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WO2022190659A1 - Procédé de production de combustible et système de production de combustible - Google Patents

Procédé de production de combustible et système de production de combustible Download PDF

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Publication number
WO2022190659A1
WO2022190659A1 PCT/JP2022/001909 JP2022001909W WO2022190659A1 WO 2022190659 A1 WO2022190659 A1 WO 2022190659A1 JP 2022001909 W JP2022001909 W JP 2022001909W WO 2022190659 A1 WO2022190659 A1 WO 2022190659A1
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Prior art keywords
treated
fuel production
fuel
gas
catalyst
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Ceased
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English (en)
Japanese (ja)
Inventor
剛 伊藤
利正 大橋
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Hitachi Ltd
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Hitachi Ltd
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    • 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
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/12—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by dry-heat treatment only
    • 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
    • C08J11/04—Recovery or working-up of waste materials of polymers
    • C08J11/10—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation
    • C08J11/16—Recovery or working-up of waste materials of polymers by chemically breaking down the molecular chains of polymers or breaking of crosslinks, e.g. devulcanisation by treatment with inorganic material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/08—Production of synthetic natural gas

Definitions

  • the present invention relates to a fuel production method for producing fuel from an object to be treated that contains macromolecular organic matter, and a fuel production system to which this fuel production method is applied.
  • waste containing high-molecular organic matter has been treated by burning it at high temperatures.
  • waste resin such as ion exchange resin
  • the volume can be reduced to 1/10 or less.
  • the waste resin is an ion-exchange resin used in a nuclear power plant, it is necessary to recover radioactive substances scattered during combustion. Therefore, in the case of performing a process of burning at a high temperature exceeding 1000° C., the scale of processing equipment such as an off-gas system is increased.
  • CO 2 is generated when high-molecular weight organic matter is burned.
  • CO2 emissions There is a demand for reducing CO2 emissions from the viewpoint of environmental impact. Therefore, as one of the techniques for reducing CO 2 emissions, a technique for converting CO 2 into fuel such as methanol and methane has been proposed. For example, a method of synthesizing methanol by reacting a gas containing carbon monoxide, carbon dioxide, and hydrogen at 50 atm and 250° C. or lower using a copper-based catalyst has been proposed (e.g., See Patent Document 2).
  • Patent Document 1 does not describe the application of methanol synthesis from carbon dioxide to carbon dioxide generated by combustion of high-molecular weight organic matter.
  • the present invention it is possible to reduce the decomposition temperature of an object to be treated that contains high-molecular-weight organic substances and to produce fuel from the object-to-be-treated that contains high-molecular organic substances through a series of operations.
  • a fuel manufacturing method and a fuel manufacturing system are provided.
  • the fuel production method of the present invention is a method for producing fuel from an object to be treated that contains a high-molecular-weight organic substance, wherein the object to be treated contains an oxide semiconductor and a catalyst containing a metal that supplies electrons to the object to be treated. and a heating step of heating the object to be treated in contact with the catalyst in an atmosphere containing hydrogen and oxygen.
  • the fuel production system of the present invention produces fuel from an object to be treated containing macromolecular organic matter.
  • a reaction vessel containing an object to be treated, an oxide semiconductor, and a catalyst containing a metal that supplies electrons to the object to be treated, a heating device for heating the inside of the reaction vessel, and a gas containing hydrogen and oxygen into the reaction vessel. and a supply unit for supplying.
  • the reaction tank has an air supply port for supplying the gas containing hydrogen and oxygen supplied from the supply unit into the reaction tank, and an exhaust port for discharging the exhaust gas generated by the reaction of the object to be treated from the reaction tank.
  • a fuel production method capable of reducing the decomposition temperature of an object to be treated that contains high-molecular organic matter and producing fuel from the object to be treated that includes high-molecular organic matter through a series of operations;
  • a fuel production system can be provided.
  • FIG. 1 is a flow chart of a first embodiment of a fuel manufacturing method
  • 1 is a schematic configuration diagram of one embodiment of a fuel production system to which the fuel production method of which the flow chart is shown in FIG. 1 is applied
  • FIG. Fig. 2 is a flow chart of a second embodiment of a fuel manufacturing method
  • FIG. 4 is a schematic configuration diagram of one embodiment of a fuel production system that applies the fuel production method whose flow chart is shown in FIG. 3
  • 3 is a flow chart of a third embodiment of a fuel manufacturing method
  • FIG. 6 is a schematic configuration diagram of one embodiment of a fuel production system to which the fuel production method whose flow chart is shown in FIG. 5 is applied
  • 1 is a schematic configuration diagram of one form of a fuel production system using exhaust heat from a plant
  • the fuel production method is a method for producing fuel from an object to be treated containing macromolecular organic matter.
  • a catalyst containing an oxide semiconductor and a metal that supplies electrons to an object to be treated in the reaction mechanism of fuel production (hereinafter also simply referred to as a metal that supplies electrons) is brought into contact with the object to be treated. It has a contacting step.
  • the catalyst used in the contact step preferably contains a transition metal different from the electron-supplying metal (hereinafter also simply referred to as a transition metal) together with the oxide semiconductor and the electron-supplying metal.
  • the fuel production method has a heating step of heating the object to be treated with the catalyst in an atmosphere containing hydrogen and oxygen.
  • the fuel manufacturing system performs processing for manufacturing fuel from a processing object containing high-molecular organic matter.
  • the fuel production system includes a reaction vessel containing an object to be treated, an oxide semiconductor, and a catalyst containing a metal that supplies electrons, a heating device for heating the inside of the reaction vessel, and a gas containing hydrogen and oxygen into the reaction vessel. and a supply unit for supplying.
  • the reaction tank has an air supply port for supplying the gas containing hydrogen and oxygen supplied from the supply unit into the reaction tank, and an exhaust port for discharging the fuel gas generated by the reaction of the object to be treated from the reaction tank. , and a recovery facility for recovering the fuel gas.
  • examples of the target macromolecular organic matter include wastes containing various resins such as ion exchange resins and waste plastics.
  • the ion-exchange resin it is possible to apply an ion-exchange resin for water purification treatment or an ion-exchange resin for nuclear reactor plants.
  • the polymer organic material may be a mixture of different types of resins, such as a mixture of an ion exchange resin and other resins. It is desirable that substances other than organic substances (for example, high-melting point inorganic substances, etc.) be as small as possible in the target waste. Therefore, it is desirable to separate substances other than organic substances from organic substances before performing the heating step. However, the heating step may be performed in a state containing substances other than organic substances that could not be separated, and then the residues other than organic substances may be disposed of.
  • an oxide semiconductor with a bandgap of 2.0 eV or more can be used. Examples include TiO 2 , V 2 O 5 , Cr 2 O 3 , NiO, Fe 2 O 3 , Fe 3 O 4 , ZnO, SrTiO 3 and the like.
  • the oxide semiconductor one or more selected from these oxide semiconductors can be used.
  • holes excited in the oxide semiconductor by heat have sufficient oxidizing power and can oxidatively decompose the polymer.
  • an oxide semiconductor with a bandgap of 2.0 eV or more electrons excited in the oxide semiconductor by heat have a sufficient reducing power, and a metal or a transition metal that supplies electrons used as a catalyst can be used. can be recovered.
  • Ag is preferably used as the electron-supplying metal.
  • a metal that supplies electrons to an object to be treated as a catalyst supplies electrons to a functional group contained in a polymer organic substance that is an object to be treated.
  • decomposition of the functional group of the polymer by the electron-supplying metal is promoted.
  • the oxidative decomposition of the high-molecular-weight organic matter, which is the object to be treated can be promoted.
  • metals that supply electrons take oxygen from carbon monoxide (CO) and carbon dioxide (CO 2 ) produced by decomposition of polymers, promoting the production of methanol (CH 3 OH) and methane (CH 4 ). do.
  • the amount of the metal that supplies electrons is preferably 0.02-5 wt. %, more preferably 0.1-1 wt. %.
  • Transition metals different from metals that supply electrons include Ti, V, Cr, Mn, iron group elements (Fe, Co, Ni), platinum group elements (Ru, Rh, Pd, Os, Ir, Pt), It is preferable to use one or more selected from Cu and Au. Among them, it is more preferable to use Ag as the electron-supplying metal and Cu as the transition metal different from the electron-supplying metal.
  • the transition metal element receives electrons excited in the oxide semiconductor, suppresses the recombination of electrons and holes in the oxide semiconductor, and oxidizes the polymer by the holes. It can accelerate decomposition.
  • the transition metal removes electrons to further suppress the recombination of electrons and holes, thereby further promoting oxidative decomposition as compared with the case where a metal that supplies electrons is used alone.
  • the transition metal that has been reduced by receiving electrons takes oxygen from carbon monoxide (CO) and carbon dioxide (CO 2 ) generated by decomposition of the polymer, and converts it into methanol (CH 3 OH) and methane (CH 4 ). promote the generation of
  • the amount of the transition metal different from the electron-supplying metal is preferably 0.02-5 wt. %, more preferably 0.1-1 wt. %.
  • the atmosphere containing hydrogen for example, water vapor or hydrogen gas can be used.
  • the atmosphere containing oxygen for example, water vapor, oxygen gas, or air can be used.
  • the amount of hydrogen and oxygen to be supplied is preferably such that the total number of moles of hydrogen and oxygen is two times or more, particularly preferably four times or more, the number of moles of the object to be treated.
  • the rate of decomposition of the organic matter in the object to be treated is improved.
  • oxygen is supplied at a molar ratio of 2 times or more and hydrogen is supplied at a molar ratio of 4 times or more with respect to the object to be processed.
  • Examples of methods for bringing the object to be treated and the catalyst into contact include a method of mixing powders of oxide semiconductors, electron-supplying metals, and transition metals with the object to be treated. Further, there is a method of mixing particles of an oxide semiconductor, a metal that supplies electrons, and a transition metal with an object to be treated. Furthermore, there is a method of adding a solution of raw materials for an oxide semiconductor, a metal that supplies electrons, and a transition metal to an object to be treated, and heating the object to precipitate the oxide semiconductor, the metal that supplies electrons, and the transition metal. mentioned.
  • the oxide semiconductor, the electron-supplying metal, and the transition metal can also be brought into contact with the object to be treated in separate operations. For example, after mixing an oxide semiconductor powder with an object to be processed, a solution (aqueous solution or the like) containing a metal that supplies electrons and a transition metal is added. By depositing the metal that supplies electrons by heating and the transition metal, the catalyst can be brought into contact with the object to be treated.
  • a solution aqueous solution or the like
  • the above catalysts may be placed on the walls of the reaction vessel or stirred. A method is possible in which the catalyst is attached to a blade and the attached catalyst is brought into contact with the object to be treated.
  • the action of a catalyst containing an oxide semiconductor, a metal that supplies electrons, and a transition metal is estimated as follows.
  • the following explanation is a reaction mechanism assumed by the inventors in the expression of catalytic action, and the fuel production method according to the present embodiment is not limited to the following reaction mechanism.
  • h + generated by thermal excitation has a strong oxidizing power, and oxidatively decomposes the carbon chain of the polymer organic substance in contact with the oxide semiconductor.
  • the electron-supplying metal and the transition metal since the electron-supplying metal and the transition metal are present at the same time, the electron-supplying metal and the transition metal receive e ⁇ generated by the thermal excitation and prevent recombination of h + and e ⁇ . , promotes oxidative decomposition reactions.
  • the following formula (2) represents the case where a metal M is a metal that supplies electrons and a transition metal, and the metal M exists in the state of an oxide MO n .
  • the metal oxide MO n- ⁇ that receives e ⁇ generated by thermal excitation deprives CO and CO 2 generated by the oxidative decomposition of the high-molecular-weight organic matter as shown in the following formula (3), and converts active carbon C give rise to CO 2 +MO n ⁇ ⁇ C+MO n (3)
  • macromolecular organic substances contain not only carbon chains but also functional groups.
  • the decomposition of this functional group is accelerated by the supply of electrons. Electrons supplied from the oxide semiconductor by thermal excitation are consumed in the above equations (1) to (4). Therefore, by adding a metal that supplies electrons, the decomposition of the functional group can be promoted as shown in the following formula (5).
  • the functional group preferably contains sulfide. Polymeric organic substance (functional group) + e ⁇ ⁇ SO 4 +CO 2 +H 2 O (5) The CO 2 generated in the above formula (5) is supplied to the above formula (3), and by further producing active carbon, it becomes possible to produce fuels such as CH 3 OH and CH 4 according to the above formula (4).
  • the degree of reduction in the treatment temperature and the amount of heat generated vary depending on the type and amount of the oxide semiconductor used as the catalyst, the metal that supplies electrons, and the transition metal. can be processed.
  • Table 1 shows the difference in reaction temperature depending on the type of catalyst.
  • the treatment temperature can be lowered to about 250 ° C., which is higher than when TiO 2 or Fe 2 O 3 is used alone. Therefore, the reaction temperature can be greatly reduced.
  • lowering the treatment temperature it becomes possible to carry out the heating step at a temperature of 500°C or less, preferably in the range of 200°C to 500°C.
  • the object to be treated containing high-molecular weight organic matter is brought into contact with a catalyst containing an oxide semiconductor and a metal that supplies electrons. heating in an atmosphere containing As a result, the decomposition temperature of the object to be treated containing high-molecular organic matter can be reduced, and fuel can be produced from the object to be treated including high-molecular organic matter through a series of operations. Furthermore, by using a catalyst containing a transition metal in addition to the oxide semiconductor and the metal that supplies electrons as a catalyst, the decomposition temperature of the object to be treated containing high-molecular organic substances is further reduced, and the high-molecular organic substances are contained. Fuel can be efficiently produced from the object to be treated through a series of operations.
  • the treatment temperature can be lowered to, for example, about 280° C., particularly 250° C. or less, so that exhaust heat from external equipment such as a power plant can be used in the heating process.
  • the treatment temperature can be lowered, so that thermal decomposition can be achieved at a treatment temperature lower than the volatilization temperature of the radionuclide.
  • the volatilization temperature of radionuclides is, for example, about 300° C. for technetium (Tc), about 500° C. for cesium (Cs), and over 1000° C. for cobalt (Co).
  • the fuel production system includes a reaction tank containing the object to be treated and the catalyst, a heating device for heating the inside of the reaction tank, and a supply unit for supplying a gas containing hydrogen and oxygen to the reaction tank.
  • the reaction tank has an air supply port for supplying the gas containing hydrogen and oxygen supplied from the supply unit into the reaction tank.
  • a catalyst containing an oxide semiconductor and a metal that supplies electrons, or a catalyst containing a transition metal in these is brought into contact with the object to be treated, so that hydrogen and oxygen from the supply part are included.
  • a gas is supplied into the reactor from the air supply port.
  • FIG. 1 A flow chart of a first embodiment of a fuel manufacturing method is shown in FIG.
  • an object to be treated 101 containing a polymeric organic substance and a catalyst 102 containing an oxide semiconductor and a metal that supplies electrons are prepared.
  • the catalyst preferably contains a transition metal in addition to the oxide semiconductor and the electron-supplying metal.
  • the oxide semiconductor used for the catalyst 102 the above-described oxide semiconductor (for example, TiO 2 or the like) is used.
  • a solution (aqueous solution or other solution) containing Ag or the like is used as the metal for supplying electrons used in the catalyst 102 .
  • a solution (aqueous solution or other solution) containing the transition metal for example, Cu, Fe, etc.
  • step S1 the catalyst 102 is brought into contact with the processing object 101 by supplying the processing object 101 with the catalyst 102 and mixing the processing object 101 and the catalyst 102 together.
  • step S2 the atmosphere gas 103 is supplied to the object 101 to be processed which is brought into contact with the catalyst 102 .
  • the atmosphere gas 103 the above-described gas containing hydrogen and oxygen (for example, a mixed gas of water vapor, hydrogen, and oxygen) is used.
  • the object to be treated 101 in contact with the catalyst 102 is placed in the atmospheric gas 103 .
  • step S3 the processing object 101 brought into contact with the catalyst 102 in the atmosphere gas 103 is heated.
  • the object 101 to be treated is decomposed into a solid residue 104 and a gaseous exhaust gas 105 containing fuel components (CH 3 OH, CH 4 ).
  • the object 101 to be treated is brought into contact with the catalyst 102 , and then the object 101 to be treated is heated in the atmosphere gas 103 .
  • the decomposition temperature of the object to be treated containing high-molecular organic matter can be reduced, and fuel can be produced from the object to be treated including high-molecular organic matter through a series of operations.
  • FIG. 2 shows a schematic configuration diagram of one form of a fuel production system to which the fuel production method whose flow chart is shown in FIG. 1 is applied.
  • the fuel production system shown in FIG. 2 includes a reaction tank 6, a heating device 4, and a recovery device 8.
  • the reaction tank 6 has an air supply port 5 and an exhaust port 7. As shown in FIG.
  • the reaction tank 6 accommodates an object to be treated (including high-molecular organic matter such as resin) 2 and a catalyst 1 .
  • the air supply port 5 is provided on the lower surface of the reaction vessel 6
  • the exhaust port 7 is provided on the upper surface of the reaction vessel 6 .
  • a supply unit 3 for supplying gas containing hydrogen and oxygen is connected to the air supply port 5 .
  • Specific configurations of the supply unit 3 include, for example, a vaporizer for generating steam, a gas cylinder (hydrogen cylinder, oxygen cylinder, etc.), a compressor for supplying air, a gas purification device, and the like. Then, the gas supply port 5 supplies the gas containing hydrogen and oxygen supplied from the supply unit 3 into the reaction vessel 6 .
  • the heating device 4 heats the inside of the reaction tank 6 by heating the gas containing hydrogen and oxygen supplied from the supply unit 3 . Thereby, the heating device 4 heats the processing object 2 accommodated in the reaction tank 6, and causes the processing object 2 to react with the atmospheric gas and decompose.
  • fuel can be produced as described below.
  • a catalyst 1 containing an oxide semiconductor and a metal that supplies electrons, or a catalyst 1 containing a transition metal together with these, and an object to be treated containing a high-molecular organic substance are placed in a reaction vessel 6 in advance. It contains thing 2.
  • the inside of the reaction vessel 6 is heated.
  • the inside of the reaction tank 6 is heated by heating the supplied gas with the heating device 4 while supplying the gas containing hydrogen and oxygen into the reaction tank 6 from the air supply port 5 .
  • the object to be treated 2 is decomposed by reacting with hydrogen and oxygen, and a residue and an exhaust gas, which is a gas containing fuel components (CH 3 OH, CH 4 ), are generated.
  • Exhaust gas generated by the reaction of the object 2 during heating is discharged from the exhaust port 7 .
  • Exhaust gas, which is a gas containing fuel components, discharged from the exhaust port 7 is recovered by a recovery device 8 . After heating is completed, the residue (and catalyst 1) remaining in the reactor 6 is removed.
  • the fuel production system can produce fuel as described above.
  • a catalyst 1 containing an oxide semiconductor and a metal that supplies electrons, or a catalyst 1 containing a transition metal together with these, and an object to be processed containing a high-molecular organic substance are placed in the reaction tank 6. 2 is housed again and heated.
  • the catalyst 1 and the object 2 to be treated containing high-molecular organic matter are placed in advance in the reaction tank 6, so that the catalyst 1 and the object 2 to be treated are brought into contact with each other. can be done.
  • the fuel production system is provided with an air supply port 5, a gas containing hydrogen and oxygen is supplied from the air supply port 5, and the object 2 to be processed contained in the reaction tank 6 is caused to react with hydrogen and oxygen. be able to.
  • the fuel production system is provided with the heating device 4, it is possible to heat and decompose the object to be treated 2 contained in the reaction tank 6.
  • the fuel production system includes the exhaust port 7 and the recovery device 8 , the exhaust gas generated by heating can be discharged from the exhaust port 7 to the outside of the reaction tank 6 and recovered by the recovery device 8 . . Then, in the reaction tank 6 , the catalyst 1 and the object 2 to be treated containing high-molecular-weight organic substances are heated by the heating device 4 while being in contact with each other in an atmosphere containing hydrogen and oxygen. As a result, the decomposition temperature of the processing object 2 containing high-molecular organic matter can be reduced, and fuel can be produced from the processing object 2 containing high-molecular organic matter through a series of operations.
  • FIG. 3 A flow chart of a second embodiment of the fuel manufacturing method is shown in FIG. As shown in FIG. 3, in the second embodiment, the residue 104 generated in the heating step of step S3 is separated from the fuel production method of the first embodiment shown in FIG. 102 is recovered. It should be noted that redundant description of the same configuration as in the first embodiment will be omitted.
  • a step (solid separation step) of solid separation of the residue 104 in step S4 is performed to separate the incombustible waste 106 and the catalyst 107 .
  • the catalyst 107 obtained in the solid separation step of step S4 is recovered and supplied to the object 101 to be treated in the same manner as the catalyst 102 supplied first.
  • the non-combustible waste 106 is disposed of.
  • the particle-shaped catalyst 107 and the catalyst 102 are used in order to perform the step of solid separation of the residue 104 in step S4. Then, a sieve or the like having openings smaller than the particles of the catalyst 107 and the catalyst 102 is used to separate the residue 104 in step S4 into solids.
  • the catalyst 102 is brought into contact with the object 101 to be treated, and the object 101 is heated in an atmosphere containing hydrogen and oxygen. to heat. This makes it possible to decompose the object 101 to be treated at a significantly lower temperature than in the conventional combustion method, and to produce fuel from the object to be treated including macromolecular organic matter through a series of operations. can.
  • step S4 the step of separating the residue 104 into solids in step S4 is performed to separate the incombustible waste 106 and the catalyst 107, and the obtained catalyst 107 is recovered and treated.
  • the object 101 is supplied. Since the catalyst 107 is recovered and reused in this manner, the amount of the catalyst 102 used can be reduced.
  • FIG. 4 shows a schematic configuration diagram of one embodiment of a fuel production system to which the fuel production method whose flow chart is shown in FIG. 3 is applied.
  • the fuel production system shown in FIG. 4 further differs from the fuel production system shown in FIG. 2 in that a stirrer 9, a stirring blade 10, an inlet 11 and an outlet 12 are provided.
  • a stirring blade 10 is provided in the reaction vessel 6 .
  • the agitating blade 10 agitates the catalyst 1 and the object 2 to be treated by rotating a shaft powered by the agitator 9 .
  • the discharge port 12 is provided at the bottom inside the reaction tank 6 .
  • the outlet 12 has separation equipment such as a sieve with openings smaller than the particles of the catalyst 1 . Separation equipment such as this sieve can separate the catalyst 1 from the incombustible wastes in which the objects to be treated are decomposed. The non-combustible waste passes through openings in the separation equipment and is discharged from outlet 12 .
  • the inlet 11 is provided on the upper surface of the reaction vessel 6 . Since the incombustible waste is discharged from the discharge port 12, a new processing object 2 can be added from the input port 11, and the processing object 2 can be heated and decomposed. Since other configurations are the same as those of the fuel production system shown in FIG. 2, redundant description will be omitted.
  • the incombustible waste generated by the decomposition of the object 2 to be treated is separated. It can be discharged separately from the catalyst 1 .
  • the inlet 11 is provided on the upper surface of the reaction tank 6 , a new processing object 2 can be additionally introduced through the inlet 11 .
  • the stirring blades 10 are provided in the reaction vessel 6, by stirring with the stirring blades 10, it is possible to maintain the contact between the object to be treated 2 added from the inlet 11 and the catalyst 1. can.
  • the object 2 to be treated can be added and the contact between the object 2 to be treated and the catalyst 1 can be maintained, and the object 2 to be treated can be continuously fed. can be processed.
  • the catalyst 1 can be separated from the non-combustible waste by the separation equipment of the discharge port 12, and the catalyst 1 can be continuously used while the object 2 to be treated is continuously treated. . Therefore, the amount of catalyst 1 used can be reduced.
  • the catalyst can be applied to the inner wall of the reaction tank 6 or the stirring blade 10 and the catalyst can be used continuously. .
  • this catalyst if the catalyst decreases due to abrasion or the like, the catalyst is applied again to the inner wall of the reaction tank 6 and the stirring blade 10 to replenish the catalyst.
  • this configuration for imparting the catalyst can be applied to the fuel production system of FIG. 2 for batch processing, or applied to the fuel production system of FIG. 4 for continuous processing.
  • FIG. 5 A flow chart of a third embodiment of the fuel production method is shown in FIG. As shown in FIG. 5, the third embodiment separates the exhaust gas 105 generated in the heating process of step S3 in contrast to the fuel production method of the first embodiment shown in FIG. It should be noted that redundant description of the same configuration as in the first embodiment will be omitted.
  • a step (gas separation step) of gas separation of the exhaust gas 105 in step S5 is performed, and the exhaust gas 105 is separated into the fuel gas 109 (CH 4 OH, CH 4 ) and the non-fuel gas 110 ( H 2 O, CO 2 , SO x , NO x ).
  • the non-fuel gas 110 contained in the exhaust gas 105 is removed in order to reduce the impurities mixed in when the fuel gas 109 is recovered.
  • H2O is separated through a hygroscopic material, and CO2 , SOx , NOx are removed through an alkali trap. This reduces the non-fuel gas concentration in the recovered fuel gas.
  • the catalyst 102 is brought into contact with the object 101 to be treated, and the object 101 is heated in an atmosphere containing hydrogen and oxygen. to heat.
  • the generated exhaust gas 105 is separated into the fuel gas 109 and the non-fuel gas 110 by the step of gas separation of the exhaust gas 105 in step S5, and the purity of the recovered fuel gas is can increase
  • FIG. 6 shows a schematic configuration diagram of one embodiment of a fuel production system to which the fuel production method whose flow chart is shown in FIG. 5 is applied.
  • the fuel production system shown in FIG. 6 further differs from the fuel production system shown in FIG. 2 in that a trap 13 connected to the exhaust port 7 on the upper surface of the reaction vessel 6 is provided.
  • the trap 13 is arranged between the exhaust port 7 of the reaction vessel 6 and the recovery device 8 .
  • the trap 13 has a hygroscopic agent inside, and causes water vapor (H 2 O) in the exhaust gas from the exhaust port 7 to react with the hygroscopic agent.
  • the trap 13 removes water vapor from the exhaust gas and suppresses the discharge of the water vapor to the outside.
  • the trap 13 has an alkaline compound inside, and causes acid gases (CO 2 , SO x , NO x ) in the exhaust gas from the exhaust port 7 to react with the alkaline compound.
  • the trap 13 converts the acid gas into a salt or an aqueous salt solution, etc., and suppresses the gas from being discharged to the outside.
  • the hygroscopic agent and alkaline compound that have disappeared due to the reaction are replenished to the trap 13 as necessary. Since other configurations are the same as those of the fuel production system shown in FIG. 2, redundant description will be omitted.
  • the trap 13 connected to the exhaust port 7 on the upper surface of the reaction tank 6 is provided, so that the water vapor and acid gas in the exhaust gas are discharged to the outside as gas. can be suppressed.
  • FIG. 7 shows a schematic configuration diagram of one mode of a fuel production system for a fourth embodiment of the fuel production method.
  • the fuel production system shown in FIG. 7 shows a schematic configuration of one form of the fuel production system in the case of utilizing the waste heat of the plant.
  • the fuel production system shown in FIG. 7 further includes heat exchangers 14 and 15 as compared with the fuel production systems shown in FIGS. Also, the fuel production system shown in FIG. 7 is connected to the plant 16 .
  • the heat exchanger 14 is connected to the exhaust port 7 on the upper surface of the reaction vessel 6 . Also, the heat exchanger 14 is connected to the air supply port 5 on the bottom surface of the reaction vessel 6 . A gas containing hydrogen and oxygen is supplied to the heat exchanger 14 from the lower side in the figure. A gas containing hydrogen and oxygen is supplied to the air supply port 5 on the bottom surface of the reaction tank 6 through the heat exchanger 14 . Exhaust gas is supplied to the heat exchanger 14 from the exhaust port 7 . The exhaust gas passes through the heat exchanger 14 , is discharged from the heat exchanger 14 to the right side in the figure, passes through the trap 13 and is recovered by the recovery device 8 .
  • the heat exchanger 14 is composed of separate pipes so that the gas flow path containing hydrogen and oxygen and the exhaust gas flow path do not mix with each other. Also, the heat exchanger 14 is configured such that the contact area between the two tubes is large so that heat can be exchanged between the exhaust gas and the gas containing hydrogen and oxygen.
  • the heat exchanger 15 is connected to the air supply port 5 on the lower surface of the reaction vessel 6 on the upstream side (supply section 3 side) of the heat exchanger 14 .
  • the heat exchanger 15 is also connected to a plant 16 outside the fuel production system.
  • a gas containing hydrogen and oxygen is supplied to the heat exchanger 15 from the lower side in the drawing.
  • a gas containing hydrogen and oxygen is supplied to the air supply port 5 on the bottom surface of the reaction tank 6 through the heat exchanger 15 .
  • the heat exchanger 15 is also connected to a high-temperature exhaust system 18 of the plant 16 , and high-temperature exhaust gas is supplied from the high-temperature exhaust system 18 to the heat exchanger 15 as a heat medium.
  • the high temperature exhaust passes through the heat exchanger 15 and is discharged to the outside of the fuel production system.
  • the heat exchanger 15 is composed of separate tubes so that the gas flow path containing hydrogen and oxygen and the heat medium flow path supplied from the outside of the plant 16 or the like do not mix with each other. Also, the heat exchanger 15 is configured such that the two tubes have a large contact area so that heat can be exchanged between the high-temperature heat medium and the gas containing hydrogen and oxygen.
  • the air supply port 5 is connected to the supply unit 3 for supplying gas containing hydrogen and oxygen and to the steam discharge device 17 of the plant 16 .
  • the supply unit 3 and the steam discharge device 17 of the plant 16 are joined upstream of the heat exchangers 14 and 15 and connected to the air supply port 5 .
  • the steam discharge device 17 supplies the preheated steam generated in the plant 16 into the reaction vessel 6 from the air supply port 5 as part of the gas containing hydrogen and oxygen.
  • the supply unit 3 of the fuel production system reacts not only the above-mentioned gas cylinder, compressor, gas purification device, etc., but also the gas introduced from the outside of the fuel production system as part of the gas containing hydrogen and oxygen. It can be fed into tank 6 . Since other configurations are the same as those of the fuel production system shown in FIG. 2, redundant description will be omitted.
  • the atmospheric gas supplied to the air supply port 5 is heat-exchanged with the exhaust gas from the exhaust port 7 and the high-temperature exhaust gas from the high-temperature exhaust device 18. can be heated with Therefore, in this fuel production system, the energy applied from the heating device 4 can be reduced.
  • the steam discharged from the steam discharge device 17 can be used as part of the atmospheric gas supplied from the supply unit 3 into the reaction tank 6 . Therefore, in this fuel production system, the energy used to generate steam in the supply section 3 can be reduced.
  • each embodiment from the second embodiment to the fourth embodiment described above is the configuration of a plurality of embodiments as long as it does not cause problems in the fuel production process and the operation of the fuel production system. can be combined as appropriate.

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  • Chemical Kinetics & Catalysis (AREA)
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  • Health & Medical Sciences (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Sustainable Development (AREA)
  • Engineering & Computer Science (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Separation, Recovery Or Treatment Of Waste Materials Containing Plastics (AREA)
  • Liquid Carbonaceous Fuels (AREA)

Abstract

L'invention concerne un procédé de production d'un combustible à partir d'un objet à traiter contenant un matériau organique polymère. Le procédé comprend : une étape de contact pour mettre un catalyseur, qui comprend un semi-conducteur d'oxyde et un métal fournissant des électrons à l'objet à traiter, en contact avec l'objet à traiter ; et une étape de chauffage pour chauffer l'objet à traiter, qui a été mis en contact avec le catalyseur, dans une atmosphère qui contient de l'hydrogène et de l'oxygène. Le procédé de production de combustible permet de produire un combustible, par l'intermédiaire d'une série d'opérations, à partir d'un objet à traiter contenant un matériau organique polymère ; et une réduction de la température de décomposition de l'objet à traiter contenant un matériau organique polymère.
PCT/JP2022/001909 2021-03-09 2022-01-20 Procédé de production de combustible et système de production de combustible Ceased WO2022190659A1 (fr)

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JP2021037295A JP2022137689A (ja) 2021-03-09 2021-03-09 燃料製造方法および燃料製造システム
JP2021-037295 2021-03-09

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000103602A (ja) * 1998-09-30 2000-04-11 Toshiba Corp 水素の製造方法及び樹脂類の燃料化方法
JP2009513466A (ja) * 2005-10-31 2009-04-02 エレクトロファック アクチェンゲゼルシャフト 水素の製造方法の使用
JP2016159190A (ja) * 2015-02-26 2016-09-05 Ｊｆｅエンジニアリング株式会社 有害低密度廃棄物処理方法及び有害低密度廃棄物処理装置
JP2020185513A (ja) * 2019-05-10 2020-11-19 国立大学法人東北大学 固体触媒およびその製造方法、油状物の製造方法
WO2021192034A1 (fr) * 2020-03-24 2021-09-30 株式会社日立製作所 Procédé de réduction de volume pour déchets, dispositif de réduction de volume pour déchets

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2000103602A (ja) * 1998-09-30 2000-04-11 Toshiba Corp 水素の製造方法及び樹脂類の燃料化方法
JP2009513466A (ja) * 2005-10-31 2009-04-02 エレクトロファック アクチェンゲゼルシャフト 水素の製造方法の使用
JP2016159190A (ja) * 2015-02-26 2016-09-05 Ｊｆｅエンジニアリング株式会社 有害低密度廃棄物処理方法及び有害低密度廃棄物処理装置
JP2020185513A (ja) * 2019-05-10 2020-11-19 国立大学法人東北大学 固体触媒およびその製造方法、油状物の製造方法
WO2021192034A1 (fr) * 2020-03-24 2021-09-30 株式会社日立製作所 Procédé de réduction de volume pour déchets, dispositif de réduction de volume pour déchets

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