics, etc., depending on the chemical reaction to be performed in the reaction tube. From the viewpoint of thermal conductivity, the porous layer is preferably made of metal.
  • the thickness of the porous layer in the multilayer structure tube is not particularly limited, but is, for example, 0.1 to 2.0 mm.
  • the relative density, porosity, open porosity, effective porosity, pore size distribution, etc. of the porous layer can be appropriately set according to the chemical reaction to be performed in the reaction tube.
  • the porous layer preferably has a relative density of 20% to 80%.
  • the relative density (density index) is defined by the following formula.
  • Relative density [%] apparent density / true density x 100
  • the true density is the density when only the volume occupied by the solid itself is used as the volume for density calculation, and can be calculated using the density of the metal bulk as the true density or based on the pycnometer method.
  • the apparent density is the density when the volume of the solid itself and internal voids is taken as the volume, and can be calculated based on the Archimedes method.
  • Bulk density is the density of the solid itself, pores and internal voids as a volume, and can be calculated based on a dimensional method using a vernier caliper, micrometer, or the like.
  • the non-porous layer in the multi-layer structure pipe is a layer with a dense or dense structure that does not substantially have communicating pores.
  • the non-porous layer is substantially impervious to fluid and prevents fluid from escaping.
  • the non-porous layer may have voids (internal voids) enclosed within the layer as long as the effects of the present invention are exhibited.
  • the non-porous layer preferably has a relative density of 99% or greater, most preferably 100%.
  • the non-porous layer can be appropriately selected from metals, ceramics, and the like. From the viewpoint of thermal conductivity, the non-porous layer is preferably made of metal.
  • the thickness of the non-porous layer in the multilayer structure tube is not particularly limited, but is, for example, 0.1 to 2.0 mm. From the viewpoint of thermal expansion, etc., it is preferable that the porous layer and the non-porous layer are made of the same material.
  • the transition of the ratio of pores from the porous layer to the non-porous layer may be stepwise or gradational.
  • the ratio of the thickness of the porous layer to the thickness of the non-porous layer is preferably 1/50 to 50/1, more preferably 1/30 to 10/1, and still more preferably 1/10 to 2/1. 1.
  • the catalyst in the multilayer structure tube is carried on the porous layer.
  • a catalyst can be appropriately selected according to the chemical reaction to be performed in the reaction tube.
  • Ni-based catalysts Ni-based catalysts, platinum group metal-based catalysts, other noble metal-based catalysts, and the like can be used.
  • methanation catalysts include nickel aluminate (NiAl x O y ), Ru/NiAl x O y , Ru/Al 2 O 3 , Ru/TiO 2 , Ni/TiO 2 , Ru—Ni/TiO 2 and the like. can be mentioned.
  • CO selective oxidation catalysts include Ru/Al 2 O 3 , Ru/C, Rh porphyrin/C, Co x —Fe 2 O, Co 3 O 4 , Cu/CeO 2 —ZrO 2 and Ni/CeO 2 .
  • the method for supporting the catalyst on the porous layer is not particularly limited.
  • the catalyst can be supported by contacting the porous layer with an aqueous solution or dispersion of the component that constitutes the catalyst (catalyst component).
  • Contacting the porous layer with the aqueous solution or dispersion of the catalyst component can be done by immersing the reaction tube having the porous layer in the aqueous solution or dispersion of the catalyst component, or by immersing the reaction tube with the porous layer in the aqueous solution of the catalyst component.
  • it can be carried out by a method of flowing a dispersion liquid, or the like.
  • a heat treatment eg, drying, baking, etc.
  • the second reaction tube b comprises a single-layer structure tube and a catalyst.
  • a single-layer structure tube consists of a cylindrical non-porous layer 2.
  • the single-layer structure tube has a fluid inlet and a fluid outlet, and has a reaction tube lumen 3 communicating from the fluid inlet to the fluid outlet.
  • the plane (cross section) cut at right angles to the longitudinal direction of the single-layer structure pipe can be, for example, circular, oval, elliptical, oval, square with rounded corners, square, etc. from the point of view, it is preferably circular.
  • the inner diameter and outer diameter of the single-layer structure tube can be appropriately designed according to the reaction scale, strength, pressure resistance, and the like.
  • the non-porous layer in the single-layer structure pipe may be, for example, a laminate of layers of different materials as long as it has a dense or minute structure that does not substantially have communicating pores.
  • the non-porous layer is substantially impervious to fluid and prevents fluid from escaping.
  • the non-porous layer may have voids (internal voids) enclosed within the layer as long as the effects of the present invention are exhibited.
  • the non-porous layer preferably has a relative density of 99% or greater, most preferably 100%.
  • the non-porous layer can be appropriately selected from metals, ceramics, and the like. From the viewpoint of thermal conductivity, the non-porous layer is preferably made of metal.
  • the thickness of the non-porous layer in the single-layer structure tube is not particularly limited, but is, for example, 0.1 to 4.0 mm.
  • the catalyst 1′′ is filled in the reaction tube lumen of the single-layer structure tube.
  • the catalyst can be appropriately selected according to the chemical reaction to be performed in the reaction tube.
  • the catalyst carried in the porous layer of the multi-layer structure tube can be the same as the catalyst supported in the porous layer.
  • the catalyst filled in the reaction tube lumen of the single-layer structure tube has the following forms: For example, a spherical body, an ellipsoidal body, a cylindrical body, etc. can be used, etc.
  • the packing density of the catalyst can be appropriately selected according to the chemical reaction to be performed in the reaction tube.
  • the fluid outlet of the first reaction tube a is connected to the fluid inlet of the second reaction tube b so that the inner lumen of each reaction tube communicates.
  • the first reaction tube a and the second reaction tube b may be directly connected, or as shown in FIG. may be connected via
  • the thickness of the first reaction tube may be the same as or different from that of the second reaction tube.
  • the length of the first reaction tube may be the same as or different from the length of the second reaction tube.
  • the volumes of the first reaction tube and the second reaction tube can be appropriately selected according to the chemical reactions to be performed in the reaction tubes.
  • the first reaction tube a further has a plate-like porous layer 4 protruding from the inner surface of the cylindrical porous layer toward the inner cavity of the reaction tube (Fig. 5).
  • the shape of the plate-like porous layer is not particularly limited.
  • the plate-like porous layer 5 has a cross shape (FIG. 6).
  • the plate-like porous layer 6 has a spiral shape (Fig. 7).
  • the plate-like porous layer contributes to controlling fluid flow, increasing the amount of catalyst supported, and increasing the contact area between the fluid and the porous layer. 5, 6, and 7, a plate-like non-porous layer is provided so as to protrude from the inner surface of the cylindrical non-porous layer of the second reaction tube b toward the inner cavity of the reaction tube. good too.
  • reaction tube of the present invention further has plate fins 11 protruding outward from the outer surface of the reaction tube.
  • the plate fins may be provided so that the plate surface is parallel to the longitudinal direction of the reaction tube, or may be provided so that the plate surface is helical.
  • the faces may be provided so as to be non-parallel (eg, perpendicular).
  • the ends of plate fins protruding outward from the outer surface of the tube are connected to the outer surface of another adjacent reaction tube.
  • plate fins 11 are provided so that the plate surface is parallel to the longitudinal direction of the reaction tube, and the end of the plate fin 11 is connected to the outer surface of another adjacent reaction tube. .
  • This makes it possible to suppress the vibration of the reaction tube, control the flow of the heat transfer medium, promote the release of reaction heat, and the like.
  • the ends of the plate fins projecting outward from the outer surface of the reaction tube may be connected to the inner surface of the heat transfer medium tube.
  • the plate fins are preferably made of the same material as the reaction tube.
  • the plate fins may be plate-shaped without holes or plate-shaped with holes.
  • a perforated plate can contribute to controlling the flow of the heat transfer medium, reducing dead space, and increasing the contact area with the heat transfer medium.
  • the hole is not limited to an elliptical shape, and can be formed in various shapes, and can be provided at an appropriate location depending on the purpose.
  • the plate fins may be made of non-porous material or may be made of porous material.
  • the heat transfer medium pipe 12 is a pipe having a heat transfer medium inlet 16 and a heat transfer medium outlet 17, and a heat transfer medium pipe inner cavity 13 communicating from the heat transfer medium inlet to the heat transfer medium outlet.
  • the surface cut perpendicular to the longitudinal direction of the heat transfer medium tube can be, for example, circular, oval, elliptical, oval, square with rounded corners, square, or the like. A circular shape is preferable from the viewpoint of pressure resistance and weight reduction.
  • the fluid raw material flows into the reaction tube lumen through the fluid inlet 8a of the first reaction tube a, and the fluid raw material is brought into contact with the catalyst in the reaction tube lumen.
  • a mechanism in which a chemical reaction is caused and a fluid mixture containing a fluid product obtained by the chemical reaction flows out from the reaction tube lumen at the fluid outlet 8b of the second reaction tube b, and heat transfer at the heat transfer medium inlet The heat transfer medium flows into the heat transfer medium tube lumen, and the heat transfer medium flows out from the heat transfer medium tube lumen at the heat transfer medium outlet, and the reaction tube is inserted through the heat transfer medium tube lumen. , the heat transfer medium in the heat transfer medium tube lumen exchanges heat with that in the reaction tube lumen through the reaction tube wall.
  • the fluid inlet 8a is distinguished from the heat transfer medium inlet 16 or the heat transfer medium outlet 17, and the fluid raw material flows into the reaction tube lumen at the fluid inlet of the first reaction tube.
  • the fluid inlet of the first reaction tube is distinguished from the heat transfer medium inlet or heat transfer medium outlet of the heat transfer medium tube, for example, by a plate 25 that holds the end of the reaction tube on the fluid inlet side. can be done.
  • a device for preparing the fluid raw material for example, a mixing mechanism for mixing each component constituting the fluid raw material at a predetermined ratio, and each component constituting the fluid raw material.
  • a tank for storage, a compressor 31, a heat exchanger 32, etc. can be installed.
  • the raw material is liquid such as liquefied carbon dioxide
  • a vaporizer 34 or the like can be provided for safely vaporizing the raw material.
  • Components constituting the fluid raw material can be appropriately selected according to the chemical reaction to be performed in the reactor.
  • the fluid raw material used for the methanation reaction of carbon dioxide contains at least hydrogen gas and carbon dioxide gas.
  • the flow rate of the fluid raw material into the inner lumen of the reaction tube can be appropriately set according to the chemical reaction to be performed in the reactor.
  • the heat transfer medium flows into the heat transfer medium tube lumen 13 at the heat transfer medium inlet.
  • the heat transfer medium is not particularly limited as long as it does not deteriorate in the temperature range for performing the desired chemical reaction and can maintain fluidity.
  • Specific examples of heat transfer media include polyhydric alcohols such as glycerin and polyglycol; phenols and phenolic ethers such as anisole, diphenyl ether and phenol; polyphenyls such as terphenyl, o-dichlorobenzene, poly Chlorinated benzenes and polyphenyls such as chloropolyphenyl; Silicic acid esters such as tetraallyl silicates; Fractionated tars and petroleum oils such as naphthalene derivatives, mineral oils; Nitrates and nitrites such as sodium nitrate, sodium nitrite, potassium nitrate silicones; fluorine compounds; glycols; molten metals and alloys such as Na metal,
  • the heat transfer medium inlet and the heat transfer medium outlet are not particularly limited in their arrangement, but are preferably arranged so that the heat transfer medium can easily flow in a direction perpendicular to the longitudinal direction of the reaction tube.
  • Partition plates can be provided alternately from the left and right sides of the inner surface of the heat transfer medium tube to cause the flow of the heat transfer medium to meander.
  • a spiral partition plate can be provided along the inner surface of the heat transfer medium tube to swirl the flow of the heat transfer medium.
  • the partition plate may have a hole through which the reaction tube can pass so as to hold the intermediate portion of the reaction tube.
  • the fluid outlet 8b is distinguished from the heat transfer medium inlet 16 or the heat transfer medium outlet 17, and the fluid mixture containing the fluid product flows out of the reaction tube lumen 3 at the fluid outlet 8b of the second reaction tube. do.
  • the fluid outlet of the second reaction tube is distinguished from the heat transfer medium inlet or heat transfer medium outlet of the heat transfer medium tube, for example, by a plate 26 that holds the end of the reaction tube on the fluid outlet side. can be done.
  • the heat transfer medium flows out of the heat transfer medium tube lumen at the heat transfer medium outlet. The outflowing heat transfer medium can be recycled.
  • the fluid mixture that flows out from the fluid outlet of the second reaction tube may contain unreacted fluid raw materials, fluid by-products, etc. in addition to the fluid product.
  • the fluid product obtained in the methanation reaction of carbon dioxide is methane
  • the fluid by-product is water.
  • the reaction tube 10 is inserted into the heat transfer medium tube lumen 13 so that the heat transfer medium in the heat transfer medium tube lumen is passed through the non-porous layer and/or the porous layer of the reaction tube to the fluid in the reaction tube lumen 3. heat can be exchanged between From the viewpoint of heat exchange efficiency, the first reaction tube preferably has a plate-like porous layer protruding inward from the inner surface of the reaction tube wall.
  • the second reaction tube preferably has a plate-like non-porous layer protruding inward from the inner surface of the reaction tube wall.
  • the reaction tube preferably has plate fins projecting outward from the outer surface of the reaction tube wall.
  • the temperature distribution in the flow direction of the reaction tube tends to be uneven. Hot spots can also occur in highly exothermic chemical reactions. It is desired to suppress the generation of hot spots and to uniform the temperature distribution in the flow direction of the reaction tube. Place the heat transfer medium inlet close to the part where hot spots may occur, or divide the heat transfer medium tube lumen with a partition plate and separate the heat transfer medium inlet and the heat transfer medium flow into each of the divided sections. An outlet may be provided to lower the temperature of each of the heat transfer medium flowing through the split heat transfer medium tube lumens closer to where hot spots may occur.
  • the temperature distribution in the flow direction of the reaction tube can be made uniform.
  • the plate fins may be provided only in a portion of the area where the catalyst is placed, which is closer to the fluid inlet, or provided only in a portion of the area where the catalyst is placed, which is closer to the fluid outlet. It may be provided over the entire area where the catalyst is placed.
  • the catalytic reactor or gas-phase catalytic reactor is not particularly limited by its manufacturing method.
  • it can be manufactured by preparing a reaction tube, a heat transfer medium tube, and accessories, respectively, and assembling them by welding, screwing, or the like.
  • the 3D data may be 3D shape data of the target part.
  • 3D shape data can be designed with 3D CAD.
  • the 3D data may be, for example, STL (Stereolithography) data obtained by converting 3D shape data.
  • STL data expresses a three-dimensional solid shape with an aggregate of small triangles (polygons).
  • Formation (modeling) of a three-dimensional object by lamination of cross-sectional shapes is performed by the powder bed fusion (PBF) method, metal deposition method, material extrusion deposition (FDM) method, liquid metal inkjet method, binder jet method, and laminate molding by PBF. It can be performed by a hybrid method of cutting. Among these, the powder bed fusion (PBF) method and the metal deposition method are preferred.
  • the powder bed fusion method is a method in which material powder is laid down and the part to be shaped is melted and solidified using a laser or electron beam as a heat source. It is shaped by spreading material powder and repeating melting and solidification. After the molding is finished, the unsolidified powder is removed and the molded object is taken out.
  • the powder bed fusion method includes the laser beam heat source method and the electron beam heat source method.
  • a laser beam is applied to the material powder that is laid out to melt, solidify, or sinter the material for additive manufacturing.
  • melting and solidification are usually performed in an inert atmosphere such as nitrogen.
  • positioning is performed by changing the angle of the mirror when irradiating the laser.
  • the powder bed/electron beam heat source method irradiates and collides an electron beam in a high vacuum with the powder bed and electron beam heat source method, which converts the kinetic energy into heat and melts the powder. Melt and solidify at The electron beam heat source method uses a lens with a magnetic field to change the direction of the electron beam. As a result, the electron beam heat source system is capable of high-speed positioning.
  • the metal deposition method is a method of forming by layering and solidifying molten metal materials in a predetermined location.
  • the metal deposition method does not require powder removal work after completion of modeling.
  • the metal deposition method includes the laser beam heat source method using metal powder as the material, and the arc discharge method using alloy wire as the material.
  • metal powder is injected from a nozzle and simultaneously irradiated with a laser beam to supply the metal powder to the molten pool and solidify to form a model.
  • Three-dimensional shapes are drawn by moving the melt nozzle or stage. Different metals can be shaped by switching the supply route of the metal powder.
  • the laser output is large, so it is suitable for high-speed molding.
  • the metal wire is melted by the arc discharge at the tip of the metal wire, and the metal wire is laminated to create a model.
  • Equipment and material costs are relatively low, and high-speed modeling is possible.
  • heat treatment can be performed for stress relaxation and strength improvement. Conditions such as temperature, time and atmosphere in the heat treatment can be appropriately set according to the metal material to be used.
  • the material powder spread is arranged so that the portion corresponding to the non-porous layer is irradiated more strongly than the portion corresponding to the porous layer.
  • a multilayer structure plate composed of an annular non-porous layer and an annular porous layer laminated inside thereof is repeatedly formed.
  • material powders metal powders; powders of inorganic compounds such as oxides, carbides, nitrides and borides can be used.
  • a catalytic reactor 30b of Embodiment 2 comprises at least one first reactor 20a and at least one second reactor 20b (eg, FIG. 14).
  • the catalytic reaction device 30b of Embodiment 2 includes a reactor 10 in which a reaction tube 10 consisting of a first reaction tube a and a second reaction tube b is inserted into one heat transfer medium tube.
  • the first reaction tube 10a is inserted through one first heat transfer medium tube
  • the second reaction tube 10b is inserted through the second heat transfer medium tube. It is substantially the same as the catalytic reaction device 30a of Embodiment 1, except for some differences.
  • the first reactor 20a comprises a first reaction tube 10a and a first heat transfer medium tube.
  • the first reaction tube 10a comprises a multilayer structure tube and a catalyst.
  • the multi-layer structure tube consists of a cylindrical non-porous layer and a cylindrical porous layer laminated inside thereof.
  • the multilayer structure tube has a fluid inlet, a fluid outlet, and a reaction tube lumen that communicates from the fluid inlet to the fluid outlet. Since the function, structure, etc. of the multilayer structure tube in the first reaction tube 10a are the same as those of the first reaction tube a, the description of the multilayer structure tube in the first reaction tube 20a is the same as that of the multilayer structure in the first reaction tube a. The description of the tube is read and used. The type and loading method of the catalyst in the first reaction tube 10a are the same as those of the catalyst in the first reaction tube a. is read and used.
  • first reaction tube 10a further has a plate-like porous layer 4 protruding from the inner surface of the cylindrical porous layer toward the inner cavity of the reaction tube (Fig. 5).
  • the shape of the plate-like porous layer is not particularly limited.
  • the plate-like porous layer 5 has a cross shape (Fig. 6).
  • the plate-like porous layer 6 has a spiral shape (FIG. 7). The plate-like porous layer contributes to controlling fluid flow, increasing the amount of catalyst supported, and increasing the contact area between the fluid and the porous layer.
  • first reaction tube 10a further has plate fins 11 protruding outward from the outer surface of the first reaction tube 10a.
  • the plate fins may be provided so that the plate surface is parallel to the longitudinal direction of the first reaction tube 20a, or may be provided so that the plate surface is spiral.
  • the plate surface may be provided so as to be non-parallel (for example, at right angles) to the longitudinal direction.
  • first reaction tube 10a Another aspect of the first reaction tube 10a is that the ends of plate fins protruding outward from the outer surface of the tube are connected to the outer surface of another adjacent reaction tube.
  • plate fins 11 are provided so that the plate surface is parallel to the longitudinal direction of the reaction tube, and the end of the plate fin 11 is connected to the outer surface of another adjacent reaction tube. .
  • This makes it possible to suppress the vibration of the first reaction tube 20a, control the flow of the heat transfer medium, promote the release of reaction heat, and the like.
  • the end of the plate fin protruding outward from the outer surface of the first reaction tube 10a is connected to the inner surface of the heat transfer medium tube.
  • the plate fins are preferably made of the same material as the reaction tube.
  • first heat transfer medium tube can be read as "first heat transfer medium tube” and used.
  • the fluid raw material flows into the reaction tube lumen at the fluid inlet of the first reaction tube 10a, and the fluid raw material is brought into contact with the catalyst in the reaction tube lumen to cause a chemical reaction.
  • the heat transfer medium flows into the heat transfer medium tube inner cavity at the heat transfer medium inlet of the first heat transfer medium tube, and the heat transfer medium flows out of the heat transfer medium tube inner cavity at the heat transfer medium outlet of the first heat transfer medium tube.
  • the first reaction tube is inserted through the heat transfer medium tube lumen of the first heat transfer medium tube, and the heat transfer medium in the heat transfer medium tube lumen flows through the reaction tube wall into the reaction tube lumen It has a mechanism that exchanges heat with what is inside.
  • the fluid inlet of the first reaction tube 10a is distinguished from the heat transfer medium inlet 16a or the heat transfer medium outlet 17a of the heat transfer medium tube, and the fluid raw materials react at the fluid inlet of the first reaction tube 10a. Flow into the lumen of the vessel.
  • the fluid inlet can be distinguished from the heat transfer medium inlet 16a or the heat transfer medium outlet 17a, for example, by a plate that holds the end of the first reaction tube on the fluid inlet side.
  • a device for preparing the fluid raw material for example, a mixing mechanism for mixing each component constituting the fluid raw material in a predetermined ratio, each component constituting the fluid raw material
  • a tank for storing the components, a compressor 31, a heat exchanger 32, etc. can be installed.
  • the raw material is liquid such as liquefied carbon dioxide
  • a vaporizer 34 or the like can be provided for safely vaporizing the raw material.
  • Components constituting the fluid raw material can be appropriately selected according to the chemical reaction to be performed in the reactor.
  • the fluid raw material used for the methanation reaction of carbon dioxide contains at least hydrogen gas and carbon dioxide gas.
  • the flow rate of the fluid raw material into the inner lumen of the reaction tube can be appropriately set according to the chemical reaction to be performed in the reactor.
  • the heat transfer medium flows into the heat transfer medium tube lumen of the first heat transfer medium tube at the heat transfer medium inlet.
  • the heat transfer medium is not particularly limited as long as it does not deteriorate in the temperature range for performing the desired chemical reaction and can maintain fluidity. Examples of the heat transfer medium include those described above.
  • the pressure of the heat transfer medium flowing through the heat transfer medium tube lumen and the pressure of the substance flowing through the reaction tube lumen 3 are not particularly limited. is preferably less than the compressive strength of the non-porous layer.
  • the heat transfer medium inlet and the heat transfer medium outlet are not particularly limited in their arrangement, but should be arranged so that the heat transfer medium can easily flow in a direction perpendicular to the longitudinal direction of the first reaction tube. is preferred.
  • Partition plates can be provided alternately from the left and right sides of the inner surface of the heat transfer medium tube to cause the flow of the heat transfer medium to meander.
  • a spiral partition plate can be provided along the inner surface of the heat transfer medium tube to swirl the flow of the heat transfer medium.
  • the partition plate may have a hole through which the reaction tube can pass so as to hold the intermediate portion of the reaction tube.
  • the fluid outlet of the first reaction tube 10a is distinguished from the heat transfer medium inlet 16a or the heat transfer medium outlet 17a, at which the fluid mixture a1 containing the fluid products flows out of the reaction tube lumen.
  • the fluid outlet can be distinguished from the heat transfer medium inlet or the heat transfer medium outlet, for example, by a plate that holds the end of the first reaction tube 10a on the fluid outlet side.
  • the heat transfer medium flows out of the heat transfer medium tube lumen at the heat transfer medium outlet. The outflowing heat transfer medium can be recycled.
  • the fluid mixture a1 flowing out from the fluid outlet of the first reaction tube 10a may contain unreacted fluid raw materials, fluid by-products, etc. in addition to fluid products.
  • the fluid product obtained in the methanation reaction of carbon dioxide is methane
  • the fluid by-product is water. Water may be condensed and removed from the system.
  • the first reaction tube 10a is inserted into the heat transfer medium tube lumen, and the heat transfer medium in the heat transfer medium tube lumen passes through the non-porous layer and/or the porous layer of the reaction tube to the fluid inside the reaction tube lumen. heat can be exchanged between From the viewpoint of heat exchange efficiency, the first reaction tube 10a preferably has a plate-like porous layer projecting inward from the inner surface of the reaction tube wall. Also, the first reaction tube 10a preferably has plate fins projecting outward from the outer surface of the reaction tube wall.
  • An outlet may be provided to lower the temperature of each of the heat transfer medium flowing through the split heat transfer medium tube lumens closer to where hot spots may occur.
  • the temperature distribution in the flow direction of the reaction tube can be made uniform.
  • the plate fins may be provided only in a portion of the area where the catalyst is placed, which is closer to the fluid inlet, or provided only in a portion of the area where the catalyst is placed, which is closer to the fluid outlet. It may be provided over the entire area where the catalyst is placed.
  • the second reactor 20b comprises a second reaction tube 10b and a second heat transfer medium tube.
  • the second reaction tube 10b comprises a single-layer structure tube and a catalyst.
  • the single-layer structure tube consists of a cylindrical non-porous layer, has a fluid inlet and a fluid outlet, and has a reaction tube lumen communicating from the fluid inlet to the fluid outlet. Since the function, structure, etc. of the single-layer structure tube in the second reaction tube 10b are the same as those of the second reaction tube b, the description of the single-layer structure tube in the second reaction tube 10b is The description of the single-layer structure pipe is read and used. The type and filling method of the catalyst in the second reaction tube 10b are the same as those of the catalyst in the second reaction tube b. Reread the explanation and use it.
  • Another embodiment of the second reaction tube 10b further has a plate-like non-porous layer that protrudes from the inner surface of the cylindrical non-porous layer toward the inner cavity of the reaction tube.
  • the shape of the plate-like non-porous layer is not particularly limited.
  • the plate-like non-porous layer has a cross shape.
  • Another aspect of the second reaction tube 10b is that the plate-like non-porous layer has a spiral shape.
  • the plate-like non-porous layer contributes to controlling fluid flow, increasing the amount of catalyst supported, and increasing the contact area between the fluid and the porous layer.
  • Another embodiment of the second reaction tube 10b further has plate fins 11 protruding outward from the outer surface of the second reaction tube 10b.
  • the plate fins may be provided so that the plate surface is parallel to the longitudinal direction of the second reaction tube 10b, or may be provided so that the plate surface is spiral.
  • the plate surface may be provided so as to be non-parallel (for example, at right angles) to the longitudinal direction.
  • Another aspect of the second reaction tube 10b is that the ends of plate fins protruding outward from the outer surface of the tube are connected to the outer surface of another adjacent reaction tube.
  • plate fins 11 are provided so that the plate surface is parallel to the longitudinal direction of the reaction tube, and the end of the plate fin 11 is connected to the outer surface of another adjacent reaction tube. .
  • This makes it possible to suppress the vibration of the second reaction tube 10b, control the flow of the heat transfer medium, promote the release of reaction heat, and the like.
  • the ends of the plate fins protruding outward from the outer surface of the second reaction tube 10b are connected to the inner surface of the heat transfer medium tube.
  • the plate fins are preferably made of the same material as the reaction tube.
  • the fluid mixture a1 flows into the reaction tube lumen at the fluid inlet of the second reaction tube, and the fluid mixture a1 is brought into contact with the catalyst in the reaction tube lumen to cause a chemical reaction.
  • a mechanism for the heat transfer medium to flow into the medium tube lumen and flow out of the heat transfer medium tube lumen at the heat transfer medium outlet of the second heat transfer medium tube, and the second reaction tube to the heat transfer medium tube.
  • a mechanism is inserted through the heat transfer medium tube lumen to exchange heat between the heat transfer medium in the heat transfer medium tube lumen and that in the reaction tube lumen through the reaction tube wall.
  • the fluid outlet of the first reactor 20a is connected to the fluid inlet of the second reactor 20b so that the respective reaction tube lumens communicate.
  • Gas-liquid separation may be performed by providing a condenser (heat exchanger 35a) or the like between the fluid outlet of the first reactor and the fluid inlet of the second reactor.
  • the method for obtaining a fluid product of the present invention comprises, in the catalytic reaction apparatus of Embodiment 1 of the present invention, supplying a fluid raw material into the reaction tube lumen at the fluid inlet of the first reaction tube; By supplying the medium to the heat transfer medium tube lumen at the heat transfer medium inlet, flowing it through the heat transfer medium tube lumen, and discharging the medium from the heat transfer medium tube lumen at the heat transfer medium outlet, performing a chemical reaction while controlling the temperature; and discharging a fluid mixture containing a fluid product obtained by the chemical reaction from the inner lumen of the reaction tube at the fluid outlet of the second reaction tube.
  • the method for obtaining a fluid product of the present invention comprises, in the catalytic reaction apparatus of Embodiment 2 of the present invention, supplying a fluid raw material into the reaction tube lumen at the fluid inlet of the first reaction tube; A medium is supplied to the heat transfer medium tube lumen at the heat transfer medium inlet of the first heat transfer medium tube, flows into the heat transfer medium tube lumen, and flows from the heat transfer medium tube lumen to the first heat transfer medium tube.
  • a chemical reaction is performed while controlling the temperature of the substance inside the reaction tube lumen, and the fluid product obtained by the chemical reaction is discharged from the reaction tube lumen at the fluid outlet of the first reaction tube.
  • a gas containing CO 2 (carbon dioxide) and H 2 (hydrogen) is used as a fluid raw material, and CO 2 is reduced.
  • the amount of gas containing CO 2 and H 2 to be introduced can be appropriately set according to the reaction rate, the capacity of the reaction tube lumen, and the like.
  • the reduction reaction of CO2 proceeds as follows. CO2 +H2 ⁇ CO + H2O CO2 + 3H2 -> CH3OH + H2O CO2 + 4H2 -> CH4 + 2H2O
  • the catalytic reactor and the method for obtaining fluid products of the present invention are other than the method of producing CO (carbon monoxide), methanol or methane from a gas containing CO 2 (carbon dioxide) and H 2 (hydrogen). It can also be preferably used for the C1 chemical synthesis method and the like.
  • C1 chemical synthesis methods include a method of producing carbon monoxide and hydrogen by reacting methane and water (steam), a method of producing carbon monoxide and hydrogen by reacting methane and carbon dioxide, and a method of producing carbon monoxide and hydrogen by reacting methane and carbon dioxide.
  • a method for producing carbon dioxide and hydrogen by reacting carbon and water a method for producing carbon dioxide and hydrogen by reacting methane and water, and a method for producing methane and carbon dioxide by reacting carbon monoxide and hydrogen a method for producing methanol by reacting carbon monoxide and hydrogen; a method for producing acetone and water by reacting carbon monoxide and hydrogen; a method for producing acetone and water by reacting carbon monoxide and hydrogen; , or a method for producing methanol.
  • products CO (carbon monoxide), methanol or methane
  • unreacted substances mainly CO 2
  • separation and purification methods include a membrane separation method, an adsorption separation method, an absorption separation method, a distillation separation method, a cryogenic separation method, and the like.
  • the membrane separation method is preferable from the viewpoint of separation selectivity, separation speed, and inexpensive and compact equipment.
  • Unreacted substances (mainly CO 2 ) and low-concentration methane obtained in the separation and purification of methane can be used as fluid raw materials in the above-described method for producing methane.
  • carbon monoxide is toxic to the human body, it is preferable to treat it so that the concentration of carbon monoxide is 30 ppm or less.
  • Methods for reducing the concentration of carbon monoxide include, for example, converting carbon monoxide into methane by a CO methanation reaction, converting carbon monoxide into carbon dioxide by a CO selective oxidation reaction, and using an adsorbent or absorbent to convert carbon monoxide into carbon dioxide. can be exemplified by adsorbing or absorbing the
  • methane obtained by separation and refinement can be supplied to gas turbines as fuel. Electric power can be generated by this gas turbine. Since flue gas from gas turbines usually contains carbon dioxide, it can be used as a fluid feedstock in the methane production process described above.
  • the present invention can be used in various chemical reactions.
  • the present invention utilizes hydrogen produced by electrolysis of water, etc., utilizes carbon dioxide produced by breathing of humans and animals or by burning fuel, produces water, or produces methane as fuel. Useful.
  • the invention can also be used in space stations, spacecraft, rockets, and the like.
  • Example 1 324 multi-layered tubes with a length of 300 mm, an outer diameter of 3.9 mm, and an inner diameter of 3.0 mm were prepared, which consisted of a metal cylindrical non-porous layer and a metal cylindrical porous layer laminated inside it. .
  • a CO 2 methanation catalyst (particle size range: 3-6 mm, METH135, manufactured by Clariant) was pulverized to obtain a catalyst powder.
  • a catalyst slurry was obtained by mixing 30 parts by mass of catalyst powder, 20 parts by mass of silica sol (trade name Snowtex N, manufactured by Nissan Chemical Industries) and 50 parts by mass of water.
  • the multi-layer structure tube was immersed in the catalyst slurry, removed from the slurry, wiped off the catalyst slurry adhering to the outer surface of the tube, and dried at 150° C. for 1 hour. This was repeated to support 300 g/m 2 (0.85 g per reaction tube) of a methanation catalyst on the porous layer to obtain a first reaction tube a.
  • 324 first reaction tubes a were inserted into the inner cavity of a circular tube (first heat transfer medium tube) made of SUS316 having a length of 300 mm, an outer diameter of 114.3 mm and a thickness of 2.1 mm. Between the adjacent first reaction tubes a, plate fins are installed, the two are connected and arranged parallel to the longitudinal direction of the heat transfer medium tubes as shown in FIG.
  • the holding plates 25 and 26 were sealed with end plates each having a first reactor fluid inlet 9a and a first reactor fluid outlet 9b.
  • a heat transfer medium inlet 16a and a heat transfer medium outlet 17b are provided on the side surface of the heat transfer medium tube.
  • Thermocouples were installed on the porous layer at predetermined intervals.
  • a CO 2 methanation catalyst (particle size range 3-6 mm, METH135, manufactured by Clariant) was pulverized with a hammer mill and classified to obtain a granular catalyst with a particle size range of 1-2 mm.
  • the above-mentioned granular catalyst and granular alumina with a particle size range of 1 to 2 mm were uniformly mixed at a volume ratio of 1:1 in the lumen of a circular tube (single-layer structure tube) made of SUS316 with an inner diameter of 3 mm and a length of 300 mm.
  • a second reaction tube was obtained.
  • the amount of CO 2 methanation catalyst in the second reaction tube was 0.85 g per reaction tube.
  • 324 second reaction tubes were inserted into the inner cavity of a SUS316 circular tube (second heat transfer medium tube) having a length of 300 mm, an outer diameter of 114.3 mm and a thickness of 2.1 mm.
  • a plate fin was installed between the adjacent second reaction tubes, the two were connected, arranged parallel to the longitudinal direction of the heat transfer medium tube as shown in FIG. 10, and fixed with a holding plate.
  • Each portion of the retainer plate was sealed with a head plate, each having a second reactor fluid inlet and a second reactor fluid outlet.
  • a heat transfer medium inlet 16b and a heat transfer medium outlet 17b are provided on the side surface of the heat transfer medium tube.
  • a thermocouple was placed in the lumen of the second reaction tube.
  • a reactor was assembled by connecting the fluid outlet 9b of the first reactor and the fluid inlet of the second reactor with a connecting pipe.
  • a heat transfer medium (trade name: Barreltherm 400, boiling point: 390°C) is supplied from the heat transfer medium inlet 16a to the heat transfer medium pipe lumen at a pressure of less than 0.1 MPa, and the heat transfer medium outlet 17b is supplied from the heat transfer medium pipe lumen. and the temperature at the fluid inlet 10a of the first reaction tube was adjusted to 330°C. The supply flow rate of the heat transfer medium was 50 L/min on average.
  • a heat transfer medium (trade name: Barreltherm 400, boiling point: 390°C) is supplied from the heat transfer medium inlet 16b into the heat transfer medium pipe lumen at a pressure of less than 0.1 MPa, and the heat transfer medium outlet 17b is supplied from the heat transfer medium pipe lumen. and the temperature at the fluid inlet of the second reaction tube was adjusted to 330°C.
  • the supply flow rate of the heat transfer medium was 50 L/min on average.
  • Hydrogen gas was supplied from the fluid inlet 9a of the first reactor to the first reaction tube and the second reaction tube at normal pressure and 0.1 Nm 3 /h for 6 hours. A reduction treatment of the CO 2 methanation catalyst in the tube was performed.
  • a fluid raw material of 20 parts by volume of carbon dioxide and 80 parts by volume of hydrogen was supplied at 5.0 Nm 3 /h from the fluid inlet 9a of the first reactor through the fluid inlet of the first reaction tube and into the reaction tube lumen 3. supplied to The fluid mixture a1 is discharged from the fluid outlet 9b of the first reactor through the fluid outlet of the first reaction tube, and is passed through the connecting tube from the fluid inlet of the second reactor to the fluid inlet of the second reaction tube. and fed into the reaction tube lumen. The fluid mixture a2 was discharged from the fluid outlet of the second reactor through the fluid outlet of the second reaction tube. The internal pressure in the first reaction tube and the second reaction tube was adjusted to 0.5 MPaG.
  • Fluid mixture a1 and fluid mixture a2 were analyzed respectively.
  • the methanation reaction rate of carbon dioxide was 82%.
  • the maximum temperature of the porous layer of the first reaction tube was 333°C.
  • the temperature difference in the longitudinal direction of the first reaction tube was within 3°C.
  • the maximum temperature of the catalyst-filled portion of the second reaction tube was 340°C.
  • the temperature difference in the longitudinal direction of the second reaction tube was within 10°C.
  • Example 2 The above-mentioned granular catalyst and granular alumina having a particle size of 1 to 2 mm were uniformly mixed at a volume ratio of 1:1 in the lumen of a circular tube (single-layer structure tube) made of SUS316 with an inner diameter of 8 mm and a length of 300 mm. After filling, a second reaction tube was obtained. The amount of CO 2 methanation catalyst in the second reactor tube was 6.05 g per reactor tube. Forty-six second reaction tubes were inserted through the inner cavity of a SUS316 circular tube (second heat transfer medium tube) having a length of 300 mm, an outer diameter of 114.3 mm and a thickness of 2.1 mm.
  • SUS316 circular tube second heat transfer medium tube
  • thermocouple was placed in the lumen of the second reaction tube.
  • a reactor was assembled by connecting the fluid outlet port 9b of the first reactor used in Example 1 and the fluid inlet port of the second reactor with a connecting pipe.
  • a heat transfer medium (trade name: Barreltherm 400, boiling point: 390°C) is supplied from the heat transfer medium inlet 16a to the heat transfer medium pipe lumen at a pressure of less than 0.1 MPa, and the heat transfer medium outlet 17b is supplied from the heat transfer medium pipe lumen. and the temperature at the fluid inlet 10a of the first reaction tube was adjusted to 330°C. The supply flow rate of the heat transfer medium was 50 L/min on average.
  • a heat transfer medium (trade name: Barreltherm 400, boiling point: 390°C) is supplied from the heat transfer medium inlet 16b into the heat transfer medium pipe lumen at a pressure of less than 0.1 MPa, and the heat transfer medium outlet 17b is supplied from the heat transfer medium pipe lumen. and the temperature at the fluid inlet of the second reaction tube was adjusted to 330°C.
  • the supply flow rate of the heat transfer medium was 50 L/min on average.
  • Example 2 Using this reactor, the reduction treatment and the methanation reaction of carbon dioxide were performed in the same manner as in Example 1.
  • the methanation reaction rate of carbon dioxide was 82%.
  • the maximum temperature of the porous layer of the first reaction tube was 333°C.
  • the temperature difference in the longitudinal direction of the first reaction tube was within 3°C.
  • the maximum temperature of the catalyst-filled portion of the second reaction tube was 348°C.
  • the temperature difference in the longitudinal direction of the second reaction tube was within 15°C.
  • Comparative example 1 A granular CO 2 methanation catalyst with a particle size of 1 to 2 mm and granular alumina with a particle size of 1 to 2 mm were placed in the lumen of a circular tube (single-layer structure tube) made of SUS316 with an inner diameter of 3 mm and a length of 300 mm at a volume ratio of 1:1. The uniform mixture obtained in 1 was filled to obtain a catalyst-filled reaction tube. Reduction treatment and methanation of carbon dioxide were performed in the same manner as in Example 1, except that the 324 first reaction tubes installed in the first reactor used in Example 1 were replaced with 324 catalyst-filled reaction tubes. reacted. The methanation reaction rate of carbon dioxide was 80%. The maximum temperature of the catalyst packed portion of the reaction tube installed in the first reactor was 380°C. The temperature difference in the longitudinal direction of the reaction tube was within 50°C.
  • Comparative example 2 A granular CO2 methanation catalyst with a particle size of 1 to 2 mm and granular alumina with a particle size of 1 to 2 mm were placed in the lumen of a circular tube (single-layer structure tube) made of SUS316 with an inner diameter of 8 mm and a length of 300 mm, at a volume ratio of 1:1. to obtain a catalyst-filled reaction tube.
  • Reduction treatment and methanization of carbon dioxide were performed in the same manner as in Example 1, except that the 324 first reaction tubes installed in the first reactor used in Example 1 were replaced with 46 catalyst-filled reaction tubes. reacted.
  • the methanation reaction rate of carbon dioxide was 80%.
  • the maximum temperature of the catalyst packed portion of the reaction tube installed in the first reactor was 400°C.
  • the temperature difference in the longitudinal direction of the reaction tube was within 70°C.
  • Example 3 A multi-layer structure tube having a length of 300 mm, an outer diameter of 3.9 mm and an inner diameter of 3.0 mm, comprising a metal cylindrical non-porous layer and a metal cylindrical porous layer laminated inside thereof, and an inner diameter of 3 mm and A circular tube (single-layer structure tube) made of SUS316 having a length of 300 mm was connected with a socket (pipe joint) to obtain one reaction tube as shown in FIG. The CO 2 methanation catalyst was supported and packed in the same manner as in Example 1. 324 of them were prepared.
  • a reaction tube 324 was placed in the inner cavity of a circular tube (first heat transfer medium tube) made of SUS316 having a length of 650 mm, an outer diameter of 114.3 mm and a thickness of 2.1 mm so that the multilayer structure tube was on the fluid inlet side.
  • a book was inserted, and a reactor was obtained and a reactor was assembled in the same manner as the method for assembling the first reactor in Example 1.
  • Reduction treatment and methanation reaction were carried out in the same manner as in Example 1 using this reactor.
  • the methanation reaction rate of carbon dioxide was 80%.
  • the maximum temperature in the reaction tube was 339°C.
  • the temperature difference in the longitudinal direction of the reaction tube was within 9°C.
  • the present invention can be provided with various chemical engineering devices such as instrumentation, pipes, tanks, towers, etc., as long as they have the features described above.
  • various chemical engineering devices such as instrumentation, pipes, tanks, towers, etc., as long as they have the features described above.
  • those skilled in the art will understand that changes, replacements, additions, and omissions are included in the scope of the present invention as long as they do not depart from the gist of the present invention.

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Abstract

Selon l'invention, un tube de réaction comprend au moins un premier tube de réaction et au moins un second tube de réaction. Le premier tube de réaction comprend : un tube à structure multicouche qui est formé à partir d'une couche non poreuse cylindrique et d'une couche poreuse cylindrique empilée sur le côté interne de la couche non poreuse, comprend une entrée de fluide et une sortie de fluide, et comprend une cavité interne de tube de réaction reliant l'entrée de fluide à la sortie de fluide ; et un catalyseur supporté par la couche poreuse. Le second tube de réaction comprend : un tube à structure monocouche qui est formé à partir d'une couche non poreuse cylindrique, comprend une entrée de fluide et une sortie de fluide, et comprend une cavité interne de tube de réaction reliant l'entrée de fluide à la sortie de fluide ; et un catalyseur remplissant la cavité interne du tube de réaction du tube à structure monocouche. La sortie de fluide du premier tube de réaction est reliée à l'entrée de fluide du second tube de réaction de sorte que les cavités internes de tube de réaction du premier tube de réaction et du second tube de réaction communiquent l'une avec l'autre.
PCT/JP2022/027552 2021-07-13 2022-07-13 Dispositif de réaction isotherme WO2023286803A1 (fr)

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JPS4215682B1 (fr) * 1960-12-23 1967-08-29
JPS59222428A (ja) * 1983-05-31 1984-12-14 Kobe Steel Ltd 高効率メタン化装置
JPS6456133A (en) * 1987-08-27 1989-03-03 Kobe Steel Ltd Pipe wall catalyst reaction device
JPH04187501A (ja) * 1990-11-21 1992-07-06 Mitsubishi Heavy Ind Ltd メタノール改質方法及び装置
JPH05186203A (ja) * 1992-01-07 1993-07-27 Toshiba Corp 水蒸気改質用触媒エレメント
JP2001137689A (ja) * 1999-08-31 2001-05-22 Nippon Shokubai Co Ltd 接触気相酸化反応器
JP2005518265A (ja) * 2001-08-02 2005-06-23 ビーピー・コーポレーション・ノース・アメリカ・インコーポレーテッド 不均質触媒を有する化学変換用フローリアクター
US20080131361A1 (en) * 2006-12-05 2008-06-05 Diwakar Garg Process and apparatus for the production of hydrogen gas
US20100162626A1 (en) * 2008-12-31 2010-07-01 Clomburg Jr Lloyd Anthony Adiabatic reactor and a process and a system for producing a methane-rich gas in such adiabatic reactor
WO2018140349A1 (fr) * 2017-01-24 2018-08-02 Basf Corporation Catalyseurs monolithiques pour époxydation
JP2020093216A (ja) * 2018-12-12 2020-06-18 株式会社Ihi 触媒反応装置
JP2021154194A (ja) * 2020-03-25 2021-10-07 三菱パワー株式会社 ガス状生成物を得るための装置およびガス状生成物を得るための方法
JP2022095370A (ja) * 2020-12-16 2022-06-28 三菱重工業株式会社 触媒反応装置

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