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WO2023234008A1 - Système d'alimentation en agent réducteur, procédé d'alimentation en agent réducteur et système de réaction en boucle chimique - Google Patents

Système d'alimentation en agent réducteur, procédé d'alimentation en agent réducteur et système de réaction en boucle chimique Download PDF

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Publication number
WO2023234008A1
WO2023234008A1 PCT/JP2023/018252 JP2023018252W WO2023234008A1 WO 2023234008 A1 WO2023234008 A1 WO 2023234008A1 JP 2023018252 W JP2023018252 W JP 2023018252W WO 2023234008 A1 WO2023234008 A1 WO 2023234008A1
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WO
WIPO (PCT)
Prior art keywords
reducing agent
tower
metal particles
tank
supply system
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/JP2023/018252
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English (en)
Japanese (ja)
Inventor
博嗣 熊澤
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Tokyo Ohka Kogyo Co Ltd
Original Assignee
Tokyo Ohka Kogyo Co Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Tokyo Ohka Kogyo Co Ltd filed Critical Tokyo Ohka Kogyo Co Ltd
Priority to JP2024524314A priority Critical patent/JPWO2023234008A1/ja
Priority to CN202380034783.2A priority patent/CN119032244A/zh
Priority to KR1020247035160A priority patent/KR20250020392A/ko
Publication of WO2023234008A1 publication Critical patent/WO2023234008A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24V—COLLECTION, PRODUCTION OR USE OF HEAT NOT OTHERWISE PROVIDED FOR
    • F24V30/00—Apparatus or devices using heat produced by exothermal chemical reactions other than combustion
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
    • 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
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08J—WORKING-UP; GENERAL PROCESSES OF COMPOUNDING; AFTER-TREATMENT NOT COVERED BY SUBCLASSES C08B, C08C, C08F, C08G or C08H
    • C08J11/00—Recovery or working-up of waste materials
    • C08J11/02—Recovery or working-up of waste materials of solvents, plasticisers or unreacted monomers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K5/00—Feeding or distributing other fuel to combustion apparatus
    • F23K5/02—Liquid fuel
    • F23K5/06—Liquid fuel from a central source to a plurality of burners
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23N—REGULATING OR CONTROLLING COMBUSTION
    • F23N1/00—Regulating fuel supply

Definitions

  • the present invention relates to a reducing agent supply system, a reducing agent supply method, and a chemical loop reaction system.
  • an oxidation tower that oxidizes metal particles into metal oxide particles
  • a reduction tower that generates carbon dioxide by reacting the metal oxide particles with a reducing agent and turn the metal oxide particles into metal particles
  • a reduction tower that oxidizes metal particles and metal oxide particles.
  • a chemical loop reaction system is known that includes a circulation section that circulates particles between a reduction tower and an oxidation tower (see, for example, Patent Document 1).
  • a reducing agent is supplied to a reduction tower.
  • the reducing agent for example, organic solvent waste generated in the process of manufacturing semiconductor elements, liquid crystal display elements, etc. is used.
  • This waste liquid may contain, for example, powdered or granular resin components as a solid content.
  • solid resin components and the like may settle in the lower part of the container and coagulate. Therefore, when waste liquid is sent from a storage container to a reduction tower, if a large amount of solid content is contained in the waste liquid, it may cause malfunction of the pump, clogging of piping, etc., and the waste liquid cannot be sent properly to the reduction tower.
  • There are issues such as:
  • the present invention provides a reducing agent supply system, a reducing agent supply method, and a chemical loop reaction system that can appropriately supply a reducing agent to a reduction tower even if the reducing agent contains powdered or granular solid content.
  • the purpose is to provide.
  • a reducing agent supply system includes an oxidation tower that oxidizes metal particles into oxidized metal particles, a reduction tower that reduces the oxidized metal particles into metal particles, and a reduction tower that reduces metal particles and oxidized metal particles.
  • a system for supplying a reducing agent for reducing oxidized metal particles to a reducing column of a chemical loop reaction system comprising: a circulation section for circulating between a column and an oxidation column, the reducing agent tank storing the reducing agent; , a sedimentation prevention mechanism that prevents settling of solid content contained in the reducing agent in the reducing agent tank, and a reducing agent supply line that connects the reducing agent tank and the reducing tower.
  • a reducing agent supply method includes an oxidation tower that oxidizes metal particles into oxidized metal particles, a reduction tower that reduces the oxidized metal particles into metal particles, and a reduction tower that reduces metal particles and oxidized metal particles.
  • a method for supplying a reducing agent for reducing oxidized metal particles to a reducing column of a chemical loop reaction system comprising: a circulation section for circulating between a column and an oxidizing column; the reducing agent is stored in a reducing agent tank; stirring the reducing agent in the reducing agent tank; and supplying the reducing agent from the reducing agent tank to the reduction tower.
  • a chemical loop reaction system includes an oxidation tower that oxidizes metal particles to form oxidized metal particles, a reduction tower that reduces the oxidized metal particles to form metal particles, and a reduction tower that reduces metal particles and oxidized metal particles.
  • a chemical loop reaction system comprising a circulation section for circulating between a tower and an oxidation tower, and comprising the reducing agent supply system of the above embodiment.
  • the settling prevention mechanism in the reducing agent tank prevents the solids from settling and coagulating at the bottom of the reducing agent tank. can be prevented. Therefore, when the reducing agent is sent from the reducing agent tank to the reducing tower, it is possible to prevent the solid content from causing malfunction of the pump, clogging of pipes, etc., and to appropriately supply the reducing agent to the reducing tower. As a result, the reducing agent is appropriately supplied to the reduction tower of the chemical loop reaction system, so that the chemical loop reaction system can be stably operated.
  • FIG. 1 is a diagram showing an example of a reducing agent supply system and a chemical loop reaction system according to the first embodiment. It is a diagram showing an example of an oxidation tower and a reduction tower.
  • FIG. 2 is an enlarged view of the main parts of the reducing agent supply system. It is a flow chart showing an example of a reducing agent supply method concerning a 1st embodiment.
  • 5 is a flowchart following FIG. 4 showing an example of a reducing agent supply method. 6 is a flowchart showing a part of the flowchart of FIG. 5 in detail.
  • FIG. 3 is an enlarged view of main parts of a reducing agent supply system according to a first modification.
  • FIG. 3 is an enlarged view of main parts of a reducing agent supply system according to a first modification.
  • FIG. 7 is an enlarged view of main parts of a reducing agent supply system according to a second modification.
  • FIG. 7 is an enlarged view of main parts of a reducing agent supply system according to a 32nd modification.
  • FIG. 7 is an enlarged view of main parts of a reducing agent supply system according to a fourth modification. It is a figure showing an example of a reducing agent supply system and a chemical loop reaction system concerning a 2nd embodiment. It is a flow chart which shows an example of a reducing agent supply method concerning a 2nd embodiment. It is a figure showing an example of a reducing agent supply system and a chemical loop reaction system concerning a 3rd embodiment. It is a flow chart which shows an example of a reducing agent supply method concerning a 3rd embodiment. It is a figure showing an example of a reducing agent supply system and a chemical loop reaction system concerning a 4th embodiment.
  • FIG. 7 is an enlarged view of main parts of a reducing agent supply system according to a fifth modification.
  • the chemical loop reaction system 100 includes an oxidation tower 10, a reduction tower 20, a fluidizing gas supply line 16 (nitrogen supply line 18), an air supply line 19, and a reducing agent supply line. 21, a circulation section 60, and a control section C, and further includes a reducing agent supply system 200.
  • the oxidation tower 10 oxidizes the metal particles M into oxidized metal particles MO.
  • the oxidation tower 10 is a cylindrical outer tower made of a heat-resistant material such as a steel plate.
  • the upper end of the oxidation tower 10 is closed with a top plate 10A.
  • the oxidation tower 10 includes an upper part 11, a central part 12, a lower part 13, and an exhaust part 14.
  • the upper part 11 has a cylindrical upper part 11A that extends in the vertical direction, and a reduced diameter part 11B that reduces in diameter downward from the lower end of the upper part 11A.
  • the central portion 12 is connected to the lower end of the reduced diameter portion 11B and has a cylindrical shape extending downward.
  • the lower part 13 has an enlarged diameter part 13A that is connected to the lower end of the central part 12 and whose diameter increases downward, and a cylindrical lower part 13B that extends downward from the lower end of the enlarged diameter part 13A.
  • the lower end of the lower part 13 is closed by a first bottom plate 13C. Note that the diameter of the central portion 12 is smaller than the diameter of the lower portion 13B of the lower portion 13 and the diameter of the upper portion 11A of the upper portion 11. Further, the diameter of the lower part 13B of the lower part 13 is smaller than the diameter of the upper part 11A of the upper part 11.
  • the air supply pipe 43 connects an air chamber 91 and an air nozzle 42, which will be described later, and sends air from the air chamber 91 to the air nozzle 42.
  • a configuration may be provided that includes a height adjustment mechanism that can change the height of the air nozzle 42 by adjusting the length of the air supply pipe 43.
  • the fluidizing gas nozzle 44 spouts fluidizing gas upward and supplies the fluidizing gas to the oxidation tower 10.
  • the fluidizing gas include nitrogen and the like.
  • the fluidizing gas nozzle 44 is arranged below the lower end of the reduction tower 20. With this configuration, by jetting out the fluidizing gas from the fluidizing gas nozzle 44, the fluidizing gas can be supplied to the oxidizing tower 10, and the metal particles M and the metal oxide particles MO can be made to flow in the oxidizing tower 10.
  • the fluidizing gas supply pipe 45 is provided to penetrate the first bottom plate 13C, and holds the fluidizing gas nozzle 44 at its upper end.
  • the fluidizing gas supply pipe 45 is set to a length that allows the fluidizing gas nozzle 44 to be disposed below the lower end of the reduction tower 20 .
  • the fluidizing gas supply pipe 45 connects a fluidizing gas chamber 92 and a fluidizing gas nozzle 44, which will be described later, and sends the fluidizing gas in the fluidizing gas chamber 92 to the fluidizing gas nozzle 44.
  • a configuration may be provided that includes a height adjustment mechanism that can change the height of the fluidizing gas nozzle 44 by adjusting the length of the fluidizing gas supply pipe 45.
  • An air chamber 91 and a fluidizing gas chamber 92 are provided below the lower part 13 of the oxidation tower 10.
  • a cylindrical portion 90 is provided whose upper end is closed by the first bottom plate 13C and whose lower end is closed by the second bottom plate 90A.
  • An air chamber 91 and a fluidizing gas chamber 92 are formed by partitioning the inside of this cylindrical portion 90 with a partition plate 93.
  • the cylindrical part 90 is provided with the same inner diameter as the lower part 13.
  • the air chamber 91 communicates with the lower part 13 via the air supply pipe 43 and the air nozzle 42.
  • the fluidizing gas chamber 92 communicates with the lower part 13 via the fluidizing gas supply pipe 45 and the fluidizing gas nozzle 44 .
  • the air chamber 91 includes an air introduction section 46.
  • the air introduction part 46 is provided to penetrate the second bottom plate 90A, and is connected to the air supply line 19.
  • the air chamber 91 stores air sent through the air supply line 19 and the air introduction section 46.
  • the air chamber 91 is pressurized by air sent from the air supply line 19. By increasing the pressure in the air chamber 91, the air in the air chamber 91 is ejected from the air nozzle 42 into the oxidation tower 10 via the air supply pipe 43.
  • the air blown into the oxidation tower 10 functions as an oxidizing agent in the oxidation tower 10.
  • the fluidizing gas chamber 92 includes a fluidizing gas introduction section 47.
  • the fluidizing gas introduction section 47 is provided to penetrate the second bottom plate 90A, and is connected to the fluidizing gas supply line 16.
  • the fluidizing gas chamber 92 stores the fluidizing gas sent through the fluidizing gas supply line 16 and the fluidizing gas introduction section 47.
  • the fluidizing gas chamber 92 is pressurized by the fluidizing gas sent from the fluidizing gas supply line 16 .
  • the fluidizing gas in the fluidizing gas chamber 92 is ejected from the fluidizing gas nozzle 44 into the oxidation tower 10 via the fluidizing gas supply pipe 45.
  • the fluidized gas ejected into the oxidation tower 10 fluidizes the metal oxide particles MO present within the oxidation tower 10. Further, a part of the fluidized gas ejected into the oxidation tower 10 enters the reduction tower 20 and fluidizes the metal particles M or the metal oxide particles MO in the reduction tower 20.
  • the exhaust part 14 is provided at the upper end of the oxidation tower 10, passing through a fixing part 10B provided on the top plate 10A.
  • the gas in the oxidation tower 10 is discharged from the oxidation tower 10 via the exhaust section 14.
  • a solid-gas separation section 15 is provided in the exhaust section 14 .
  • the solid-gas separation section 15 separates solid components contained in the gas discharged from the exhaust section 14 from gas.
  • a filter, a cyclone device, etc. are used, for example.
  • the gas discharged from the exhaust section 14 is mainly composed of nitrogen and contains a small amount of oxygen, as will be described later. After solid components are removed from the gas discharged from the exhaust section 14 in the solid-gas separation section 15, it is released into the atmosphere or reused as a fluidizing gas.
  • the reduction tower 20 is arranged inside the oxidation tower 10.
  • the reduction tower 20 is a cylindrical inner tower made of a heat-resistant material such as a steel plate and has an outer diameter smaller than the inner diameter of the oxidation tower 10.
  • the reduction tower 20 converts the metal oxide particles MO into metal particles M while reacting the metal oxide particles MO with a reducing agent R to generate carbon dioxide.
  • the reduction tower 20 is located inside the oxidation tower 10 of the oxidation tower 10, and is arranged with its vertical central axes aligned.
  • the reduction tower 20 is formed to have a length spanning the upper part 11, the central part 12, and the lower part 13 of the oxidation tower 10 in the vertical direction.
  • one reduction tower 20 is disposed within the oxidation tower 10, but the present invention is not limited to this, and a plurality of reduction towers 20 may be disposed within the oxidation tower 10.
  • the reduction tower 20 includes a fuel nozzle 40, a fuel supply pipe 41, and a solid-gas separator 50.
  • the fuel nozzle 40 is located at a position slightly above the lower end of the reduction tower 20. It is arranged in a state where it is inserted into the reduction tower 20.
  • the fuel nozzle 40 spouts fuel (reducing agent R), water vapor, and carrier gas upward. This configuration suppresses fuel and the like ejected from the fuel nozzle 40 from being supplied to the outside of the reduction tower 20. Note that the fuel (reducing agent R), water vapor, and carrier gas will be described later.
  • the outer diameter of the fuel nozzle 40 is smaller than the inner diameter of the reduction tower 20, and a gap is formed between the fuel nozzle 40 and the reduction tower 20 through which the metal oxide particles MO can pass.
  • the fuel supply pipe 41 holds the fuel nozzle 40 at its upper part.
  • the fuel supply pipe 41 is provided to penetrate the first bottom plate 13C, the fluidizing gas chamber 92, and the second bottom plate 90A, and is connected to the reducing agent supply line 21 at the lower part.
  • the length of the fuel supply pipe 41 is set to a difference that allows the fuel nozzle 40 to be inserted into the reduction tower 20 .
  • the fuel nozzle 40 may be provided with a height adjustment mechanism that can change the height of the fuel nozzle 40 by adjusting the length of the fuel supply pipe 41.
  • Fuel (reducing agent R) and the like are ejected from the reducing agent supply line 21 into the reduction tower 20 from the fuel nozzle 40 via the fuel supply pipe 41.
  • the fuel nozzle 40 spouts fuel (reducing agent R) and the like upward.
  • an upward flow is formed in the reduction tower 20, and the metal oxide particles MO are taken in from the opening at the lower end of the reduction tower 20 and made to rise.
  • a gap is formed between the fuel nozzle 40 and the reduction tower 20, and the metal oxide particles MO ascend through the gap in the reduction tower 20, and while ascending inside the reduction tower 20.
  • the metal particles M are reduced by the fuel (reducing agent R) ejected from the fuel nozzle 40.
  • the solid-gas separator 50 is connected to the reduction tower 20 via a connecting pipe 53 provided at the top.
  • the solid-gas separator 50 is connected to a protection tube 51 provided outside the reduction tower 20 and is provided in parallel to the reduction tower 20 .
  • the solid-gas separator 50 uses, for example, a cyclone that separates solid components and gas components by generating a swirling flow inside.
  • the solid components are metal particles M and oxidized metal particles MO that have not been reduced in the reduction tower 20.
  • the solid-gas separator 50 returns the separated solid components to the oxidation tower 10.
  • An exhaust pipe 54 is provided at the top of the solid-gas separator 50.
  • the separated gas components are exhausted from the exhaust pipe 54.
  • the gas component is primarily carbon dioxide and may contain water vapor.
  • the exhaust pipe 54 is connected to an exhaust section 57.
  • the exhaust part 57 is provided to penetrate the fixed part 10B provided on the top plate 10A.
  • the exhaust section 57 is provided with a gas-liquid separator 58 (see FIG. 1).
  • the gas-liquid separator 58 separates liquid components (for example, water vapor) contained in the gas components discharged from the exhaust section 57.
  • the solid-gas separator 50 generates a swirling flow in the cylindrical body portion 52 by guiding the flow discharged upward from the connecting pipe 53 through the introduction portion 56.
  • the swirling flow continues to swirl while moving downward in the body portion 52 .
  • the solid component moves downward while swirling near the inner wall of the body 52 and is discharged into the oxidation tower 10 through an opening 55 whose diameter is reduced in the lower part of the body 52.
  • the gas component flows upward in the central portion of the swirling flow and is exhausted by the exhaust section 57 via the exhaust pipe 54. That is, the solid-gas separator 50 returns metal particles M and the like to the oxidation tower 10 from the flow of the solid-gas mixture discharged from the reduction tower 20, and discharges carbon dioxide.
  • the oxidation tower 10 and the reduction tower 20 are installed on the floor F via the support part 94, as shown in FIG.
  • a load cell 95 is arranged between the support part 94 and the floor surface F.
  • the output of the load cell 95 is input to the control section C.
  • the load cell 95 outputs the load of the metal particles M and the metal oxide particles MO in addition to the oxidation tower 10 and the reduction tower 20.
  • the control unit C can measure the amount of metal particles M and metal oxide particles MO based on the output from the load cell 95.
  • the metal particles M and the metal oxide particles MO may be damaged when circulating between the oxidation tower 10 and the reduction tower 20 in the circulation section 60. This broken piece may be discharged from the oxidation tower 10 together with gas components in the solid-gas separator 50 described above. As a result, the loads of the metal particles M and the metal oxide particles MO are reduced by the amount discharged from the oxidation tower 10.
  • the control unit C determines how much the weight of the oxidation tower 10 and the reduction tower 20 (including the weight of the metal particles M and the metal oxide particles MO) has been since the start of operation when the metal particles M were accommodated. It may be determined whether or not the metal particles M should be replenished by calculating the extent to which the weight has decreased.
  • the control unit C may calculate the amount of metal particles M to be replenished from the amount of decrease in weight, and display the replenishment amount on a display device or the like.
  • the fluidizing gas supply line 16 supplies fluidizing gas to the fluidizing gas chamber 92.
  • the fluidizing gas supply line 16 (nitrogen supply line 18) has one end connected to the fluidizing gas introduction section 47 and the other end connected to a nitrogen supply section (not shown).
  • the nitrogen supply section includes, for example, a tank for storing nitrogen, a pump, and the like.
  • the nitrogen supply unit may be connected to a nitrogen supply system provided in a building such as a factory, for example, and may be shared with other equipment.
  • the air supply line 19 supplies air to the air chamber 91.
  • the air supply line 19 has one end connected to an air supply section (not shown) and the other end connected to the air introduction section 46 .
  • the air supply section includes, for example, a tank that stores air, a pump that sends air, and the like.
  • the air supply line 19 sends air from the air supply section to the air introduction section 46 .
  • the air supply line 19 may include, for example, a flow meter, a pressure regulating valve, and the like. By operating these flowmeters, pressure regulating valves, etc., the air supply line 19 can send air at a preset flow rate to the air introduction section 46.
  • the reducing agent supply line 21 supplies an organic solvent or the like which is the reducing agent R as a fuel to the fuel nozzle 40.
  • the organic solvent and the like function as a reducing agent in the reduction tower 20.
  • the organic solvent may contain powdered or granular resin (solid content).
  • An organic solvent, which is a reducing agent R, is sent to the reducing agent supply line 21 from a reducing agent tank 30 of a reducing agent supply system 200, which will be described later. Note that details of the reducing agent supply system 200 will be described later.
  • the circulation unit 60 circulates the metal particles M and the metal oxide particles MO between the reduction tower 20 and the oxidation tower 10.
  • the metal particles M filled in the oxidation tower 10 are oxidized to become oxidized metal particles MO and are in a fluidized state in the lower part 13 of the oxidation tower 10.
  • the oxidized metal particles MO enter the reduction tower 20 due to the flow of fuel ejected from the air nozzle 42, and after becoming metal particles M, the metal particles M are returned to the oxidation tower 10 by the solid-gas separator 50.
  • the circulation unit 60 circulates the metal particles M and the metal oxide particles MO between the reduction tower 20 and the oxidation tower 10.
  • the control unit C centrally controls the entire chemical loop reaction system 100.
  • the control unit C controls, for example, starting and stopping the operation of the chemical loop reaction system 100, setting the temperatures in the oxidation tower 10 and the reduction tower 20, and setting the operating time.
  • the control unit C raises the temperature inside the oxidation tower 10 and the reduction tower 20 to a predetermined temperature, supplies air to the oxidation tower 10, and so on.
  • FIG. 3 is an enlarged view of the main parts of the reducing agent supply system 200.
  • the reducing agent supply system 200 includes a reducing agent tank 30, a weight measuring device 31, a base 32, a stirring device (sedimentation prevention mechanism) 33, a supply section 34, and a supply pipe 35. , a discharge pipe 36, and a reducing agent pump P.
  • the reducing agent supply system 200 is configured to include a reducing agent supply line 21 and a control section C shown in FIG.
  • the reducing agent tank 30 stores reducing agent R, which is the fuel for the chemical loop reaction system 100.
  • the reducing agent tank 30 has, for example, a cylindrical shape with a bottom and an open top, but is not limited to the cylindrical shape, and may have a cylindrical shape with a bottom such as a rectangular shape or a polygonal shape in plan view. It may be the body.
  • the size of the reducing agent tank 30 can be set as appropriate depending on the amount of reducing agent R to be stored. Further, the material of the reducing agent tank 30 may be any material as long as it is resistant to corrosion by the reducing agent R, and examples thereof include metal, resin, and the like.
  • the reducing agent R used in this embodiment is not particularly limited, but is, for example, an organic solvent.
  • the organic solvent may contain solid content such as powdered or granular resin.
  • the solid content may be generated by a chemical reaction when a plurality of types of reducing agents R are mixed in the reducing agent tank 30.
  • the reducing agent R may be mixed with water in various solutions described below.
  • the reducing agent R for example, organic agents used in organic synthesis of paints, plastics, etc., and chemicals in general can be used. Chemical solutions used in the manufacturing process of elements can be used.
  • Examples of the chemical solution include those containing polar solvents such as ketone solvents, ester solvents, alcohol solvents, ether solvents, and amide solvents; hydrocarbon solvents, and the like.
  • chemical solutions containing resins include resin solutions generated by separation and purification during organic synthesis of resins, and chemical solutions for lithography containing resins such as resin solutions in which resin components for resist are dissolved in organic solvent components, and resist compositions. Examples include insulating film compositions, antireflection film compositions, block copolymer compositions applied to directed self assembly (DSA) technology, and resin compositions for imprinting.
  • examples of lithography chemicals used in pattern formation include pre-wet solvents, resist solvents, and developing solutions.
  • ketone solvents include 1-octanone, 2-octanone, 1-nonanone, 2-nonanone, acetone, 2-heptanone (methyl amyl ketone), 4-heptanone, 1-hexanone, 2-hexanone, diisobutyl ketone, Examples include cyclohexanone, methylcyclohexanone, phenylacetone, methyl ethyl ketone, methyl isobutyl ketone, acetylacetone, acetonylacetone, ionone, diacetonyl alcohol, acetyl carbinol, acetophenone, methylnaphthyl ketone, isophorone, propylene carbonate, and the like.
  • ester solvents include methyl acetate, butyl acetate, ethyl acetate, isopropyl acetate, pentyl acetate, isopentyl acetate, amyl acetate, propylene glycol monomethyl ether acetate, ethylene glycol monoethyl ether acetate, diethylene glycol monobutyl ether acetate, diethylene glycol monoethyl Ether acetate, ethyl-3-ethoxypropionate, 3-methoxybutyl acetate, 3-methyl-3-methoxybutyl acetate, methyl formate, ethyl formate, butyl formate, propyl formate, ethyl lactate, butyl lactate, propyl lactate, etc. Can be mentioned.
  • alcoholic solvents include methyl alcohol, ethyl alcohol, n-propyl alcohol, isopropyl alcohol, n-butyl alcohol, sec-butyl alcohol, tert-butyl alcohol, isobutyl alcohol, n-hexyl alcohol, n-heptyl alcohol, Alcohols such as n-octyl alcohol and n-decanol; glycol solvents such as ethylene glycol, diethylene glycol, and triethylene glycol; ethylene glycol monomethyl ether, propylene glycol monomethyl ether, ethylene glycol monoethyl ether, propylene glycol monoethyl ether, diethylene glycol monomethyl Examples include glycol ether solvents such as ether, triethylene glycol monoethyl ether, and methoxymethylbutanol.
  • ether solvent examples include dioxane, tetrahydrofuran, and the like, in addition to the above-mentioned glycol ether solvents.
  • amide solvents include N-methyl-2-pyrrolidone, N,N-dimethylacetamide, N,N-dimethylformamide, hexamethylphosphoric triamide, and 1,3-dimethyl-2-imidazolidinone. Can be mentioned.
  • hydrocarbon solvent examples include aromatic hydrocarbon solvents such as toluene and xylene; aliphatic hydrocarbon solvents such as pentane, hexane, octane, and decane.
  • thermoplastic resins examples include thermoplastic resins and thermosetting resins.
  • Thermosetting resins include polyethylene, polypropylene, polyvinyl chloride, polystyrene, acrylonitrile-butadiene-styrene, acrylonitrile-styrene, polymethyl methacrylic, polyvinyl alcohol, polyvinylidene chloride, polyethylene terephthalate, engineering plastics, super engineering plastics, etc. Can be mentioned.
  • thermosetting resin examples include phenol resin, urea resin, melamine resin, unsaturated polyester, epoxy resin, silicone resin, polyurethane, and the like.
  • the organic solvent used as the reducing agent R in this embodiment is preferably a used or unnecessary organic solvent waste liquid from the viewpoint of recycling waste as a fuel, and a resin waste liquid generated by separation and purification during organic synthesis of resin. Also, organic solvent waste liquid generated in the manufacturing process of semiconductor devices and liquid crystal display devices is more preferable. Examples of this organic solvent waste liquid include the various chemical solutions mentioned above, or a mixture thereof.
  • the weight measuring device 31 measures the weight of the reducing agent tank 30.
  • the weight measuring device 31 is arranged between the floor surface F and the base 32.
  • a known weighing scale such as a load cell can be used, for example.
  • the output of the weight measuring device 31 is input to the control section C.
  • the reducing agent tank 30 is placed on the upper surface of the base 32.
  • the stirring device 33 prevents the solid content contained in the reducing agent R from settling by stirring the reducing agent R.
  • the stirring device 33 includes a propeller 33A, a rotating shaft 33B, and a rotational drive source 33C.
  • the propeller 33A is provided at the lower end of the rotating shaft 33B, and is arranged near the bottom of the reducing agent tank 30.
  • the propeller 33A is composed of a plurality of blades, it may be a single blade. Alternatively, the propeller 33A may be provided in multiple stages in the vertical direction on the rotating shaft 33B.
  • the propeller 33A is made of, for example, a material that is resistant to corrosion by the reducing agent R (eg, metal, resin, etc.).
  • the rotating shaft 33B extends along the vertical direction, and is rotatably supported around the central axis O by a support portion (not shown).
  • the propeller 33A rotates around the central axis O due to the rotation of the rotating shaft 33B.
  • the rotation drive source 33C rotates the rotation shaft 33B around the central axis O.
  • As the rotational drive source 33C for example, an electric motor or the like is used.
  • the operation of the rotational drive source 33C is controlled by the control section C.
  • the control unit C instructs the timing and rotation speed of the propeller 33A.
  • the reducing agent R By rotating the propeller 33A in the reducing agent R stored in the reducing agent tank 30, the reducing agent R can be stirred. That is, even if the reducing agent R contains solid content, by stirring the reducing agent R, it is possible to prevent the solid content from settling and coagulating near the bottom of the reducing agent tank 30.
  • the control unit C may obtain information on the reducing agent R stored in the reducing agent tank 30 in advance, and may instruct whether or not the propeller 33A needs to be rotated, the timing, the number of rotations, the rotation time, etc.
  • the control unit C may rotate the propeller 33A continuously or intermittently.
  • the reducing agent R is supplied to the reducing agent tank 30 via the supply pipe 35 by the supply section 34 (see FIG. 1).
  • the supply unit 34 includes, for example, a liquid sending pump, and supplies the waste liquid (reducing agent R) sent from the waste liquid lines of various devices to the reducing agent tank 30 using the liquid sending pump.
  • the supply unit 34 may include a tank that temporarily stores waste liquid.
  • the reducing agent R is supplied from one supply pipe 35 to the reducing agent tank 30, but the present invention is not limited to this form, and different reducing agents R or the same type of reduction can be supplied from a plurality of supply pipes 35.
  • the agent R may be supplied to the reducing agent tank 30.
  • the operation of the supply section 34 is controlled by the control section C.
  • the control unit C may continuously supply the reducing agent R to the reducing agent tank 30, or may intermittently supply the reducing agent R by operating the supply unit 34 based on the measurement result of the weight measuring device 31.
  • R may be supplied to the reducing agent tank 30.
  • the control unit C may supply the reducing agent R to the reducing agent tank 30 at a timing when the reducing agent R in the reducing agent tank 30 decreases and the reducing agent tank 30 becomes lighter. With this configuration, it is possible to maintain a state in which the reducing agent tank 30 contains a predetermined amount or more of the reducing agent R.
  • the discharge pipe 36 delivers the reducing agent R in the reducing agent tank 30 to the reducing agent supply line 21.
  • One end of the discharge pipe 36 is inserted into the reducing agent R in the reducing agent tank 30, and the other end is connected to the reducing agent pump P (see FIG. 1).
  • the reducing agent pump P sucks up the reducing agent R from the reducing agent tank 30 via the discharge pipe 36 and sends out the reducing agent R to the reducing agent supply line 21 .
  • any liquid feeding pump or the like can be used as the reducing agent pump P.
  • the control unit C centrally controls the reducing agent supply system 200.
  • the control unit C drives the rotational drive source 33C to control the rotation of the propeller 33A. Further, the control unit C drives the supply unit 34 based on the measurement result of the weight measuring device 31, and controls the amount of reducing agent R supplied to the reducing agent tank 30.
  • the control section C is configured as a part of the control section C of the chemical loop reaction system 100, it is not limited to this form.
  • the control unit C may be configured as a separate control unit from the control unit C of the chemical loop reaction system 100.
  • metal particles M are filled into the oxidation tower 10.
  • the metal particles M include iron, iron oxide (FeO, Fe 2 O 3 , Fe 3 O 4 ), ilmenite (FeTiO 3 ), and the like.
  • the oxidation tower 10 may be filled with not only the metal particles M but also the metal oxide particles MO.
  • the amount of metal particles M to be filled is such that the metal particles M (or metal oxide particles MO) flow in the oxidation tower 10 by the fluidized gas jetted into the oxidation tower 10 from the fluidized gas nozzle 44, and the metal particles M are transported by the circulation section 60. It is set within a range that allows circulation.
  • the filling amount of the metal particles M is set, for example, within a range that allows the reduction tower 20 to sufficiently generate carbon dioxide.
  • a preheating burner (not shown) disposed inside the oxidation tower 10 (for example, the central part 12 thereof) or an electric lamp (not shown) attached to the peripheral wall of the oxidation tower 10 (for example, the central part 12 thereof)
  • the metal particles M are preheated to, for example, about 600° C. by a preheating means such as a heater.
  • a predetermined amount of air is supplied from the air supply line 19 to the air chamber 91 via the air introduction part 46.
  • the air supplied to the air chamber 91 is ejected into the oxidation tower 10 from the air nozzle 42.
  • the air blown into the oxidation tower 10 functions as an oxidizing agent and oxidizes the metal particles M into oxidized metal particles MO.
  • the control unit C supplies the reducing agent R from the supply unit 34 to the reducing agent tank 30 via the supply pipe 35.
  • the control unit C rotates the propeller 33A to stir the reducing agent R, and prevents the solid content contained in the reducing agent R from settling in the reducing agent tank 30.
  • the control unit C causes the reducing agent pump P to send out the reducing agent R in the reducing agent tank 30 from the discharge pipe 36 to the reducing agent supply line 21.
  • the reducing agent R is injected into the reducing tower 20 from the fuel nozzle 40 via the reducing agent supply line 21 .
  • fluidizing gas is supplied from the fluidizing gas supply line 16 to the fluidizing gas chamber 92 via the fluidizing gas introduction section 47.
  • the fluidizing gas in the fluidizing gas chamber 92 is ejected into the oxidation tower 10 from the fluidizing gas nozzle 44 .
  • the fluidizing gas fluidizes the metal particles M within the oxidation tower 10. Nitrogen is sent to the fluidizing gas supply line 16, and nitrogen is ejected from the fluidizing gas nozzle 44 as a fluidizing gas.
  • the metal particles M preheated to the reaction temperature react with oxygen in the supplied air to generate metal oxide particles MO.
  • heat is generated by the oxidation reaction of the metal, and the temperatures of the metal particles M, the oxidized metal particles MO, and the air flowing in the oxidation tower 10 rise.
  • heat is generated due to the oxidation reaction of the metal, and no high temperature portion of 1500° C. or higher is generated, so thermal NO x is not generated.
  • the metal oxide particles MO may be in a further oxidized form.
  • the metal oxide particles MO are Fe 3 O 4
  • the metal oxide particles MO may be further oxidized to become Fe 2 O 3 or the like.
  • the oxidized metal particles MO and the unoxidized metal particles M flow into the reduction tower 20 in the oxidation tower 10 and then rise inside the reduction tower 20.
  • the metal oxide particles MO undergo a reduction action by an organic solvent and become metal particles M.
  • the solid components and gas components rising in the reduction tower 20 are separated into solid components and gas components by the solid-gas separator 50.
  • the gas components ascend through the solid-gas separator 50 and are exhausted from the exhaust section 57 at the upper part of the reduction tower 20 .
  • the solid components, that is, the metal particles M and the remaining metal oxide particles MO are returned into the oxidation tower 10 by the solid-gas separator 50.
  • the air supplied to the oxidation tower 10 becomes a high-temperature gas and is discharged from the exhaust section 14 at the upper part of the oxidation tower 10.
  • metal pieces and the like in the gas discharged from the oxidation tower 10 are separated by the solid-gas separator 15 and returned to the oxidation tower 10 when necessary.
  • the discharged gas becomes either highly concentrated nitrogen containing no oxygen or a mixed gas containing residual oxygen and nitrogen.
  • nitrogen may be sent to a nitrogen storage tank or the like and stored through a recovery line (not shown).
  • the chemical loop reaction system 100 of the first embodiment by stirring the reducing agent R in the reducing agent tank 30, coagulation and sedimentation of the reducing agent R in the reducing agent tank 30 is suppressed. Ru. Therefore, when the reducing agent R is supplied to the reducing column 20 of the chemical loop reaction system 100, the reducing agent pump P does not malfunction and the discharge pipe 36 and reducing agent supply line 21 are not clogged. As a result, the chemical loop reaction system 100 can be stably operated.
  • FIG. 4 is a flowchart illustrating an example of the reducing agent supply method according to the first embodiment.
  • FIG. 5 is a flowchart following FIG. 4 and illustrating an example of the reducing agent supply method.
  • FIG. 6 is a flowchart showing a part of the flowchart of FIG. 5 in detail. 4 to 6 show the operational flow of the chemical loop reaction system 100, and this flow includes the reducing agent supply method according to the first embodiment.
  • the operations shown in the flowcharts of FIGS. 4 to 6 may be performed by the control unit C, or may be performed by an operator or the like.
  • the oxidation tower 10 is filled with metal particles M (step S01).
  • the oxidation tower 10 is provided with a raw material input port (not shown), and a predetermined amount of metal particles M are charged from the raw material input port and filled into the oxidation tower 10.
  • the metal particles M may be introduced by a supply device or the like, or by an operator. When the metal particles M are introduced using a supply device or the like, the amount of injection may be set in advance and the injection may be performed automatically under the control of the control unit C.
  • step S02 the temperatures of the oxidation tower 10 and the reduction tower 20 are raised.
  • step S02 the temperature of the oxidation tower 10 and the reduction tower 20 is raised by an electric heater (not shown) or the like.
  • step S03 sedimentation of the solid content contained in the reducing agent R is prevented.
  • the reducing agent R is supplied to the reducing agent tank 30 from the supply unit 34 via the supply pipe 35. Note that, as described above, the amount of the reducing agent R stored in the reducing agent tank 30 is maintained at a constant amount based on the measurement result of the weight measuring device 31.
  • step S03 the reducing agent R in the reducing agent tank 30 is stirred by the rotation of the propeller 33A of the stirring device 33, and solid content contained in the reducing agent R is prevented from settling.
  • step S04 air is supplied to the oxidation tower 10 (step S04).
  • step S04 air is supplied to the oxidation tower 10 via the air nozzle 42.
  • the amount of air to be supplied is appropriately set depending on the filling amount of metal particles M.
  • nitrogen is supplied to the oxidation tower 10 and the reduction tower 20 (step S05).
  • step S05 nitrogen is supplied to the oxidation tower 10 via the fluidizing gas nozzle 44.
  • step S06 the reducing agent R, which is a fuel, is supplied to the reducing tower 20 (step S06).
  • the reducing agent R is sucked up from the reducing agent tank 30 via the exhaust pipe 36 by the reducing agent pump P, and is supplied to the reducing tower 20 from the fuel nozzle 40 via the reducing agent supply line 21.
  • the reducing agent pump P malfunctions, the discharge pipe 36 or It is possible to suppress clogging of the reducing agent supply line 21 and the fuel nozzle 40, and to appropriately supply the reducing agent R to the reduction tower 20.
  • steps S04 to S06 may be performed in order or may be performed simultaneously.
  • the solid-gas separator 50 is operated (step S07).
  • carbon dioxide and metal particles M are separated by the solid-gas separator 50 (step S08).
  • the solid-gas separator 50 separates carbon dioxide, which is a gas component, and metal particles M, which is a solid component.
  • carbon dioxide is exhausted from the solid-gas separator 50 to the outside through an exhaust section 57.
  • the metal particles M are sent to the oxidation tower 10 (step S09).
  • the metal particles M are returned from the solid-gas separator 50 to the oxidation tower 10.
  • step S10 the operating state of the chemical loop reaction system 100 is continued for a predetermined period of time (step S10).
  • the flowchart shown in FIG. 6 is executed during a predetermined period of time in step S10.
  • the operation of the flowchart shown in FIG. 6 may be executed by the control unit C, or may be executed by an operator or the like.
  • the weight of the reducing agent tank 30 is measured (step S21).
  • the control unit C obtains the measured value of the weight of the reducing agent tank 30 by the weight measuring device 31.
  • step S22 the control unit C determines whether the weight of the reducing agent tank 30 is lighter than a preset threshold.
  • the control unit C compares the measured value obtained from the weight measuring device 31 with a threshold value stored in advance in a storage unit (not shown), etc., and determines whether the measured value is smaller than the threshold value. do. If it is determined that the weight of the reducing agent tank 30 is lighter than the threshold value (YES in step S22), the reducing agent R is replenished into the reducing agent tank 30 (step S23).
  • step S23 the control unit C supplies the reducing agent R to the reducing agent tank 30 using the supply unit 34.
  • the control unit C may supply a preset amount of the reducing agent R to the reducing agent tank 30, or may refer to the measurement result of the weight measuring device 31 and determine the measured value.
  • the reducing agent R may be supplied to the reducing agent tank 30 until the amount exceeds the threshold value. Note that if it is determined that the weight of the reducing agent tank 30 is heavier than the threshold value (NO in step S22), the reducing agent R is not replenished.
  • Steps S21 to S23 are repeatedly executed during the predetermined time period during which the chemical loop reaction system 100 is operated in step S10 described above.
  • the control unit C stops the supply of air, reducing agent R, and nitrogen (step S11).
  • the control unit C stops the stirring device 33 and the solid-gas separator 50 (step S12).
  • step S12 the chemical loop reaction system 100 and the reducing agent supply system 200 stop operating, and the series of processes described above ends.
  • reducing agent supply systems 200A, 200B, 200C, and 200D according to modified examples will be described with reference to FIGS. 7 to 10.
  • FIGS. 7 to 10 the same components as those in the above-described embodiment are given the same reference numerals, and the description thereof will be omitted or simplified.
  • FIG. 7 is an enlarged view of main parts of a reducing agent supply system 200A according to a first modification.
  • the reducing agent supply system 200A includes a stirring device (sedimentation prevention mechanism) 133.
  • the reducing agent supply system 200A is configured to include the reducing agent supply line 21 and the control section C shown in FIG.
  • the stirring device 133 includes a propeller 33A, a rotating shaft 33B, a rotational drive source 33C, and heating devices 133A and 133B.
  • the propeller 33A, rotating shaft 33B, and rotational drive source 33C have the same configuration as in the above-described embodiment, so a description thereof will be omitted.
  • the heating devices 133A and 133B can heat the reducing agent tank 30 and heat the reducing agent R stored in the reducing agent tank 30. Therefore, even when the viscosity of the reducing agent R is high, the viscosity of the reducing agent R can be reduced and the fluidity can be improved. Further, depending on the heating temperature of the reducing agent R, powdery or granular solid resin or the like can be melted in the reducing agent R.
  • the heating device 133A is provided on the outer peripheral side of the reducing agent tank 30.
  • the heating device 133B is provided on the base 32.
  • electric heaters are used as the heating devices 133A and 133B.
  • the heating device 133A is not limited to being provided in contact with the outer peripheral surface of the reducing agent tank 30, but may be provided apart from the outer peripheral surface of the reducing agent tank 30.
  • the present invention is not limited to providing both of the heating devices 133A and 133B, and may be a form in which either one of the heating devices 133A and 133B is provided.
  • the heating device may be arranged inside the reducing agent tank 30 (for example, inside the reducing agent R stored therein).
  • the operation of the heating devices 133A and 133B is controlled by the control section C.
  • the control unit C controls the operation timing, heating temperature, heating time, etc. of the heating devices 133A and 133B.
  • the control unit C causes the heating devices 133A and 133B to heat the reducing agent R to a predetermined temperature at the timing when the propeller 33A is rotated to stir the reducing agent R.
  • the control unit C may first heat the reducing agent R to a predetermined temperature using the heating devices 133A and 133B to reduce the viscosity of the reducing agent R, and then rotate the propeller 33A.
  • the viscosity of the reducing agent R is low, when the propeller 33A is rotated, the load placed on the propeller 33A, the rotating shaft 33B, and the rotational drive source 33C can be reduced.
  • the heating devices 133A and 133B are stopped at the same time as the stirring device 133 is stopped, for example, in step S12 of FIG. 5 described above.
  • the reducing agent R can be appropriately supplied to the reduction tower 20. Furthermore, in the first modification, since the reducing agent R is heated by the heating devices 133A and 133B to increase its fluidity, the reducing agent R is efficiently stirred, and the reducing agent R is contained in the reducing agent R in the reducing agent tank 30. It is possible to further suppress sedimentation or agglomeration of the solid content.
  • FIG. 8 is an enlarged view of main parts of a reducing agent supply system 200B according to a second modification.
  • the reducing agent supply system 200B includes a stirring device (sedimentation prevention mechanism) 233.
  • the reducing agent supply system 200B is configured to include the reducing agent supply line 21 and the control section C shown in FIG.
  • the stirring device 233 includes a stirring bar 233A and a drive section 233B.
  • a rod-shaped magnet or a magnetic material is used for the stirrer 233A, and the stirrer 233A is arranged at the bottom of the reducing agent tank 30.
  • the stirrer 233A is a rod-shaped body having a dimension shorter than the inner diameter of the reducing agent tank 30, and is used in accordance with the inner diameter of the reducing agent tank 30.
  • the stirrer 233A is rotatable around the central axis O1 at the bottom of the reducing agent tank 30.
  • the drive unit 233B rotates the stirrer 233A around the central axis O1.
  • the drive unit 233B has, for example, a configuration that switches the position (or direction) of the magnetic flux B acting on the stirrer 233A, and by sequentially switching the position of the magnetic flux B, moves the stirrer 233A around the central axis O1. It may also be in the form of rotation. Further, the drive unit 233B may be configured to rotate the stirrer 233A around the central axis O1 by, for example, rotating a magnet that attracts the stirrer 233A with an electric motor. The operation of the drive section 233B is controlled by the control section C.
  • the reducing agent R in the reducing agent tank 30 is stirred by the stirring bar 233A being rotated around the central axis O1 by the drive unit 233B.
  • the reducing agent R can be appropriately supplied to the reduction tower 20.
  • the heating devices 133A and 133B of the first modification described above may be provided.
  • FIG. 9 is an enlarged view of main parts of a reducing agent supply system 200C according to a third modification.
  • the reducing agent supply system 200C includes a stirring device (sedimentation prevention mechanism) 333.
  • the reducing agent supply system 200C is configured to include the reducing agent supply line 21 and the control section C shown in FIG.
  • the stirring device 333 includes a vibrator 333A.
  • the vibrator 333A is connected to a drive circuit (not shown), etc., and vibrates at a predetermined frequency. For example, a piezo element or the like is used as the vibrator 333A.
  • the vibrator 333A is placed, for example, at the center of the bottom of the reducing agent tank 30, but is not limited to this position, and can be placed anywhere, such as on the inner wall surface of the reducing agent tank 30, if the reducing agent R is present. It can be placed in the position of Further, the shape of the vibrator 333A is arbitrary.
  • the operation of the vibrator 333A is controlled by the control section C.
  • the reducing agent R in the reducing agent tank 30 is stirred by the vibration of the vibrator 333A.
  • the vibrator 333A is placed at one location in the reducing agent tank 30, but a plurality of vibrators 333A may be placed in the reducing agent tank 30.
  • the plurality of vibrators 333A may be arranged at intervals on the bottom, inner wall, etc. of the reducing agent tank 30.
  • the frequencies at which they vibrate may be the same or different.
  • the vibrator 333A may be provided outside the reducing agent tank 30, and vibrate to vibrate the reducing agent tank 30 itself (or shake the reducing agent tank 30).
  • the heating devices 133A and 133B of the first modification described above may be provided.
  • FIG. 10 is an enlarged view of main parts of a reducing agent supply system 200D according to a fourth modification.
  • the reducing agent supply system 200D includes a stirring device (sedimentation prevention mechanism) 433.
  • the reducing agent supply system 200D is configured to include the reducing agent supply line 21 and the control section C shown in FIG.
  • the stirring device 433 includes an ultrasonic oscillator 433A.
  • the ultrasonic oscillator 433A is connected to a drive circuit (not shown), etc., and oscillates ultrasonic waves.
  • the ultrasonic oscillator 433A may be of an electrostrictive type or a magnetostrictive type.
  • the ultrasonic oscillator 433A is provided on the base 32, for example, so as to be in contact with the lower surface of the reducing agent tank 30.
  • the operation of the ultrasonic oscillator 433A is controlled by the control unit C.
  • the reducing agent R in the reducing agent tank 30 is stirred by the ultrasonic oscillator 433A oscillating ultrasonic waves.
  • one ultrasonic oscillator 433A is arranged, but a plurality of ultrasonic oscillators 433A may be arranged.
  • the ultrasonic oscillator 433A may be provided at any position, and may be provided on the outer wall surface of the reducing agent tank 30.
  • the fourth modification as in the first embodiment described above, even if the reducing agent R contains powdery or granular solids, it is possible to suppress the solids from settling or aggregating. . Therefore, the reducing agent R can be appropriately supplied to the reduction tower 20.
  • the heating devices 133A and 133B of the first modification described above may be provided.
  • FIG. 11 is a diagram showing an example of a reducing agent supply system 200E and a chemical loop reaction system 100A according to the second embodiment. Note that the same configurations as those in the first embodiment described above are given the same reference numerals, and the description thereof will be omitted or simplified. As shown in FIG. 11, the chemical loop reaction system 100A includes a reducing agent supply system 200E.
  • the chemical loop reaction system 100A includes an oxidation tower 10, a reduction tower 20, a fluidizing gas supply line 16 (nitrogen supply line 18), an air supply line 19, a reducing agent supply line 21, a first supply line 21A, It includes a second supply line 21B, a switching valve 21C, a circulation section 60, a control section C, and a reducing agent supply system 200E.
  • the reducing agent supply system 200E includes a first supply system 200E1 and a second supply system 200E2. Further, the reducing agent supply system 200E includes a reducing agent supply line 21 and a control section C. Each of the first supply system 200E1 and the second supply system 200E2 has the same configuration as the reducing agent supply system 200 of the first embodiment described above. Note that the same reducing agent R may be stored in the reducing agent tank 30 of the first supply system 200E1 and the reducing agent tank 30 of the second supply system 200E2, or different reducing agents R may be stored. .
  • each of the first supply system 200E1 and the second supply system 200E2 includes a supply section 34, but the first supply system 200E1 and the second supply system 200E2 are connected to each other from one supply section 34.
  • the reducing agent R may be supplied to each reducing agent tank 30.
  • each of the first supply system 200E1 and the second supply system 200E2 includes a reducing agent pump P, one reducing agent pump P may be provided in the reducing agent supply line 21.
  • the first supply system 200E1 is connected to the switching valve 21C via the first supply line 21A.
  • the second supply system 200E2 is connected to the switching valve 21C via the second supply line 21B.
  • the switching valve 21C is, for example, a three-way valve, and switches between a first state in which the first supply line 21A is connected to the reducing agent supply line 21 and a second state in which the second supply line 21B is connected to the reducing agent supply line 21. .
  • the operation of the switching valve 21C may be controlled by the control unit C or may be performed by an operator or the like.
  • the control unit C sets the switching valve 21C to the first state
  • the reducing agent R is transferred from the reducing agent tank 30 of the first supply system 200E1 to the reducing agent supply line 21 via the first supply line 21A and the switching valve 21C. It is sent and supplied to the reduction tower 20.
  • the control unit C sets the switching valve 21C to the second state
  • the reducing agent R is transferred from the reducing agent tank 30 of the second supply system 200E2 to the reducing agent supply line via the second supply line 21B and the switching valve 21C. 21 and supplied to the reduction tower 20.
  • the control unit C may, for example, switch the switching valve 21C between the first state and the second state at regular intervals. In addition, when performing maintenance on either the first supply system 200E1 or the second supply system 200E2, the control unit C switches the switching valve 21C so that the reducing agent R can be supplied from either the other. good.
  • control unit C compares, for example, the amount of reducing agent R stored in the reducing agent tank 30 of the first supply system 200E1 and the amount of reducing agent R stored in the reducing agent tank 30 of the second supply system 200E2. Then, the switching valve 21C may be switched so that the reducing agent R is supplied to the reducing tower 20 from the reducing agent tank 30 that stores a larger amount. Further, the control unit C controls, for example, the amount of reducing agent R sent to the reducing agent tank 30 of the first supply system 200E1 (that is, the amount of waste liquid), and the amount of reducing agent R sent to the reducing agent tank 30 of the second supply system 200E2. The switching valve 21C may be controlled to compare the amount of R and supply the reducing agent R to the reduction tower 20 from the reducing agent tank 30 that sends a larger amount.
  • FIG. 12 is a flowchart illustrating an example of the reducing agent supply method according to the second embodiment. Note that steps S01 to S09 and steps S11 and subsequent steps are the same as those in the flowcharts shown in FIGS. 4 and 5, and therefore their description will be omitted.
  • the flowchart shown in FIG. 12 is executed during a predetermined period of time in step S10 shown in FIG. Note that the operation of the flowchart shown in FIG. 12 may be executed by the control unit C, or may be executed by an operation of an operator or the like.
  • step S32 the control unit C operates the switching valve 21C to switch the reducing agent tank 30 (step S32).
  • step S32 the control unit C switches the switching valve 21C so that the reducing agent R is supplied from another reducing agent tank 30 instead of the reducing agent tank 30 currently being supplied (step S32).
  • step S32 the control unit C switches the switching valve 21C from the first state to the second state or from the second state to the first state.
  • the reducing agent R is supplied to the reduction tower 20 from the reducing agent tank 30 of the second supply system 200E2 instead of the reducing agent tank 30 of the first supply system 200E1.
  • the second state to the first state the reducing agent R is supplied to the reduction tower 20 from the reducing agent tank 30 of the first supply system 200E1 instead of the reducing agent tank 30 of the second supply system 200E2.
  • Steps S31 and S32 are repeatedly executed during the predetermined time period during which the chemical loop reaction system 100 is operated in step S10 described above. After the predetermined time in step S10 has elapsed, steps S11 and subsequent steps shown in FIG. 5 are executed. Note that if the control unit C determines not to change the reducing agent tank 30 (NO in step S31), steps S11 and subsequent steps shown in FIG. 5 are executed after a predetermined period of time has elapsed.
  • the reducing agent supply system 200E As described above, according to the reducing agent supply system 200E, chemical loop reaction system 100A, and reducing agent supply method according to the second embodiment, powdery or granular solids are added to the reducing agent R as in the first embodiment described above. It is possible to suppress sedimentation or agglomeration of the solid content even if the solid content is contained. Therefore, the reducing agent R can be appropriately supplied to the reduction tower 20. Further, in the second embodiment, since the two first supply systems 200E1 and the second supply system 200E2 are included as the supply sources of the reducing agent R, it is possible to avoid interruption of the supply of the reducing agent R to the reduction tower 20. .
  • the reducing agent R can be continuously supplied to the reduction tower 20 by operating the other one.
  • two first supply systems 200E1 and two second supply systems 200E2 are provided, but three or more may be provided.
  • FIG. 13 is a diagram showing an example of a reducing agent supply system 200 and chemical loop reaction systems 100B1 and 100B2 according to the third embodiment. Note that the same configurations as those in the first embodiment described above are given the same reference numerals, and the description thereof will be omitted or simplified.
  • one reducing agent supply system 200 that is, one reducing agent tank 30
  • Chemical loop reaction systems 100B1 and 100B2 each have the same configuration as the chemical loop reaction system 100 of the first embodiment. Note that the chemical loop reaction systems 100B1 and 100B2 may be the same in size, form, etc., or may be different from each other.
  • the reducing agent supply system 200 branches the downstream side of the reducing agent supply line 21 and includes branch lines 21D and 21E.
  • the branch line 21D supplies the reducing agent R to the reduction tower 20 of the chemical loop reaction system 100B1.
  • the branch line 21E supplies the reducing agent R to the reduction tower 20 of the chemical loop reaction system 100B2.
  • the reducing agent supply system 200 can supply the reducing agent R to the two reducing towers 20 through the branch lines 21D and 21E.
  • a switching valve 21F is provided at the branch portion of the reducing agent supply line 21.
  • a three-way valve is used as the switching valve 21F.
  • the operation of the switching valve 21F may be controlled by the control unit C or may be performed by an operator or the like.
  • the switching valve 21F switches the connection destination of the reducing agent supply line 21 between the branch line 21D and the branch line 21E.
  • the reducing agent R in the reducing agent tank 30 is sent from the reducing agent supply line 21 to the branch line 21D or branch line 21E by the switching valve 21F.
  • the switching valve 21F may have a configuration that can simultaneously send the reducing agent R to both the branch lines 21D and 21E.
  • FIG. 14 is a flowchart illustrating an example of the reducing agent supply method according to the third embodiment. Note that steps S01 to S09 and steps S11 and subsequent steps are the same as those in the flowcharts shown in FIGS. 4 and 5, and therefore their description will be omitted.
  • the flowchart shown in FIG. 14 is executed during a predetermined period of time in step S10 shown in FIG. Note that the operation of the flowchart shown in FIG. 14 may be executed by the control unit C, or may be executed by an operation by an operator or the like.
  • the control unit C determines whether to change the supply destination of the reducing agent R (step S41).
  • the control unit C controls the supply destination of the reducing agent R, for example, when the chemical loop reaction system 100B1 or the chemical loop reaction system 100B2 in operation malfunctions, or when the operation is stopped for maintenance or the like. Decide whether to change or not.
  • the supply destination may be changed by stopping the operation of one of the two chemical loop reaction systems 100B1 and 100B2 when both are in operation, and making the other one the supply destination for the reducing agent R. include.
  • step S41 If the control unit C determines to change the supply destination of the reducing agent R (YES in step S41), the control unit C operates the switching valve 21F to switch the supply destination of the reducing agent R (step S42).
  • step S42 the control unit C switches the supply destination of the reducing agent R from the chemical loop reaction system 100B1 to the chemical loop reaction system 100B2, or from the chemical loop reaction system 100B2 to the chemical loop reaction system 100B1.
  • the reducing agent R in the reducing agent tank 30 is sent to the supply destination switched by the switching valve 21F.
  • Steps S41 and S42 are repeatedly executed during the predetermined time period during which the chemical loop reaction system 100 is operated in step S10 described above. After the predetermined time in step S10 has elapsed, steps S11 and subsequent steps shown in FIG. 5 are executed. Note that if the control unit C determines not to change the supply destination of the reducing agent R (NO in step S41), steps after step S11 shown in FIG. 5 are executed after a predetermined period of time has elapsed.
  • the reducing agent R is powdered or granular, as in the first embodiment described above. Even if the solid content is contained, precipitation or aggregation of the solid content can be suppressed. Therefore, the reducing agent R can be appropriately supplied to the reduction tower 20. Further, since one reducing agent supply system 200 is used for the two chemical loop reaction systems 100B1 and 100B2, the entire system can be made more compact. In the example shown in FIG. 13, two chemical loop reaction systems 100B1 and 100B2 are used, but three or more may be used.
  • FIG. 15 is a diagram showing an example of a reducing agent supply system 200 and a chemical loop reaction system 100C according to the fourth embodiment. Note that the same configurations as those in the first embodiment described above are given the same reference numerals, and the description thereof will be omitted or simplified.
  • the chemical loop reaction system 100C includes a reducing agent supply system 200.
  • the chemical loop reaction system 100C recovers carbon dioxide generated in the reduction tower 20 and uses it in the chemical loop reaction system 100C. As shown in FIG.
  • the chemical loop reaction system 100C includes an oxidation tower 10, a reduction tower 20, a fluidizing gas supply line 16, a nitrogen supply line 18, an air supply line 19, a reducing agent supply line 21, It includes a steam supply line 23, a circulation section 60, a carbon dioxide supply line 70, a control section C, and a reducing agent supply system 200.
  • the reducing agent supply line 21 mixes the reducing agent R as a fuel with steam and supplies the mixture to the fuel nozzle 40 .
  • the reducing agent supply line 21 has a mixing section 22 .
  • a steam supply line 23 is connected to the mixing section 22 .
  • the mixing unit 22 mixes the reducing agent R sent through the reducing agent supply line 21 and the steam sent through the steam supply line 23 at a predetermined ratio set in advance.
  • the steam supply line 23 is equipped with a steam generation unit 24 and supplies the steam generated by the steam generation unit 24 to the mixing section 22.
  • the steam generation unit 24 includes a heat source (not shown) and heats water supplied from the water supply line 25 to generate steam.
  • the water supply line 25 is connected to a water supply section (not shown).
  • the water supply section includes, for example, a water storage tank, a water pump, and the like.
  • a carrier gas supply line 26 is connected to the steam generation unit 24.
  • the carrier gas supply line 26 supplies carrier gas to the steam generation unit 24 .
  • the carrier gas is used to flow the steam generated by the steam generation unit 24 into the steam supply line 23 .
  • the carrier gas supply line 26 is connected via a first switching valve 27 to a second nitrogen supply line 28 (described later) and a second connection line 79 that is part of the first line 74 among the carbon dioxide supply lines 70 (described later). be done.
  • the first switching valve 27 is controlled by the control unit C to switch the connection destination with the carrier gas supply line 26.
  • the first switching valve 27 is connected to the carrier gas supply line 26 , the second nitrogen supply line 28 , and the second connection line 79 .
  • the first switching valve 27 switches the connection destination of the carrier gas supply line 26 between the second nitrogen supply line 28 and the second connection line 79 .
  • nitrogen is supplied to the steam generation unit 24 as the carrier gas.
  • carbon dioxide is supplied to the steam generation unit 24 as the carrier gas.
  • the fluidizing gas supply line 16 supplies fluidizing gas to the fluidizing gas chamber 92.
  • the fluidizing gas supply line 16 has one end connected to the second switching valve 17 and the other end connected to the fluidizing gas introduction section 47 .
  • the second switching valve 17 is controlled by the control section C to switch the connection destination with the fluidizing gas supply line 16.
  • the second switching valve 17 is connected to a third connection line 80 that is a part of the first line 74 among the fluidizing gas supply line 16 , the nitrogen supply line 18 , and the carbon dioxide supply line 70 .
  • the second switching valve 17 switches the connection destination of the fluidizing gas supply line 16 between the nitrogen supply line 18 and the third connection line 80.
  • nitrogen is supplied to the fluidizing gas chamber 92 as a carrier gas.
  • carbon dioxide is supplied to the fluidizing gas chamber 92 as the fluidizing gas.
  • the nitrogen supply line 18 is connected to a nitrogen supply section (not shown).
  • the nitrogen supply section includes, for example, a tank for storing nitrogen, a pump, and the like.
  • the nitrogen supply line 18 may be connected to a nitrogen supply system provided in a building such as a factory, for example, and may be connected to other equipment.
  • the nitrogen supply line 18 branches on the upstream side of the second switching valve 17, and a second nitrogen supply line 28 is formed. Therefore, the nitrogen flowing through the nitrogen supply line 18 is divided into a flow toward the second switching valve 17 and a flow toward the first switching valve 27 via the second nitrogen supply line 28 .
  • the carbon dioxide supply line 70 supplies carbon dioxide generated in the reduction tower 20 to at least one of the reduction tower 20 and the oxidation tower 10.
  • the carbon dioxide supply line 70 is connected via an on-off valve 59 on the downstream side of the gas-liquid separation device 58 .
  • the opening/closing valve 59 is controlled by the control unit C and can adjust the flow rate of carbon dioxide flowing from the reduction tower 20 to the carbon dioxide supply line 70.
  • the carbon dioxide supply line 70 includes a recovery line 71 , a flow meter 72 , a regulating valve 73 , a first line 74 , a first tank 75 , a second line 76 , and a second tank 77 .
  • the recovery line 71 connects the on-off valve 59 and the flow rate measuring device 72 (adjusting valve 73).
  • the flow rate measuring device 72 measures the flow rate of carbon dioxide flowing through the recovery line 71 per unit time.
  • the regulating valve 73 is provided in the recovery line 71 and connected to the recovery line 71 , the first line 74 , and the second line 76 .
  • the embodiment in which the flow rate measuring device 72 and the regulating valve 73 are implemented as one device is described as an example, but the embodiment is not limited to this embodiment.
  • the regulating valve 73 may be provided downstream of the flow rate measuring device 72 in the recovery line 71.
  • the regulating valve 73 has a first mode in which the recovery line 71 and the first line 74 are communicated, a second mode in which the recovery line 71 and the second line 76 are communicated, and a second mode in which the first line 74 and the second line 76 are communicated. Switch to one of the third modes.
  • the regulating valve 73 may simultaneously execute the first mode and the second mode described above. That is, the regulating valve 73 may have a mode in which carbon dioxide from the recovery line 71 is sent to both the first line 74 and the second line 76.
  • the regulating valve 73 is set to the third mode, it becomes possible to flow the carbon dioxide stored in the first tank 75 from the second line 76 to the first line 74 via the regulating valve 73.
  • the first line 74 is provided downstream of the regulating valve 73.
  • the first line 74 includes a first connection line 78 , a second connection line 79 , and a third connection line 80 .
  • the first connection line 78 connects between the regulating valve 73 and the first tank 75.
  • the first tank 75 stores carbon dioxide sent through the first connection line 78.
  • the first tank 75 functions as a buffer that temporarily stores carbon dioxide flowing through the first line 74. Note that whether or not to provide the first tank 75 is arbitrary, and a configuration in which the first tank 75 is not provided may be used.
  • the second connection line 79 connects the first tank 75 and the first switching valve 27 described above.
  • the third connection line 80 branches from the second connection line 79 and is connected to the second switching valve 17 . That is, the third connection line 80 connects the first tank 75 and the second switching valve 17 described above.
  • the second line 76 is provided separately from the first line 74 and connects the regulating valve 73 and the second tank 77.
  • the second tank 77 stores carbon dioxide sent from the second line 76 when the regulating valve 73 is set to the second mode.
  • the second tank 77 switches the regulating valve 73 into the second mode to allow carbon dioxide to flow through the second line 76. can be sent to the first line 74.
  • whether or not to provide the second line 76 and the second tank 77 is arbitrary, and a configuration in which the second line 76 and the second tank 77 are not provided may be used.
  • the reducing agent R supplied to the reducing tower 20 is sent from the reducing agent supply system 200 to the reducing agent supply line 21, mixed with steam sent from the steam supply line 23, and then supplied to the reducing tower 20 from the fuel nozzle 40.
  • the first switching valve 27 is set so that the carrier gas supply line 26 is connected to the second nitrogen supply line 28.
  • nitrogen is supplied to the steam generation unit 24 from the second nitrogen supply line 28 as a carrier gas.
  • the steam generated in the steam generation unit 24 is conveyed to the mixing section 22 by nitrogen as a carrier gas, mixed with the reducing agent R, and supplied to the fuel nozzle 40.
  • fluidizing gas is supplied from the fluidizing gas supply line 16 to the fluidizing gas chamber 92 via the fluidizing gas introduction section 47.
  • the fluidizing gas in the fluidizing gas chamber 92 is ejected into the oxidation tower 10 from the fluidizing gas nozzle 44 .
  • the fluidizing gas fluidizes the metal particles M within the oxidation tower 10.
  • the second switching valve 17 is set so that the fluidizing gas supply line 16 is connected to the nitrogen supply line 18. Therefore, nitrogen is ejected from the fluidizing gas nozzle 44 as a fluidizing gas.
  • the carbon dioxide generated and discharged in the reduction tower 20 is separated from water in the gas-liquid separator 58 and sent to the carbon dioxide supply line 70.
  • Carbon dioxide flows through a recovery line 71 in a carbon dioxide supply line 70, and its flow rate is measured by a flow rate measuring device 72.
  • the carbon dioxide that has passed through the flow rate measuring device 72 flows along the recovery line 71 to the regulating valve 73 .
  • the mode of the regulating valve 73 is switched according to the measurement result by the flow rate measuring device 72.
  • the regulating valve 73 is set to the first mode in the initial state. That is, in the initial state, the collection line 71 and the first line 74 are connected. Therefore, carbon dioxide flows from the recovery line 71 to the first line 74 .
  • the regulating valve 73 switches from the first mode to the second mode when the flow rate of carbon dioxide per unit time in the recovery line 71 exceeds a first threshold value. In this case, the recovery line 71 and the second line 76 are communicated.
  • the amount of reduction reaction of the metal oxide particles MO increases, thereby increasing the amount of carbon dioxide generated.
  • the regulating valve 73 switches from the first mode to the second mode. Therefore, carbon dioxide is sent from the recovery line 71 to the second line 76 and stored in the second tank 77 via the second line 76.
  • the adjustment valve 73 maintains the first mode when the flow rate of carbon dioxide per unit time in the recovery line 71 is greater than or equal to the second threshold and less than the first threshold.
  • the carbon dioxide sent from the recovery line 71 to the first line 74 or the carbon dioxide sent from the second line 76 to the first line 74 is sent to the first tank 75 via the first connection line 78, and then 1 tank 75.
  • the carrier gas supply line 26 and the second connection line 79 are connected by the first switching valve 27, the connection between the carrier gas supply line 26 and the second nitrogen supply line 28 is cut off, and the connection to the carrier gas supply line 26 is cut off. Nitrogen supply stops.
  • the carbon dioxide stored in the first tank 75 flows from the second connection line 79 to the carrier gas supply line 26 via the first switching valve 27 and is supplied to the steam generation unit 24. Therefore, the carrier gas for transporting steam is switched from nitrogen to carbon dioxide.
  • the steam generated by the steam generation unit 24 is sent to the steam supply line 23 together with carbon dioxide. In this way, by supplying carbon dioxide as the carrier gas to the steam generation unit 24 instead of nitrogen, consumption of nitrogen can be suppressed.
  • the fluidizing gas supply line 16 and the third connection line 80 are connected by the second switching valve 17, the connection between the fluidizing gas supply line 16 and the nitrogen supply line 18 is cut off, and the flow of nitrogen to the fluidizing gas supply line 16 is interrupted. Supply is cut off.
  • the carbon dioxide stored in the first tank 75 flows through the third connection line 80 and flows through the fluidizing gas supply line 16 via the second switching valve 17 . Therefore, the fluidizing gas supplied to the fluidizing gas chamber 92 is switched from nitrogen to carbon dioxide.
  • Carbon dioxide in the fluidizing gas chamber 92 is supplied to the oxidizing tower 10 from the fluidizing gas nozzle 44 and is used to fluidize the metal particles M and the metal oxide particles MO. In this way, by using carbon dioxide instead of nitrogen as the fluidizing gas, the amount of nitrogen used can be reduced.
  • the reducing agent supply method is the same as the reducing agent supply method of the first embodiment, so the description thereof will be omitted.
  • the reducing agent supply system 200 stirs the reducing agent R in the reducing agent tank 30 as in the first embodiment, and when the reducing agent R contains solid content, Even so, sedimentation and agglomeration of solids are suppressed. Therefore, the reducing agent R can be appropriately sent to the reducing agent supply line 21.
  • the carbon dioxide generated in the reduction tower 20 is supplied to the reduction tower 20 and the oxidation tower 10, part or all of the nitrogen supplied to the oxidation tower 10 and the reduction tower 20 is converted into dioxide. It can be replaced with carbon, reducing the amount of nitrogen used. As a result, the chemical loop reaction system 100C can be operated more efficiently. Further, since the generated carbon dioxide is used in the chemical loop reaction system 100C, carbon dioxide can be used effectively, and the amount of carbon dioxide released into the atmosphere can be reduced.
  • FIG. 16 is an enlarged view of main parts of a reducing agent supply system 200F according to a fifth modification.
  • the same components as those in the above-described embodiment are given the same reference numerals, and the description thereof will be omitted or simplified.
  • the reducing agent supply system 200F includes a stirring device (sedimentation prevention mechanism) 533.
  • the reducing agent supply system 200F includes a reducing agent supply line 21 and a control section C shown in FIG. 15.
  • the stirring device 533 includes an ejection pipe 533A and a carbon dioxide supply line 533B.
  • the ejection pipe 533A is provided to penetrate the base 32 so as to open at the bottom of the reducing agent tank 30.
  • three ejection pipes 533A are provided, but the configuration is not limited to this, and one, two, four or more ejection pipes 533A may be provided.
  • the carbon dioxide supply line 533B is provided so as to branch from a part of the carbon dioxide supply line 70 shown in FIG. 15 and connect to each of the ejection pipes 533A. Therefore, a portion of the carbon dioxide generated in the reduction tower 20 is sent from the carbon dioxide supply line 70 to each of the ejection pipes 533A via the carbon dioxide supply line 533B.
  • the carbon dioxide sent to the ejection pipe 533A is ejected into the reducing agent R from the bottom of the reducing agent tank 30. As a result, carbon dioxide bubbles rise from the bottom of the reducing agent tank 30, thereby stirring the reducing agent R. That is, the reducing agent R is stirred by bubbling the reducing agent R stored in the reducing agent tank 30 using carbon dioxide generated in the reducing tower 20 .
  • the reducing agent R can be appropriately supplied to the reduction tower 20. Furthermore, since the reducing agent R is stirred using the carbon dioxide generated in the reducing tower 20, a driving source for stirring the reducing agent R is not required, and the reducing agent supply system 200F can be operated efficiently. Note that in the fifth modification, the heating devices 133A and 133B of the first modification described above may be provided.
  • the oxidation tower 10 may be arranged inside the reduction tower 20.
  • the oxidation tower 10 and the reduction tower 20 are arranged separately, and there is a flow path for moving the metal oxide particles MO of the oxidation tower 10 to the reduction tower 20 and a flow path for moving the metal particles M of the reduction tower 20 to the oxidation tower 10.
  • a configuration in which a flow path is provided may also be used.

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Abstract

Le problème décrit par la présente invention est de fournir correctement un agent réducteur à une tour de réduction même si l'agent réducteur contient une teneur en solides pulvérulents ou granulaires. La solution selon l'invention porte sur un système d'alimentation en agent réducteur destiné à alimenter un agent réducteur pour réduire les particules d'oxyde métallique à une tour de réduction d'un système de réaction en boucle chimique qui comprend : une tour d'oxydation qui oxyde des particules métalliques pour obtenir des particules d'oxyde métallique ; une tour de réduction qui réduit les particules d'oxyde métallique pour obtenir des particules métalliques ; et une unité de circulation qui amène les particules métalliques et les particules d'oxyde métallique à circuler entre la tour de réduction et la tour d'oxydation. Le système d'alimentation en agent réducteur comprend : un réservoir d'agent réducteur qui stocke un agent réducteur ; un mécanisme de prévention de précipitation qui empêche la teneur en solides de l'agent réducteur dans le réservoir d'agent réducteur de précipiter ; et une conduite d'alimentation en agent réducteur qui relie le réservoir d'agent réducteur à la tour de réduction.
PCT/JP2023/018252 2022-06-03 2023-05-16 Système d'alimentation en agent réducteur, procédé d'alimentation en agent réducteur et système de réaction en boucle chimique Ceased WO2023234008A1 (fr)

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JP2024524314A JPWO2023234008A1 (fr) 2022-06-03 2023-05-16
CN202380034783.2A CN119032244A (zh) 2022-06-03 2023-05-16 还原剂供给系统、还原剂供给方法、及化学链反应系统
KR1020247035160A KR20250020392A (ko) 2022-06-03 2023-05-16 환원제 공급 시스템, 환원제 공급 방법 및 케미컬 루프 반응 시스템

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4894162A (en) * 1988-04-27 1990-01-16 Ciba-Geigy Corporation Treatment of volatile organic substances at waste water treatment plants
JPH02130312A (ja) * 1988-11-08 1990-05-18 Olympia Kogyo Kk 液状燃料燃焼装置
JP2004025001A (ja) * 2002-06-25 2004-01-29 Toshiba Corp 廃液処理装置
JP2007125492A (ja) * 2005-11-02 2007-05-24 Sharp Corp 廃棄物処理方法および廃棄物処理システム
JP2011513862A (ja) * 2008-03-03 2011-04-28 アルストム テクノロジー リミテッド ファジー論理制御及び最適化システム
JP2012172891A (ja) * 2011-02-21 2012-09-10 Tokyo Gas Co Ltd 反応塔の天面側から酸化剤およびまたは還元剤が供給されるケミカルループ燃焼装置
JP2018155437A (ja) * 2017-03-16 2018-10-04 学校法人幾徳学園 有機溶剤の処理方法、及び有機溶剤処理システム

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4894162A (en) * 1988-04-27 1990-01-16 Ciba-Geigy Corporation Treatment of volatile organic substances at waste water treatment plants
JPH02130312A (ja) * 1988-11-08 1990-05-18 Olympia Kogyo Kk 液状燃料燃焼装置
JP2004025001A (ja) * 2002-06-25 2004-01-29 Toshiba Corp 廃液処理装置
JP2007125492A (ja) * 2005-11-02 2007-05-24 Sharp Corp 廃棄物処理方法および廃棄物処理システム
JP2011513862A (ja) * 2008-03-03 2011-04-28 アルストム テクノロジー リミテッド ファジー論理制御及び最適化システム
JP2012172891A (ja) * 2011-02-21 2012-09-10 Tokyo Gas Co Ltd 反応塔の天面側から酸化剤およびまたは還元剤が供給されるケミカルループ燃焼装置
JP2018155437A (ja) * 2017-03-16 2018-10-04 学校法人幾徳学園 有機溶剤の処理方法、及び有機溶剤処理システム

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TW202348894A (zh) 2023-12-16

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