WO2013125000A1 - Appareil de transport de chaleur, et procédé de transport de chaleur - Google Patents

Appareil de transport de chaleur, et procédé de transport de chaleur Download PDF

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Publication number
WO2013125000A1
WO2013125000A1 PCT/JP2012/054360 JP2012054360W WO2013125000A1 WO 2013125000 A1 WO2013125000 A1 WO 2013125000A1 JP 2012054360 W JP2012054360 W JP 2012054360W WO 2013125000 A1 WO2013125000 A1 WO 2013125000A1
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Prior art keywords
nitrous oxide
decomposition
gas
catalyst
refrigerant
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PCT/JP2012/054360
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English (en)
Japanese (ja)
Inventor
茂広 茶圓
川口　淳一郎
宏人 羽生
理嗣 曽根
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昭和電工株式会社
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Priority to PCT/JP2012/054360 priority Critical patent/WO2013125000A1/fr
Publication of WO2013125000A1 publication Critical patent/WO2013125000A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
    • B01D53/8631—Processes characterised by a specific device
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B15/00—Sorption machines, plants or systems, operating continuously, e.g. absorption type
    • F25B15/02—Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B27/00—Machines, plants or systems, using particular sources of energy
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/10—Noble metals or compounds thereof
    • B01D2255/102—Platinum group metals
    • B01D2255/1025—Rhodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/204—Alkaline earth metals
    • B01D2255/2047—Magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/20—Metals or compounds thereof
    • B01D2255/209—Other metals
    • B01D2255/2092—Aluminium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2255/00—Catalysts
    • B01D2255/40—Mixed oxides
    • B01D2255/405—Spinels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/402—Dinitrogen oxide
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25B—REFRIGERATION MACHINES, PLANTS OR SYSTEMS; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS
    • F25B2333/00—Details of boilers; Analysers; Rectifiers
    • F25B2333/003—Details of boilers; Analysers; Rectifiers the generator or boiler is heated by combustion gas
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/10—Capture or disposal of greenhouse gases of nitrous oxide (N2O)

Definitions

  • the present invention relates to a heat transport apparatus and a heat transport method using energy generated by decomposition of nitrous oxide (also referred to as N 2 O, dinitrogen monoxide).
  • nitrous oxide also referred to as N 2 O, dinitrogen monoxide
  • Japanese Patent Laid-Open No. 5-4027 Japanese Patent Laying-Open No. 2005-230795 JP 2006-181570 A Japanese Patent No. 4232820
  • heating including heating, hot water supply, hot water, drying, etc.
  • cooling including cooling, refrigeration, freezing, cold water, ice making, etc.
  • dehumidification and humidification
  • nitrous oxide as energy friendly to the global environment by using energy generated by decomposition of nitrous oxide.
  • Nitrous oxide is chemically stable and easy to handle, and is approved as a food additive (Ministry of Health, Labor and Welfare No. 34, March 22, 2005). It is also used as a combustion aid.
  • nitrous oxide is considered to be one of the causes of global warming as a greenhouse gas having a warming effect about 310 times that of carbon dioxide (CO 2 ).
  • CO 2 carbon dioxide
  • many technologies have been developed to decompose and remove nitrous oxide in exhaust gas discharged from, for example, factories, incineration facilities, and automobiles using catalysts. (For example, see Patent Documents 1 to 3.)
  • Patent Documents 1 and 2 disclose a technique in which heat generated during decomposition of nitrous oxide in the production process of adipic acid is used for preheating nitrous oxide.
  • Patent Document 3 described above in an apparatus for decomposing nitrous oxide contained in excess anesthetic gas, heat exchange is performed between a gas introduced into the decomposition apparatus and a gas discharged from the decomposition apparatus. Discloses a technique for increasing energy efficiency by reducing heating energy and cooling energy.
  • Patent Document 4 a thruster device that generates thrust by using a cracked gas obtained by catalytically decomposing nitrous oxide.
  • nitrous oxide when nitrous oxide is decomposed using a catalyst for decomposing nitrous oxide, additional nitrous oxide may be self-decomposed (thermal decomposition) by the heat of decomposition. Is possible.
  • the object of the present invention is to enable the use of nitrous oxide as energy friendly to the global environment, and to enable heat transport using the energy generated by the decomposition of this nitrous oxide. It is to provide a transport device and a heat transport method.
  • the present invention provides the following means. (1) a refrigerant circulation system in which the refrigerant circulates; An absorption liquid circulation system that is connected to the refrigerant circulation system and in which an absorption liquid that absorbs the refrigerant circulates; A condensing part for releasing heat from the refrigerant while condensing the refrigerant in the refrigerant circulation system; An evaporation unit that absorbs heat while evaporating the refrigerant in the refrigerant circulation system; An absorption part for absorbing the evaporated refrigerant into the absorption liquid in the absorption liquid circulation system; A regenerator that evaporates the absorbed refrigerant from the absorption liquid in the absorption liquid circulation system, The regenerator is provided with a heating means for heating the absorption liquid, and the heating means heats by the decomposition heat generated by the decomposition of nitrous oxide.
  • a concentration adjusting means for adjusting the concentration of nitrous oxide gas supplied to the decomposition reaction section is provided, The heat transport device according to (2) or (3) above, wherein the temperature of the cracked gas is controlled by adjusting the concentration of nitrous oxide gas supplied to the cracking reaction section.
  • a temperature measuring means for measuring the temperature of the nitrous oxide decomposition catalyst or decomposition gas is provided, The flow rate adjustment by the flow rate adjustment unit or the concentration adjustment by the concentration adjustment unit is performed based on the measurement result by the temperature measurement unit, or any one of the above items (3) to (5), Heat transport equipment.
  • (7) comprising preheating means for preheating the nitrous oxide decomposition catalyst, 7.
  • the heat transport device according to any one of the above items (2) to (6), wherein the nitrous oxide decomposition catalyst is preheated before the decomposition of the nitrous oxide is started.
  • (8) comprising nitrogen gas supply means for supplying nitrogen gas to the decomposition reaction section;
  • the heat transport according to any one of (2) to (7) above, wherein after the supply of nitrous oxide gas to the decomposition reaction section is stopped, nitrogen gas is supplied to the decomposition reaction section. apparatus.
  • the condensing part and / or the absorbing part is provided with a cooling means for cooling the refrigerant and / or the absorbing liquid, and the cooling means performs cooling by cooling heat accompanying adiabatic expansion of nitrous oxide.
  • the heat transport device according to any one of the above items (2) to (8), wherein: (10) The preceding paragraph, comprising a high-pressure gas container filled with the nitrous oxide, and supplying the nitrous oxide gas discharged from the high-pressure gas container and adiabatically expanded to the condensing unit and / or the absorbing unit The heat transport device according to (9).
  • (11) a first supply line that supplies nitrous oxide gas obtained by adiabatic expansion of the nitrous oxide to the condensing unit and / or the absorption unit; A second supply line for supplying nitrous oxide gas discharged from the condensing unit and / or the absorption unit to the decomposition reaction unit; A third supply line that supplies a nitrous oxide decomposition gas obtained by decomposing the nitrous oxide gas in the decomposition reaction section to the regeneration section. (10) Heat transport equipment.
  • the nitrous oxide gas is supplied to a decomposition reaction section where the nitrous oxide decomposition catalyst is arranged, and the nitrous oxide gas is used in the decomposition reaction section using the nitrous oxide decomposition catalyst.
  • the heat transport method according to item (12) wherein decomposition of nitrous oxide gas supplied thereafter is continued by decomposition heat generated by decomposition of the nitrous oxide gas.
  • the heat transport method according to (13), wherein the decomposition of the nitrous oxide gas is continuously performed by controlling the temperature of the decomposition gas.
  • the heat transport method according to (14), wherein the temperature of the cracked gas is controlled by adjusting the flow rate of the nitrous oxide gas.
  • the nitrous oxide gas obtained by adiabatic expansion of the nitrous oxide after cooling the refrigerant in the condensation and / or absorption step, the nitrous oxide gas is converted into a nitrous oxide decomposition catalyst.
  • the absorption liquid is heated in the regeneration step using the nitrous oxide decomposition gas obtained by decomposing using nitrous oxide and decomposing the nitrous oxide gas. Heat transport method.
  • nitrous oxide As described above, according to the present invention, it is possible to use nitrous oxide as energy friendly to the global environment, and it is possible to perform heat transport using energy generated by decomposition of this nitrous oxide. It is.
  • FIG. 1 It is a schematic diagram for demonstrating the heat transport apparatus and heat transport method to which this invention is applied. It is a schematic block diagram which shows the characterizing part of this invention with which the heat transport apparatus shown in FIG. 1 is provided. It is process drawing of the heat transport method using the heat transport apparatus shown in FIG. It is a flowchart which shows an example of the specific operation
  • a heat transport apparatus and a heat transport method to which the present invention is applied use substituting energy generated by the decomposition of nitrous oxide (N 2 O, also referred to as dinitrogen monoxide) as sub-environment-friendly energy.
  • Nitrogen oxide can be used.
  • Nitrous oxide is a stable gas at normal temperature and atmospheric pressure.
  • the temperature is about 500 ° C. or higher, self-decomposition (thermal decomposition) occurs while generating heat.
  • decomposition of nitrous oxide is accompanied by exotherm (exothermic reaction).
  • the decomposition gas of the nitrous oxide heated up by the temperature rise (heat of decomposition) accompanying this decomposition becomes about 1600 degreeC, it can be said that nitrous oxide is a substance with built-in high energy.
  • the decomposition start temperature can be lowered to, for example, about 350 to 400 ° C.
  • disassembly of nitrous oxide it is possible to carry out decomposition
  • the nitrous oxide decomposed using the catalyst becomes a mixed gas (decomposed gas) of nitrogen (N 2 ) and oxygen (O 2 ) while generating heat.
  • FIG. 1 is a schematic system diagram showing a configuration of a heat transport apparatus to which the present invention is applied.
  • This heat transport device is an absorption heat pump 100 that performs heat transport using heat of decomposition generated by decomposition of nitrous oxide (N 2 O).
  • the absorption heat pump 100 shown in FIG. 1 is connected to the refrigerant circulation system 101 through which the refrigerant R circulates, and the absorption liquid through which the absorption liquid A that absorbs the refrigerant R circulates. While condensing the circulation system 102, the refrigerant R in the refrigerant circulation system 101, the condensing part 103 that releases heat from the refrigerant R, and evaporating the refrigerant R in the refrigerant circulation system 101, heat is supplied to the refrigerant R.
  • the refrigerant circulation system 101 includes first to fourth pipes (flow paths) 107a to 107d in which the condensing unit 103, the evaporation unit 104, the absorption unit 105, and the regeneration unit 106 are connected in order.
  • the refrigerant R serves as a heat medium for transporting heat, and this refrigerant circulation system 101 repeats absorption into the absorption liquid A, evaporation from the absorption liquid A, and heat absorption and heat release accompanying state changes (vaporization and liquefaction). It will circulate inside.
  • water is used as the refrigerant R.
  • the absorbent circulation system 102 includes fourth and fifth pipes (flow paths) 107d and 107e that are connected in order between the absorption unit 105 and the regeneration unit 106.
  • the fourth pipe 107d is a common pipe constituting the refrigerant circulation system 101 and the absorbing liquid circulation system 102.
  • the absorption liquid A circulates in the absorption liquid circulation system 102 while repeating the absorption of the refrigerant R and the evaporation of the refrigerant R.
  • an aqueous solution of lithium bromide (LiBr) having a high water absorbability is used as such an absorbing liquid A.
  • the condensing unit 103 includes a condensing chamber 103a to which a first pipe 107a and a second pipe 107b are connected, and a condenser (condenser) 103b disposed inside the condensing chamber 103a. Further, the condenser 103b is thermally connected to an external radiator (cooling tower, outdoor unit) 108 as a heat exchanger on the heat radiation (high temperature) side. Specifically, a heat pipe 109 is routed between the condenser 103b (inside the condensing chamber 103a) and the radiator 108 (outside the condensing chamber 103a). It is a mechanism for passing (circulating) liquid. For example, water can be used as the coolant W.
  • the condensing unit 103 when the refrigerant (water vapor) R evaporated (vaporized) in the regenerating unit 106 is supplied to the condensing chamber 103a through the first pipe 107a, the condensing unit 103 communicates with the condenser 103b. Heat is released from the refrigerant R by heat exchange (contact with the heat pipe 109). Thus, the refrigerant R is condensed (cooled) to become liquid (water), and is sent from the condensation chamber 103a to the evaporation unit 104 through the second pipe 107b.
  • the condenser unit 103 after the heat released from the refrigerant R is absorbed in the cooling liquid W flowing through the heat pipe 109 (endothermic), is released as hot air T H from the radiator 108 by heat exchange with the outside .
  • the radiator 108 the fan has (blowing means) 108a is provided, while driving the fan 108a, it is possible to efficiently release the hot air T H to the outside.
  • the radiator 108 can be used as a heater (heating means).
  • heating, hot water supply, warm water, drying, etc. can be mentioned, for example.
  • the evaporation unit 104 includes an evaporation chamber 104a to which the second pipe 107b and the third pipe 107c are connected, and an evaporator (evaporator) 104b disposed inside the evaporation chamber 104a. Further, the inside of the evaporation chamber 104a is decompressed and is in a state close to a vacuum (a state in which the refrigerant R is easily evaporated (vaporized)). On the other hand, the evaporator 104b is thermally connected to an external heat absorber (air conditioner, indoor unit) 110 as a heat exchanger on the endothermic (low temperature) side.
  • an external heat absorber air conditioner, indoor unit
  • a heat pipe 111 is routed between the evaporator 104b (inside of the evaporation chamber 104a) and the heat absorber 110 (outside of the evaporation chamber 104a). It is a mechanism for passing (circulating) liquid.
  • water can be used as the coolant C.
  • the evaporation unit 104 when the refrigerant (water) R condensed (liquefied) in the condensing unit 103 is supplied to the evaporation chamber 104a through the second pipe 107b, the evaporation unit 104b is connected to the evaporator 104b. Heat is absorbed by the refrigerant R by heat exchange (contact with the heat pipe 111).
  • the refrigerant R dripped from the second pipe 107b is easily evaporated (vaporized) by contacting the heat pipe 111.
  • the refrigerant R becomes gas (water vapor) and is sent from the evaporation chamber 104a to the absorber 105 through the third pipe 107c.
  • the coolant C flowing in the heat pipe 109 is cooled by the heat of vaporization when the refrigerant R evaporates, and then discharged from the heat absorber 110 as the cool air TL by heat exchange with the outside.
  • the heat absorber 110 is provided with a fan (air blowing means) 110a, and the cool air TL can be efficiently discharged to the outside while driving the fan 110a.
  • the evaporating unit 104 can perform cooling using the cool air TL discharged from the heat absorber 110. That is, the heat absorber 110 can be used as a cooler (cooling means). Examples of the application field of cooling include cooling, refrigeration, freezing, cold water, and ice making.
  • the absorber 105 includes an absorber (absorber) having an absorption chamber 105a to which a third pipe 107c, a fourth pipe 107d, and a fifth pipe 107e are connected.
  • the refrigerant (water vapor) R evaporated (vaporized) in the evaporation unit 104 is supplied to the absorption chamber 105a through the third pipe 107c, the refrigerant is transferred to the absorption liquid A in the absorption chamber 105a. R is absorbed.
  • the absorbing liquid A dropped from the fifth pipe 107e is a concentrated solution having high hygroscopicity
  • the evaporated (vaporized) refrigerant (water vapor) R can be easily absorbed.
  • the absorption liquid A that has absorbed the refrigerant R becomes a dilute solution and is sent from the absorption chamber 105a to the regeneration unit 106 through the fourth pipe 107d.
  • the regeneration unit 106 includes a regeneration chamber 106a to which the fourth pipe 107d, the fifth pipe 107e, and the first pipe 107a are connected, and a heater (heating means) 112 that heats the regeneration chamber 106a. (Generator).
  • the regeneration unit 106 when the absorbing liquid A that has absorbed the refrigerant R is supplied to the regeneration chamber 106a through the fourth pipe 107d, the absorbing liquid A that has absorbed the refrigerant R is heated in the regeneration chamber 106a.
  • the refrigerant R is evaporated (vaporized) from the absorbing liquid A by being heated using 112.
  • the refrigerant R becomes gas (water vapor) and is sent from the regeneration chamber 106a to the condensing unit 103 through the first pipe 107a.
  • the absorption liquid A becomes a concentrated solution (a state in which the refrigerant R is easily absorbed) and is sent from the regeneration chamber 106a to the absorption unit 105 through the fifth pipe 107e.
  • the absorption heat pump 100 it is possible to circulate the refrigerant R in the refrigerant circulation system 101 and perform heat transport while circulating the absorption liquid A in the absorption liquid circulation system 102. It has become.
  • the heat transport apparatus to which the present invention is applied has a configuration in which the regeneration unit 106 heats the absorption liquid A in the regeneration chamber 106a by using the decomposition heat generated by the decomposition of nitrous oxide. . That is, the heater 112 replaces a heater (combustion reaction unit) that heats the regeneration chamber 106 by using combustion heat generated when conventional fossil fuel or the like is combusted.
  • the heat transport device shown in FIG. 1 is a characteristic part of the present invention, for example, as shown in FIG. 2, a nitrous oxide decomposition catalyst (hereinafter simply referred to as a catalyst) 21 that decomposes nitrous oxide.
  • a catalyst 21 that decomposes nitrous oxide.
  • a temperature measuring device (temperature measuring means) 26 for measuring the temperature of the catalyst 21 and a control unit (control means) 27 for controlling each part are provided.
  • the decomposition reactor 22 includes a main body (decomposition reaction chamber) 22a containing the catalyst 21 inside, a gas inlet 22b through which fuel gas is introduced into one end side of the main body 22a, and the main body 22a. It has a structure in which a gas discharge port 22c through which cracked gas is discharged is provided on the other end side.
  • the decomposition reactor 22 it is preferable to use a material having excellent heat resistance and oxidation resistance as the material of the decomposition reactor 22, and in particular, a member on the side of the gas discharge port 22 c exposed to high temperature and high pressure by the decomposition gas has a high temperature. It is preferable to use a material that can sufficiently withstand thermal fatigue or oxidation under high pressure. Examples of such materials include stainless steel, Ni-base alloy, and Co-base alloy. Moreover, ceramics, silicon carbide (SiC), or the like can be used as a heat shielding material. Further, these composite materials may be used. Moreover, the decomposition reactor 22 may be provided with a mechanism for forcibly cooling by water cooling or air cooling.
  • the catalyst 21 it is preferable to use a catalyst that can efficiently decompose nitrous oxide in a wide temperature range (particularly in a low temperature range) and can sufficiently withstand thermal fatigue, oxidation, and the like at high temperatures.
  • a catalyst having high decomposition efficiency of nitrous oxide and excellent heat resistance and oxidation resistance are disclosed in, for example, “JP 2002-153734 A” and “JP 2002-253967 A” described later. Things can be used.
  • any of the catalysts shown in the following [1] to [6] can be used.
  • [1] A catalyst in which aluminum (Al), magnesium (Mg), and rhodium (Rh) are supported on a carrier.
  • [2] A catalyst in which magnesium (Mg) and rhodium (Rh) are supported on an alumina (Al 2 O 3 ) support.
  • [3] A catalyst in which rhodium (Rh) is supported on a carrier in which a spinel crystalline composite oxide is formed of at least a part of aluminum (Al) and magnesium (Mg).
  • At least one metal selected from the group consisting of zinc (Zn), iron (Fe), manganese (Mn) and nickel (Ni), aluminum (Al) and rhodium (Rh) is supported on the carrier.
  • At least one metal selected from the group consisting of zinc (Zn), iron (Fe), manganese (Mn) and nickel (Ni) and rhodium (Rh) are supported on an alumina (Al 2 O 3 ) support. Catalyst.
  • a spinel crystalline composite comprising at least a part of aluminum (Al) and at least one metal selected from the group consisting of zinc (Zn), iron (Fe), manganese (Mn), and nickel (Ni)
  • the support selected from silica (SiO 2 ) and silica alumina (SiO 2 —Al 2 O 3 ) is at least selected from the group consisting of rhodium (Rh), ruthenium (Ru), and palladium (Pd).
  • Rh rhodium
  • Ru ruthenium
  • Pd palladium
  • a catalyst or the like carrying one noble metal can be suitably used. By using such a catalyst 21, it is possible to decompose nitrous oxide into nitrogen and oxygen with a decomposition efficiency close to 100%.
  • the catalyst 21 is a cordierite and metal honeycomb or porous ceramic carrier coated with alumina and impregnated with rhodium effective for decomposing nitrogen oxides by 2 to 3% by mass
  • examples thereof include those in which a support layer made of alumina is formed on a honeycomb structure made of alumina, cordierite, or silicon carbide, and rhodium that is effective in decomposing nitrogen oxides is supported on the support layer.
  • rhodium that is effective in decomposing nitrogen oxides is supported on the support layer.
  • it is not necessarily limited to these.
  • a catalyst used for decomposing and removing nitrous oxide in exhaust gas discharged in a manufacturing process of adipic acid, a manufacturing process of nitric acid, or the like can be used.
  • Such a catalyst is represented by, for example, MAl 2 O 3 (M is any one of Pd, Cu, Cu / Mg, Cu / Zn, Cu / Zn / Mg), and M is 10 to 30.
  • M is any one of Pd, Cu, Cu / Mg, Cu / Zn, Cu / Zn / Mg
  • M is 10 to 30.
  • Examples thereof include a support in which a precious metal is supported at a rate of 0.1 to 2% by mass on an alumina support containing at a rate of mass%.
  • the shape of the catalyst 21 is not particularly limited.
  • any shape such as powder, granule, pellet, honeycomb, porous, pulverized, mesh, plate, or sheet can be used. What is necessary is just to select and use the optimal shape and size suitably from shapes.
  • the filling method of the main body 22a of the catalyst 21 and the shape of the main body 22a according to the catalyst 21 are also matched to the design of the cracking reaction sections 6 and 13 included in the cracking gas boiler 1 and the cracking gas turbine 11. And can be implemented arbitrarily.
  • the decomposition reactor 22 may be configured to be able to replace the catalyst 21 (in some cases, the main body 22a) in accordance with the deterioration of the catalyst 21 over time. In addition, it is possible to extract and purify a noble metal component from the catalyst 21 whose performance has been reduced and recover it, and then use the recovered noble metal on a new carrier as a regenerated catalyst.
  • the decomposition reactor 22 is provided with a heater (preheating means) 28 for heating the catalyst 21.
  • the heater 28 preheats (preheats) the catalyst 21 to a temperature at which nitrous oxide can be decomposed (decomposition start temperature) before starting decomposition of nitrous oxide, that is, before supplying fuel gas to the decomposition reactor 22. ).
  • the heater 28 shown in FIG. 2 is arranged inside the main body 22a so as to be in contact with the periphery of the catalyst 21.
  • the heater 28 is connected to a power source (not shown) via a power supply line 29, and can generate heat by supplying power from the power source.
  • a resistance heating method, an induction heating method, or the like can be used as the heater 28 as the heater 28, a resistance heating method, an induction heating method, or the like.
  • the heating method of the catalyst 21 is not limited to the method of heating the catalyst 21 with the heater 28 arranged inside the main body 22a, and the catalyst 21 is heated with the heater 28 arranged outside the main body 22a. It is also possible to use a method of heating. In this case, the main body 22a is heated by the heater 28, and the catalyst 21 can be heated by radiation or heat conduction from the main body 22a.
  • a method for heating the catalyst 21 it is also possible to use a method for heating the catalyst 21 by directly supplying electric power to the catalyst 21.
  • the method for heating the catalyst 21 is not particularly limited, and can be appropriately selected from the methods for heating the catalyst 21.
  • the fuel gas supply line 23 is a pipe (flow path) whose one end is connected to the inlet side (gas inlet 22 b) of the cracking reactor 22 via the flow rate adjusting unit 25, and the other end side is a fuel gas A fuel gas supply source 31 is connected via the on-off valve 30.
  • the fuel gas on-off valve 30 is for opening / closing the fuel gas supply line 23 and for supplying / cutting off the fuel gas from the fuel gas supply source 31 (open / close means).
  • the fuel gas on / off valve 30 can be used not only for opening and closing the fuel gas supply line 23 but also for adjusting the opening degree (including pressure and the like).
  • the fuel gas on-off valve 30 can be a control valve with a flow rate control (flow rate control valve) that can control the flow rate.
  • the fuel gas on / off valve 30 is electrically connected to the control unit 27, and the control of the fuel gas on / off valve 30 can be controlled by the control unit 27.
  • the fuel gas on / off valve 30 is not limited to the configuration using the above-described control valve with flow rate adjustment (flow rate adjustment valve), but separately from the valve (open / close valve) for opening and closing the fuel gas supply line 23.
  • a configuration in which a regulator (flow rate regulator) for adjusting the flow rate of the fuel gas flowing in the gas supply line 23 is also possible.
  • the fuel gas supply source 31 has a fuel gas storage part in which the fuel gas is temporarily stored in order to supply fuel gas containing nitrous oxide, and the fuel gas storage part is filled with nitrous oxide.
  • a gas container for example, a cylinder, a tank, a cardle, etc.
  • the fuel gas supply source 31 can supply the fuel gas containing nitrous oxide from the high-pressure gas container 31a to the fuel gas supply line 23 by opening the fuel gas on-off valve 30. .
  • the nitrogen gas supply line 24 is a pipe (flow path) whose one end side is connected to the upstream side of the flow rate adjustment unit 25 of the fuel gas supply line 23, and the nitrogen gas opening / closing valve 32 is connected to the other end side.
  • a nitrogen gas supply source 33 is connected.
  • the nitrogen gas supply line 24 has a function as a concentration adjusting means for adjusting the concentration of nitrous oxide contained in the fuel gas by introducing the nitrogen gas into the fuel gas supply line 23.
  • the nitrogen gas opening / closing valve 32 is for opening / closing the nitrogen gas supply line 24 and for supplying / blocking the nitrogen gas from the nitrogen gas supply source 33 (opening / closing means).
  • the nitrogen gas on / off valve 32 can be used not only for opening and closing the nitrogen gas supply line 24 but also for adjusting the opening degree (including pressure and the like).
  • a control valve with a flow rate adjustment (flow rate adjustment valve) capable of controlling the flow rate is used for the nitrogen gas on-off valve 32.
  • the nitrogen gas on / off valve 32 is electrically connected to the control unit 27, and the control unit 27 can drive and control the nitrogen gas on / off valve 32.
  • the nitrogen gas on / off valve 32 is not limited to the configuration using the above-described control valve with a flow rate adjustment (flow rate adjustment valve), but separately from the valve (open / close valve) for opening and closing the nitrogen gas supply line 24.
  • a configuration in which a regulator (flow rate regulator) for adjusting the flow rate of the nitrogen gas flowing in the gas supply line 24 is also possible.
  • the nitrogen gas supply source 33 has a nitrogen gas storage part in which nitrogen gas is temporarily stored, and the nitrogen gas storage part has a high-pressure gas container (for example, a cylinder, a tank, a curdle, etc.) 33a filled with nitrogen. Is arranged.
  • the nitrogen gas supply source 33 can supply the nitrogen gas from the high-pressure gas container 33 a to the nitrogen gas supply line 24 by opening the nitrogen gas on-off valve 32.
  • the flow rate adjusting unit 25 may be anything that can adjust the flow rate (introduction amount) of the fuel gas introduced from the fuel gas supply line 23 into the decomposition reactor 22.
  • a control valve (flow rate adjusting valve) or the like can be used.
  • the flow rate adjusting unit 25 is electrically connected to the control unit 27, and the control unit 27 can drive and control the flow rate adjusting unit 25.
  • a flow meter (flow rate measuring means) for measuring the flow rate of the fuel gas flowing in the flow rate adjusting unit 25 is provided, or a regulator or a control valve with such a flow meter is used.
  • a flow rate of the fuel gas introduced into the decomposition reactor 22 can be adjusted with high accuracy.
  • the temperature measuring device 26 measures the temperature of the catalyst 21 directly or indirectly, is electrically connected to the control unit 27, and outputs a measurement result (measurement data) to the control unit 27.
  • the temperature measuring device 26 shown in FIG. 2 is attached to the main body portion 22 a of the decomposition reactor 22, and can measure the temperature on the downstream side of the catalyst 21 while being in contact with the catalyst 21.
  • the temperature on the upstream side (gas inlet 22b) side of the catalyst 21 is generally used.
  • the temperature on the downstream (gas discharge port 22c) side becomes higher than that. Therefore, the catalyst 21 exposed to the high temperature and high pressure by the cracked gas, the deterioration of the members on the gas outlet 22c side (for example, thermal fatigue, oxidation, etc.), especially nitrous oxide contains oxygen in the cracked gas. It is preferable to measure the temperature on the downstream side (gas exhaust port 22c) side of the catalyst 21 described above in order to prevent the reaction (oxidation).
  • the temperature measuring device 26 is not limited to the configuration shown in FIG. 3 described above, and may be configured to measure the temperature on the upstream side (gas inlet 22b) side of the catalyst 21. This is preferable in detecting whether or not the catalyst 21 heated by the heater 28 has been heated to the decomposition start temperature before starting the decomposition of nitrous oxide. Then, based on the measurement result by the temperature measuring device 26, when the catalyst 21 is heated to the decomposition start temperature, the heating by the heater 28 may be stopped. Thereby, the heating by the heater 28 can be performed efficiently.
  • the location which measures the temperature of the catalyst 21 it is not necessarily limited to said location, For example, in order to measure the average temperature of the catalyst 21, the temperature of the center part of the catalyst 21 is measured. It is also possible to measure the temperatures at these multiple locations separately.
  • the temperature measuring device 26 is not limited to the configuration that directly measures the temperature of the catalyst 21, and may indirectly measure the temperature of the catalyst 21 by measuring the temperature of the main body 22 a that houses the catalyst 21, for example. Is possible.
  • the temperature measuring device 26 is not limited to the configuration for directly or indirectly measuring the temperature of the catalyst 21 described above, but directly or indirectly determines the temperature of the cracked gas discharged from the gas discharge port 22c of the cracking reactor 22. It is good also as a structure to measure to. Furthermore, it is good also as a structure which measures the temperature of both these catalysts 21 and cracked gas.
  • thermometer using a thermocouple for example, a thermometer using a thermocouple, a non-contact type thermometer such as a radiation thermometer, a data logger, or the like can be used, but it is not necessarily limited to these. Instead, the catalyst 21 and the cracked gas can be appropriately selected from those that can be measured and used.
  • the control unit 27 is composed of a computer (CPU) or the like, and based on the measurement result (measurement data) from the temperature measuring device 26, according to the control program recorded therein, the flow rate adjusting unit 25 and the fuel gas on-off valve 30 described above. Control of the nitrogen gas on-off valve 32 is performed.
  • the catalyst 21 exposed to the high temperature and high pressure by the cracked gas, the members on the gas discharge port 22c side, etc. may be deteriorated (for example, thermal fatigue or oxidation). There is.
  • the temperature of the cracked gas becomes too low it may be difficult to continue the self-decomposition of nitrous oxide.
  • control unit 27 can control the temperature of the cracked gas within a range in which the decomposition of the nitrous oxide using the catalyst 21 is continued in the cracking reactor 22 so that such a problem does not occur. preferable.
  • control unit 27 controls the flow rate adjusting unit 25 based on the measurement result from the temperature measuring device 26, and the fuel gas supply line 23 supplies the decomposition reactor 22. The flow rate of the supplied fuel gas is adjusted.
  • control is performed to relatively increase the flow rate of the fuel gas supplied from the fuel gas supply line 23 to the cracking reactor 22.
  • the amount of fuel gas introduced into the cracking reactor 22 is increased, and the temperature of the cracked gas is relatively increased by increasing the amount of decomposition (heat of decomposition) of nitrous oxide decomposed in the cracking reactor 22. It is possible.
  • the decomposition of nitrous oxide using the catalyst 21 is continued in the decomposition reactor 22 while the temperature of the decomposition gas is controlled by the control unit 27. Can be performed automatically.
  • control unit 27 controls the nitrogen gas on-off valve 32 based on the measurement result from the temperature measuring device 26 and the nitrogen gas supply line 24 to the fuel gas supply line. The flow rate of the nitrogen gas supplied to 23 is adjusted.
  • control is performed to relatively increase the concentration of nitrous oxide contained in the fuel gas. That is, a control for relatively reducing the flow rate of nitrogen gas supplied from the nitrogen gas supply line 24 to the fuel gas supply line 23 or stopping supply of nitrogen gas from the nitrogen gas supply line 24 to the fuel gas supply line 23. I do. Thereby, the addition of nitrogen gas to the fuel gas flowing in the fuel gas supply line 23 is stopped or the amount added is reduced, and the concentration of nitrous oxide contained in the fuel gas can be relatively increased. it can. As the amount of decomposition (heat of decomposition) of nitrous oxide decomposed in the decomposition reactor 22 increases accordingly, the temperature of the decomposition gas can be relatively increased.
  • control is performed to relatively lower the concentration of nitrous oxide contained in the fuel gas. That is, a control for relatively increasing the flow rate of nitrogen gas supplied from the nitrogen gas supply line 24 to the fuel gas supply line 23 or starting supply of nitrogen gas from the nitrogen gas supply line 24 to the fuel gas supply line 23. I do. Accordingly, the concentration of nitrous oxide is increased while adding or increasing the amount of nitrogen gas to the fuel gas flowing in the fuel gas supply line 23 and diluting the nitrous oxide contained in the fuel gas with the nitrogen gas. Can be made relatively low. As a result, the decomposition amount (heat of decomposition) of nitrous oxide decomposed in the decomposition reactor 22 decreases, so that the temperature of the decomposition gas can be relatively lowered.
  • an inert gas such as helium (He), neon (Ne), argon (Ar), xenon (Xe), krypton (Kr), etc.
  • the concentration of nitrous oxide contained in the fuel gas can be adjusted by adding air (including dry air) or the like to the fuel gas.
  • nitrous oxide is continuously decomposed using the catalyst 21 in the decomposition reactor 22 while controlling the temperature of the decomposition gas. Is possible.
  • the above-described temperature control of the cracked gas can be performed by combining the methods using (1) and (2).
  • the above-described temperature control of the cracked gas can be stably performed with a simple configuration.
  • you may perform temperature control of cracked gas using the method of other than that.
  • NO x measurement means for measuring the concentration of NO x in the decomposition gas.
  • concentration of NO x gas such as undecomposed nitrous oxide (N 2 O), nitric oxide (NO), nitrogen dioxide (NO 2 ), etc. contained in the cracked gas, It is possible to accurately control the temperature of the cracked gas.
  • NO x removing means means for removing NO x contained in the cracked gas.
  • the NO x removal unit for example, by adding ammonia (NH 3) decomposition gas containing NO x, and selective reaction (reduction) is not ammonia and NO x by denitration catalyst, water (H 2 A denitration apparatus that decomposes into O) and nitrogen (N 2 ) can be used.
  • NH 3 ammonia
  • H 2 A denitration apparatus that decomposes into O
  • N 2 nitrogen
  • an optimum one may be selected from conventionally known ones.
  • the NO x removal means a NO x decomposition catalyst capable of directly decomposing NO x contained in the cracked gas may be used.
  • the supply of fuel gas to the cracking reactor 22 is stopped, and then nitrogen gas is supplied to the cracking reactor 22. Is preferably supplied.
  • control unit 27 performs control to close the fuel gas on-off valve 30, thereby stopping the supply of the fuel gas to the decomposition reactor 22, and the nitrogen gas supplied from the nitrogen gas supply line 24. Is introduced into the decomposition reactor 22.
  • the control unit 27 introduces nitrogen gas into the cracking reactor 22 for a certain period of time, that is, a sufficient time to remove the cracked gas remaining in the catalyst 21, and then closes the nitrogen gas on-off valve 32. And the supply of nitrogen gas to the decomposition reactor 22 is stopped.
  • inert gases such as He, Ne, Xe, Ar, Kr, air (including dry air), and the like are decomposed. It is also possible to introduce into the reactor 22.
  • step S101 the heater 28 is driven and the catalyst 21 is heated (preheated) before starting the decomposition of nitrous oxide.
  • step S102 based on the temperature of the catalyst 21 measured by the temperature measuring device 26, the control unit 27 determines whether or not the catalyst 21 has been heated to the decomposition start temperature. If it is determined that the catalyst 21 has been heated to the decomposition start temperature, the process proceeds to step S103, and the driving of the heater 28 is stopped in step S103. On the other hand, when it is determined that the catalyst 21 has not been heated to the decomposition start temperature, the heating of the catalyst 21 by the heater 28 is continued until the catalyst 21 reaches the decomposition start temperature.
  • step S104 fuel gas is supplied to the decomposition reactor 22, and the decomposition reactor 22 decomposes nitrous oxide using the catalyst 21.
  • the flow rate of the fuel gas supplied to the decomposition reactor 22, the concentration of nitrous oxide contained in the fuel gas, and the like are set in advance.
  • step S105 based on the temperature of the catalyst 21 (or cracked gas) measured by the temperature measuring device 26, the control unit 27 sets a value (range) in which the temperature of the catalyst 21 (or cracked gas) is set in advance. It is determined whether or not the number is exceeded. If it is determined that the temperature of the catalyst 21 (or cracked gas) has exceeded the set value (range), the process proceeds to step S106. On the other hand, if it is determined that the temperature of the catalyst 21 (or cracked gas) is within the set value (range), the process proceeds to step S110.
  • step S106 the control unit 27 determines (comparison) whether the temperature of the catalyst 21 (or cracked gas) is higher or lower than a set value (range).
  • step S107 When it is determined that the temperature of the catalyst 21 (or cracked gas) is higher than the set value (range), the process proceeds to step S107, and the controller 27 is supplied to the cracking reactor 22 in step S107.
  • the fuel gas flow rate or the concentration of nitrous oxide contained in the fuel gas is adjusted to decrease. Then, after the adjustment, the process proceeds to step S109.
  • step S108 when it is determined that the temperature of the catalyst 21 (or cracked gas) is lower than the set value (range), the process proceeds to step S108, and the controller 27 is supplied to the cracking reactor 22 in step S108.
  • the adjustment is made to increase the flow rate of the fuel gas or the concentration of nitrous oxide contained in the fuel gas. Then, after the adjustment, the process proceeds to step S109.
  • step S107 or step S108 for example, a range in which the set value of the flow rate of the fuel gas supplied to the cracking reactor 22 or the set value of the concentration of nitrous oxide contained in the fuel gas can be adjusted. Then, it is divided into a predetermined number of steps, and the set value is lowered or increased by one step from the current step.
  • step S109 based on the temperature of the catalyst 21 (or cracked gas) measured by the temperature measuring device 26, the control unit 27 determines whether the temperature of the catalyst 21 (or cracked gas) has returned to the set value (range). Determine whether or not.
  • the process proceeds to step S110.
  • step S106 determines whether or not the temperature of the catalyst 21 (or cracked gas) has returned to the set value (range).
  • the control unit 27 determines that it is abnormal and forcibly proceeds to step S110 (not shown in FIG. 3).
  • step S110 the control unit 27 determines whether or not to stop the fuel gas supply.
  • Examples of the case of stopping the supply of the fuel gas include a case where a stop command is received from the outside and a case where it is determined that there is an abnormality in step S109. And when stopping supply of fuel gas, it progresses to Step S111. On the other hand, when the supply of the fuel gas is not stopped, the process returns to step S105, and the temperature measurement of the catalyst 21 (or cracked gas) by the temperature measuring device 26 is continued.
  • step S111 after the supply of fuel gas is stopped, the process proceeds to step S112, and in this step S112, nitrogen gas is supplied to the decomposition reactor 22. Thereby, the cracked gas which nitrogen gas stayed in the catalyst 21 is pushed out, and the cracked gas stayed in the catalyst 21 can be removed.
  • nitrous oxide is continuously decomposed using the catalyst 21 in the decomposition reactor 22 while controlling the temperature of the decomposition gas. Is possible.
  • the measurement data measured by the temperature measuring device 26 and the determination result of the control unit 27 based on the measurement data may be displayed on a monitor (not shown) or output to a printer, for example.
  • a monitor not shown
  • a printer for example.
  • step S109 when it is determined that there is an abnormality in step S109, it may be notified as necessary.
  • the notification method is not particularly limited, and for example, an alarm can be issued or a display can be performed.
  • the fuel gas containing nitrous oxide is supplied to the cracking reactor 21, and the nitrous oxide contained in the fuel gas is supplied to the cracking reactor 21 by the above-described method.
  • the decomposition heat generated by the decomposition of the nitrous oxide can continuously decompose the nitrous oxide in the fuel gas supplied thereafter.
  • the decomposition gas (N 2 , O 2 ) of nitrous oxide obtained by decomposing nitrous oxide (N 2 O) in the decomposition reactor 22 described above is used as the above. Supply to the heater 112.
  • the heater 112 is a heating (high temperature) side heat exchanger attached to the regeneration chamber 106a. While the cracked gas passes through the heat exchanger, the regeneration chamber exchanges heat with the cracked gas. 106a is heated.
  • a heat sink (fin) 112a for improving thermal conductivity with the regeneration chamber 106a is provided in the heater 112 in contact with the heat transfer surface of the regeneration chamber 106a. . Thereby, the regeneration chamber 106a can be efficiently heated.
  • heat exchangers can be used for the heater 112 according to the application.
  • the types of heat exchangers include tube type (double pipe type, multi-pipe type (shell & tube type), spiral type, etc.), plate type, regenerative type, etc. These may be selected and used as appropriate according to the application.
  • the heat transport method to which the present invention is applied includes a condensation step S1 in which heat is released from the refrigerant R while condensing the refrigerant R in the refrigerant circulation system 101, and in the refrigerant circulation system 101.
  • Evaporating step S2 in which the refrigerant R absorbs heat while evaporating the refrigerant R
  • absorption step S3 in which the evaporated refrigerant R is absorbed by the absorbent A in the absorbent circulation system 102
  • the absorbed refrigerant R A regeneration step S4 for evaporating from the absorbent A in the absorbent circulation system 102. While repeating these steps S1 to S4, in the regeneration step S4, the heat of decomposition generated by the decomposition of nitrous oxide is used.
  • the absorption liquid A is heated.
  • the refrigerant (water vapor) R evaporated (vaporized) by the regeneration unit 106 is condensed by the condensing unit 103 to release heat from the refrigerant R. Further, the refrigerant (water) R condensed (liquefied) by the condensing unit 103 is evaporated by the evaporating unit 104, so that the refrigerant R absorbs heat. Further, the refrigerant (water vapor) R evaporated (vaporized) by the evaporation unit 104 is absorbed by the absorption liquid A by the absorption unit 105. Further, the refrigerant R absorbed in the absorbing liquid A by the absorbing unit 105 is evaporated from the absorbing liquid A while being heated by the regenerating unit 106.
  • this heat transport device it is possible to transport heat while circulating the refrigerant R in the refrigerant circulation system 101 and circulating the absorption liquid A in the absorption liquid circulation system 102. Further, in this heat transport device, when the absorbing liquid A is heated using the heater 112 in the regeneration unit 106, the heat of decomposition generated by the decomposition of nitrous oxide is used as the heat source.
  • heat transport apparatus As described above, in the heat transport apparatus and the heat transport method to which the present invention is applied, heat transport using energy generated by decomposition of nitrous oxide is possible. And according to this invention, it is possible to provide the heat transport apparatus which enabled utilization of nitrous oxide as energy friendly to a global environment, and the heat transport method using such a heat transport apparatus.
  • nitrous oxide N 2 O
  • a cooler (cooling means) 113 for cooling the condensation chamber 103a and a cooler (cooling means) 114 for cooling the absorption chamber 105a are provided using cooling heat accompanying adiabatic expansion. It is.
  • these coolers 113 and 114 are cooling (low temperature) side heat exchangers attached to the condensation chamber 103a and the absorption chamber 105a. Nitrous oxide gas that has been lowered in temperature by cooling heat) is supplied. The condensation chamber 103a and the absorption chamber 105a are cooled by heat exchange with the nitrous oxide gas while the low-temperature nitrous oxide gas passes through the heat exchanger.
  • heat sinks (fins) 113a and 114a for improving thermal conductivity between the condensation chamber 103a and the absorption chamber 105a are provided in the condensation chamber 103a and the absorption chamber 105a. It is provided in contact with the heat transfer surface. Thereby, the condensation chamber 103a and the absorption chamber 105a can be efficiently cooled.
  • heat exchangers of various types and sizes can be used for the coolers 113 and 114 according to their applications.
  • the types of heat exchangers include tube type (double pipe type, multi-pipe type (shell & tube type), spiral type, etc.), plate type, regenerative type, etc. These may be selected and used as appropriate according to the application.
  • the heat transport device shown in FIG. 5 is a first unit that supplies the cooling unit with nitrous oxide gas (N 2 O) that is discharged from the high-pressure gas container 31a (not shown in FIG. 5) and adiabatically expanded. It is obtained by decomposing the nitrous oxide gas in the supply line 115, the second supply line 116 for supplying the nitrous oxide gas discharged from the coolers 113 and 114 to the decomposition reactor 22, and the decomposition reactor 22.
  • a third supply line 117 for supplying the nitrous oxide decomposition gas (N 2 , O 2 ) to the heater 112 and a discharge line 118 for discharging the decomposition gas from the heater 112 are provided.
  • the first supply line 115 is a pipe (flow path) having one end connected to the high-pressure gas container 31a and the other end connected to the inlet side of the coolers 113 and 114.
  • the second supply line 116 has one end connected to the outlet of the coolers 113 and 114 and the other end connected to the inlet (gas inlet 22b) of the cracking reactor 22 (flow path). It is. Then, the first and second supply lines 115 and 116, nitrous oxide gas released from the high pressure gas vessels 31a (N 2 O) a decomposition reactor 22 to supply nitrous oxide gas supply line (nitrous oxide Nitrogen gas supply means).
  • the third supply line 117 is a pipe (flow path) whose one end side is connected to the outlet side (gas exhaust port 22 c) of the decomposition reactor 22 and whose other end side is connected to the inlet side of the heater 112.
  • the discharge line 118 is a pipe (flow path) whose one end is connected to the outlet of the heater 112.
  • this heat transport device it is possible to transport heat while circulating the refrigerant R in the refrigerant circulation system 101 and circulating the absorption liquid A in the absorption liquid circulation system 102. Further, in this heat transport device, when the absorbing liquid A is heated using the heater 112 in the regeneration unit 106, the heat of decomposition generated by the decomposition of nitrous oxide is used as the heat source. Further, in this heat transport device, when the refrigerant R and the absorbing liquid A are cooled using the coolers 113 and 114 in the condensation chamber 103a and the absorption chamber 105a, the cooling heat accompanying the adiabatic expansion of nitrous oxide is used as the cold source. Is used.
  • heat transport apparatus As described above, in the heat transport apparatus and the heat transport method to which the present invention is applied, heat transport using energy generated by decomposition of nitrous oxide is possible. And according to this invention, it is possible to provide the heat transport apparatus which enabled utilization of nitrous oxide as energy friendly to a global environment, and the heat transport method using such a heat transport apparatus.
  • both the coolers 113 and 114 are provided. However, only one of the coolers 113 and 114 may be provided. Is possible.
  • the characteristic part of the present invention is not necessarily limited to the configuration shown in FIG.
  • the shape, number, arrangement, etc. of the decomposition reactor 22 can be appropriately changed according to the design of the heat transport device.
  • the fuel gas supply source 31, the nitrogen gas on-off valve 32, the nitrogen gas supply source 33, and the like can be appropriately changed in accordance with the design of the heat transport device.
  • the heat transport device to which the present invention is applied passes (circulates) the refrigerant R in the refrigerant circulation system 101. It is also possible to employ a configuration in which a pump (fluid passing means) to be used and a pump (fluid passing means) for passing (circulating) the absorbing liquid A in the absorbing liquid circulating system 102 are arranged.
  • the heat transport apparatus to which the present invention is applied can be configured to include other necessary accessory equipment (equipment / parts), security equipment (equipment / parts), and the like.
  • the structure other than the characteristic part of the present invention described above can have the same structure as an existing absorption heat pump.
  • the present invention can be applied to both a heat absorption heat pump and a second type of temperature rising absorption heat pump.
  • the absorption heat pump to which the present invention is applied is not limited to the direct firing method in which heating is performed using the decomposition gas generated by the decomposition of nitrous oxide described above, but the decomposition generated by the decomposition of nitrous oxide described above.
  • the present invention can be applied to a steam cooking system in which steam is generated by heat recovery from gas and then heated using this steam.
  • examples of the absorption heat pump to which the present invention is applied include, for example, a single effect absorption type, a double effect absorption type, a triple effect absorption type heat pump, and the like.
  • the present invention can be applied.
  • the absorption liquid A with high absorbency with respect to the refrigerant
  • the former is preferably used in the air conditioning field, and the latter is preferably used in the refrigeration field.
  • Heat transport apparatus it is possible to obtain a cold air (cold) T L described above, a hot air (hot) T H, and can be variously applied to refrigeration and air conditioning fields.
  • the heat transport device to which the present invention is applied can be applied to air conditioning equipment and air conditioning equipment such as the above-described cooling and heating air conditioners.
  • the air conditioner can have a dehumidifying function for dehumidifying the room.
  • heating field in addition to heating, it can be applied to heating equipment and heating equipment that perform hot water supply, hot water, drying, and the like.
  • cooling field in addition to cooling, it can be applied to cooling equipment and cooling equipment for performing refrigeration, freezing, cold water, ice making, and the like.
  • the heat transport apparatus to which the present invention is applied can be applied to a variety of sizes from large to small. In addition to its use for factories (industrial) and homes (households), it can be used in various fields, and it can be designed to suit the application, such as installation (stationary), portable, and portable. do it.
  • Nitrous oxide used in the present invention can be produced industrially.
  • examples of the method for industrially producing nitrous oxide include methods using the following (1) to (3).
  • nitrous oxide produced industrially for example, high purity nitrous oxide having a purity of 99.9 (3N) to 99.999 (5N)%, purity of 97.0% or more (Japan Pharmacopoeia)
  • high purity nitrous oxide having a purity of 99.9 (3N) to 99.999 (5N)%, purity of 97.0% or more Japanese Pharmacopoeia
  • examples thereof include medical nitrous oxide and industrial nitrous oxide having a purity of 98% or more.
  • examples of the method for producing nitrous oxide include the following methods (4) to (10).
  • Nitric acid is reduced with zinc or tin, or with sulfurous acid gas.
  • the produced nitrous oxide is filled in the high-pressure gas container 31a by a gas maker, then sent to the fuel gas supply source 31, and temporarily stored in the fuel gas storage section.
  • the high-pressure gas container 31a can be used repeatedly by being returned to the gas manufacturer after use and being refilled.
  • the fuel gas supply method is not limited to the method of supplying using the high-pressure gas container 31a (replacement of the high-pressure gas container 31a).
  • the fuel gas supply is performed using a transportation means such as a tanker or a tank lorry. It is possible to use a method of supplying to a storage tank (high pressure gas container 31a) installed in the source 31. Furthermore, it is also possible to use a method of supplying fuel gas containing nitrous oxide to a storage tank (high pressure gas container 31a) installed in the fuel gas supply source 31 through a pipeline.
  • the nitrogen gas supply method is not limited to the method of supplying using the high-pressure gas container 33a (replacement of the high-pressure gas container 33a), and the method of supplying using the same method as the fuel gas supply method described above. It is possible.
  • the decomposition start temperature of nitrous oxide can be lowered by using the catalyst 21. After the decomposition of nitrous oxide, it is possible to continuously decompose the nitrous oxide supplied thereafter by the heat of decomposition generated by the decomposition of nitrous oxide.
  • the heat of decomposition generated by the decomposition of nitrous oxide keeps the temperature of the catalyst 21 at or above the temperature necessary for decomposing nitrous oxide. Decomposition can be performed continuously.
  • the temperature of the catalyst 21 is preferably in the range of 200 to 600 ° C. from the viewpoint of catalyst activity, and more preferably in the range of 350 to 450 ° C. from the viewpoint of ease of decomposition reaction. That is, in the present invention, it is preferable to perform preheating by the heater 28 and temperature control of the cracked gas by the control unit 27 so that the temperature of the catalyst 21 falls within such a range.
  • nitrous oxide itself undergoes autolysis at about 500 ° C. or higher, nitrous oxide is continuously decomposed without using the catalyst 21 by keeping the decomposition reactor 22 at or above the autolysis temperature. It is also possible to However, it is known that when nitrous oxide is self-decomposed without using the catalyst 21, NO x gas is generated as a decomposition byproduct. Therefore, in the present invention, it is preferable to use the catalyst 21 in order to prevent the generation of the NO x gas. The catalyst 21 can be used even when the temperature is higher than the nitrous oxide autolysis temperature.
  • the temperature of the fuel gas may be any temperature at which nitrous oxide does not liquefy, and can usually be used at room temperature or lower.
  • the fuel gas can be used by preheating to a temperature higher than room temperature. For example, when the concentration of nitrous oxide contained in the fuel gas is low, the decomposition of nitrous oxide can be promoted by preheating the fuel gas.
  • the concentration of nitrous oxide contained in the fuel gas is not particularly limited.
  • the nitrous oxide concentration adjusted in the range of 1 to 100%, or when more energy needs to be obtained Those adjusted in the range of more than 50% to 100% and further adjusted in the range of more than 70% to 100% can be used. Further, by adjusting the concentration of nitrous oxide described above, it is possible to adjust the decomposition reaction rate of nitrous oxide and the like.
  • N 2 nitrogen
  • concentration of nitrous oxide N 2 O contained in the fuel gas
  • N 2 oxygen
  • the oxygen concentration is preferably in the range of about 18 to 24%.
  • the concentration of nitrous oxide contained in the fuel gas is 44. It is preferable to be in the range of about ⁇ 63%.
  • a nitrous oxide having a concentration of less than 44% that is, a fuel gas having a low nitrous oxide concentration.
  • the energy (energy density) generated by the decomposition of the fuel gas is lowered, the decomposition reaction of the nitrous oxide contained in the fuel gas is made gentle so that the above-described decomposition gas increases the temperature and pressure.
  • a nitrous oxide having a concentration exceeding 63% that is, a fuel gas having a high nitrous oxide concentration.
  • the energy (energy density) generated by the decomposition of the fuel gas can be increased, and the output of the decomposition gas boiler 1 and the decomposition gas turbine 11 can be improved.
  • nitrous oxide concentration of 100% it is possible to continuously decompose nitrous oxide using the catalyst 21.
  • high-purity for example, purity 99.9 (3N) to 99.999 (5N)%
  • nitrous oxide is considered in consideration of the production cost of nitrous oxide. It is also possible to use nitrous oxide with a low (for example less than 97% purity).
  • the concentration adjustment of nitrous oxide by nitrogen gas described above is a method of adding nitrogen gas or the like to the fuel gas before decomposition of nitrous oxide, but nitrogen gas or the like is added to the decomposition gas after decomposition of nitrous oxide.
  • the method of adding may be sufficient.
  • a fuel gas in which the concentration of nitrous oxide has been adjusted in advance may be used.
  • nitrous oxide contained in the fuel gas in addition to the nitrogen added for adjusting the concentration of nitrous oxide described above, unmixed components that were mixed during the production of nitrous oxide described later are used. Examples include reactants, by-products, air, and inevitable impurities.
  • an oxygen concentration meter for measuring the oxygen concentration in the cracked gas may be provided.
  • oxygen measuring means oxygen measuring means
  • the space velocity (Space Velocity) of the fuel gas introduced into the decomposition reactor 22 may be set to an optimum value according to the design, for example, in the range of 10 to 140,000 hr ⁇ 1 , preferably It can be set in the range of 100 to 10,000 hr ⁇ 1 .
  • the cracked gas can also be used for fuel combustion.
  • the fuel is combustible using oxygen contained in the cracked gas, for example, in addition to fossil fuels such as petroleum, coal, and natural gas, alternative fuels such as biomass fuel are used. can do.
  • alternative fuels such as biomass fuel are used. can do.
  • the concentration of nitrous oxide contained in exhaust gas discharged from factories and incineration facilities is 10% or less, while the concentration of nitrous oxide contained in excess anesthetic gas discharged from the operating room excludes excess anesthetic gas. Although it is somewhat diluted with compressed air in the apparatus, it is 70% or less, which is a very high concentration.
  • the nitrous oxide decomposition catalyst of the present invention is a catalyst that can cope with the decomposition of nitrous oxide having a low concentration to a high concentration.
  • the nitrous oxide decomposition catalyst of the present invention can be decomposed at a relatively low temperature, is less susceptible to activity degradation due to moisture even in the presence of moisture, and reduces the generation amount of NO x below an allowable concentration.
  • the amount of NO x generated can be reduced to about 1/10 to 1/100 or less of the conventional cracking catalyst.
  • the nitrous oxide decomposition catalyst of the present invention comprises any one of the following catalysts [1] to [3] containing three kinds of metals, aluminum, magnesium and rhodium as essential components: [1] aluminum, magnesium and rhodium [2] a catalyst in which magnesium and rhodium are supported on an alumina carrier, [3] a carrier in which a spinel crystalline composite oxide is formed of at least a part of aluminum and magnesium.
  • the following [4] containing, as essential components, a catalyst on which rhodium is supported, and at least one metal selected from the group consisting of two metals, aluminum and rhodium, and zinc, iron, manganese and nickel.
  • a carrier selected from the group consisting of alumina, silica, zirconia, ceria, titania and tin oxide can be used
  • alumina A carrier selected from zirconia, ceria, titania and tin oxide can be used.
  • Carriers having a surface area of about 30 to 300 m 2 / g can be used, and there is no particular limitation on the shape, but depending on the reactor or reaction method, it is suitable for each of granular, powder, honeycomb, etc. You can choose the shape.
  • the aluminum and magnesium supported on the carrier contain aluminum in an atomic ratio of at least 2 with respect to magnesium.
  • Magnesium is preferably contained in an amount of 0.1 to 20.0% by mass based on the metal atom.
  • the spinel-type crystalline composite oxide is formed, for example, by firing a carrier supporting aluminum and magnesium.
  • the spinel structure is a structure found in an oxide having a chemical formula of XY 2 O 4 and belongs to a cubic system, and Al and Mg are known to form a MgAl 2 O 4 spinel structure.
  • the reason for the nitrous oxide decomposition catalyst of the present invention is not clear, but at least a part of aluminum forms a spinel crystalline composite oxide with magnesium, thereby improving the resolution of nitrous oxide. It is considered that the effect of reducing the generation amount of NO x is exhibited.
  • At least one metal selected from the group consisting of zinc, iron, manganese and nickel and aluminum supported on the carrier is selected from the group consisting of zinc, iron, manganese and nickel. It is preferable that at least 2 or more are contained by atomic ratio with respect to at least 1 type of metal. In addition, it is preferable that at least one metal selected from the group consisting of zinc, iron, manganese and nickel is contained in an amount of 0.1 to 40.0% by mass in terms of metal atoms.
  • At least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group consisting of zinc, iron, manganese, and nickel.
  • the spinel crystalline composite oxide can be produced by firing a carrier supporting aluminum and at least one metal selected from the group consisting of zinc, iron, manganese and nickel.
  • M Zn, Fe, Mn, Ni.
  • the reason for the nitrous oxide decomposition catalyst of the present invention is not clear, but at least a part of aluminum is at least one metal selected from the group consisting of zinc, iron, manganese and nickel, and a spinel crystalline composite. that forms the oxides, thereby improving the resolution of nitrous oxide, is believed to exert an effect of reducing the amount of generation of NO x.
  • the carrier used for the catalyst of [2] is alumina, and the alumina is not particularly limited, but those having a surface area of about 50 to 300 m 2 / g can be used.
  • the magnesium supported on the alumina preferably contains aluminum in an atomic ratio of at least 2 with respect to magnesium. Magnesium is preferably contained in an amount of 0.1 to 20.0% by mass in terms of metal atoms. Moreover, it is preferable that at least a part of aluminum forms a spinel crystalline composite oxide with magnesium.
  • the carrier used for the catalyst of [5] is alumina, and the alumina is not particularly limited, but those having a surface area of about 50 to 300 m 2 / g can be used.
  • At least one metal selected from the group consisting of zinc, iron, manganese and nickel supported on alumina is an atomic ratio of aluminum to at least one metal selected from the group consisting of zinc, iron, manganese and nickel. It is preferable that at least two or more are included. It is preferable that at least one metal selected from the group consisting of zinc, iron, manganese and nickel is contained in an amount of 0.1 to 40.0% by mass based on the metal atom.
  • at least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group consisting of zinc, iron, manganese, and nickel.
  • a catalyst in which a spinel-type crystalline composite oxide is formed of at least a part of aluminum and magnesium is used as the catalyst [3].
  • the atomic ratio of aluminum and magnesium in the catalyst of [3] is preferably such that aluminum is contained in an atomic ratio of at least 2 with respect to magnesium.
  • Magnesium is preferably contained in an amount of 0.1 to 20.0% by mass based on the metal atom.
  • the catalyst [6] uses a carrier in which a spinel crystalline composite oxide is formed of at least a part of aluminum and at least one metal selected from the group consisting of zinc, iron, manganese and nickel.
  • the atomic ratio of aluminum and at least one metal selected from the group consisting of zinc, iron, manganese and nickel in the catalyst of [6] is at least 1 selected from the group where aluminum is zinc, iron, manganese and nickel It is preferable that at least 2 or more is contained by atomic ratio with respect to the metal of seed
  • the rhodium contained in the nitrous oxide decomposition catalyst of the present invention is preferably 0.05 to 10% by mass in terms of metal atoms in any of the catalysts [1] to [6]. More preferably, the content is 0.1 to 6.0% by mass. Although it is possible to improve the catalyst activity at low temperature by increasing the amount of rhodium supported, it is not preferable to support 10% by mass or more in view of the cost of the catalyst, and 0.05% by mass or less. Sufficient nitrous oxide decomposition activity cannot be obtained.
  • nitrous oxide decomposition catalyst of the present invention Next, the method for producing the nitrous oxide decomposition catalyst of the present invention will be described.
  • Various production methods can be used for the nitrous oxide decomposition catalyst of the present invention.
  • (1) impregnation method, (2) coprecipitation method, (3) kneading method, and the like can be used.
  • the production method of the nitrous oxide decomposition catalyst of the present invention will be described.
  • the support selected from the group consisting of alumina, zirconia, ceria, titania and tin oxide is firstly at least one selected from the group consisting of aluminum and zinc, iron, manganese and nickel. Impregnation with inorganic acid salts (nitrate, hydrochloride, sulfate, etc.) or organic acid salts (oxalate, acetate, etc.) of seed metals.
  • an alumina carrier is impregnated with a magnesium inorganic acid salt (nitrate, hydrochloride, sulfate, etc.) or an organic acid salt (oxalate, acetate, etc.).
  • an inorganic support nitrate, hydrochloride, sulfate, etc.
  • an organic salt of at least one metal selected from the group consisting of zinc, iron, manganese, and nickel is used on an alumina support. Impregnate with acid salts (oxalate, acetate, etc.).
  • acid salts oxalate, acetate, etc.
  • the at least one metal salt selected from the group consisting of an aluminum salt, a magnesium salt and zinc, iron, manganese, and nickel it is preferable to use a nitrate.
  • the amount supported on the carrier of aluminum and magnesium is preferably such that aluminum is supported so that the atomic ratio with respect to magnesium is 2 or more. It is preferable to make it 0.1 to 20.0% by mass.
  • the amount of aluminum supported on at least one metal carrier selected from the group consisting of aluminum, zinc, iron, manganese and nickel is aluminum, zinc, iron, manganese and nickel. It is preferably supported so that the atomic ratio with respect to at least one metal selected from the group consisting of 2 or more is supported, and the supported amount of at least one metal selected from the group consisting of zinc, iron, manganese and nickel However, it is preferable to be 0.1 to 40.0% by mass of the total catalyst.
  • magnesium is supported so that the atomic ratio to aluminum is 1 ⁇ 2 or less, and the amount of magnesium supported is 0.1-20. It is preferable to be 0% by mass.
  • at least one metal selected from the group consisting of zinc, iron, manganese and nickel is supported so that the atomic ratio with respect to aluminum is 1 ⁇ 2 or less.
  • the supported amount of at least one metal selected from the group consisting of zinc, iron, manganese and nickel is 0.1 to 40.0% by mass of the total catalyst.
  • the carrier After supporting the desired metal salt on the carrier, the carrier is dried and fired to contain, for example, aluminum and magnesium, and at least part of the aluminum forms a spinel-type crystalline composite oxide with magnesium.
  • a carrier can be obtained, and this carrier is used as the carrier for the catalyst of [1].
  • it contains aluminum and at least one metal selected from the group consisting of zinc, iron, manganese and nickel, and at least a part of aluminum is selected from the group consisting of zinc, iron, manganese and nickel.
  • a support in which a spinel-type crystalline composite oxide is formed with at least one kind of metal can be obtained, and this support is used as a support for the catalyst of [4].
  • the drying temperature after impregnating the aluminum salt and magnesium salt in the catalyst [1], the aluminum salt in the catalyst [4], and at least one metal salt selected from the group consisting of zinc, iron, manganese and nickel is not particularly limited, but is preferably in the temperature range of 80 to 150 ° C, more preferably in the temperature range of 100 to 130 ° C.
  • the drying atmosphere is not particularly limited, and nitrogen or air can be used.
  • the drying time is not particularly limited, but when using the impregnation method, it may usually be about 2 to 4 hours.
  • Calcination of the carrier after impregnation and drying can be performed in a temperature range of 400 to 900 ° C., preferably 500 to 700 ° C.
  • the firing time is not particularly limited, but may be about 1 to 10 hours, preferably about 2 to 4 hours, and the firing temperature may be changed stepwise. Long-term firing is economically undesirable because the effect is saturated, and short-term firing may be less effective.
  • baking can be performed using a baking furnace, a muffle furnace, etc., and any of nitrogen or air may be used as a distribution gas at this time.
  • a rhodium salt is supported on the carrier obtained by firing.
  • an inorganic acid salt nitrate, hydrochloride, sulfate, etc.
  • an organic acid salt oxalate, acetate, etc.
  • the rhodium salt for example, in the case of producing a catalyst containing three kinds of metals, aluminum, magnesium and rhodium, as essential components, at least a part of the aluminum obtained using the above method is magnesium and It is preferably performed on the carrier forming the spinel crystalline composite oxide, but it may be performed simultaneously with the step of impregnating and supporting aluminum and magnesium on the carrier or the step of impregnating and supporting magnesium on the alumina carrier. Further, the supported amount of rhodium is preferably 0.05 to 10% by mass of the whole catalyst.
  • the step of supporting the rhodium salt is for producing a catalyst containing as essential components at least one metal selected from the group consisting of two metals, aluminum and rhodium, and zinc, iron, manganese and nickel.
  • the aluminum obtained by the above method is used as a carrier that forms a spinel crystalline composite oxide with at least one metal selected from the group consisting of zinc, iron, manganese, and nickel.
  • it is carried out with respect to the step of impregnating and supporting at least one metal selected from the group consisting of aluminum and zinc, iron, manganese and nickel on the support, or from zinc, iron, manganese and nickel on the alumina support.
  • the supported amount of rhodium is preferably 0.05 to 10% by mass of the whole catalyst.
  • the catalyst of [3] is produced by supporting a rhodium salt on the support in the same manner as described above. can do.
  • a rhodium salt is added to the support.
  • the catalyst of [6] can be produced by supporting the catalyst.
  • the rhodium-supported catalyst precursor is dried under the same drying conditions as described above, and the dried catalyst precursor is calcined.
  • the firing temperature is preferably 200 to 500 ° C, more preferably 300 to 400 ° C.
  • the catalyst obtained by calcination can be used as a nitrous oxide decomposition catalyst, it is preferable to further perform a reduction treatment, and a rhodium-containing catalyst with higher activity can be obtained by carrying out the reduction treatment.
  • the reduction treatment can be performed by, for example, (1) a method of re-drying after hydrazine reduction and firing, or (2) a method of hydrogen reduction, and a method of hydrogen reduction is preferably used.
  • the reduction temperature is preferably 200 to 500 ° C., more preferably 300 to 400 ° C.
  • the reduction time is not particularly limited, the treatment can be performed in about 1 to 10 hours, preferably about 2 to 4 hours. Moreover, you may perform a reduction process, without performing a baking process, and a rhodium containing catalyst with high activity can be obtained also in this case.
  • a method for producing a catalyst by carrying out a reduction treatment without performing a calcination treatment a method in which hydrogen is reduced at a temperature of 200 to 500 ° C. is preferable.
  • the above catalysts [3] and [6] can be produced.
  • a method for producing the catalyst of [3] using the coprecipitation method for example, ammonia water is dropped into an aqueous solution containing aluminum and magnesium nitrate to neutralize and precipitate, and if necessary, left to age and washed with filtered water. Check that the water has been thoroughly washed with the conductivity of the washing water. Next, after drying for about 10 to 12 hours under the same conditions as in the impregnation method, the obtained dried body is pulverized and molded with uniform particle sizes. Further, a carrier in which at least a part of aluminum forms a spinel-type crystalline composite oxide with magnesium is obtained by baking in a nitrogen or air atmosphere under the same conditions as in the impregnation method.
  • the amount of aluminum and magnesium is preferably such that aluminum has an atomic ratio of 2 or more with respect to magnesium, and magnesium is preferably contained in an amount of 0.1 to 20.0% by mass of the total catalyst in terms of metal atoms. .
  • At least a part of the aluminum thus obtained carries a rhodium salt on a carrier that forms a spinel-type crystalline composite oxide with magnesium.
  • the method, the amount supported, and the subsequent treatment method are the same as the above impregnation method. Can be done.
  • an aqueous solution containing an aluminum nitrate and at least one metal nitrate selected from the group consisting of zinc, iron, manganese and nickel is used as a method for producing the catalyst of [6] using the coprecipitation method.
  • Aqueous ammonia is added dropwise to neutralize and precipitate, and if necessary, aged as it is, washed with filtered water, and it is confirmed that it has been sufficiently washed with the conductivity of the washing water.
  • the obtained dried body is pulverized and molded with uniform particle sizes.
  • At least a part of aluminum is selected from the group consisting of zinc, iron, manganese and nickel and spinel crystallinity.
  • a carrier forming a complex oxide is obtained.
  • the amount of at least one metal selected from the group consisting of aluminum and zinc, iron, manganese and nickel is an atomic ratio of aluminum to at least one metal selected from the group consisting of zinc, iron, manganese and nickel.
  • at least one metal selected from the group consisting of zinc, iron, manganese and nickel is contained in an amount of 0.1 to 40.0% by mass in terms of metal atoms. It is preferable.
  • At least a portion of the aluminum thus obtained carries a rhodium salt on a carrier that forms a spinel crystalline composite oxide with at least one metal selected from the group consisting of zinc, iron, manganese and nickel.
  • the method, the loading amount and the subsequent treatment method can be carried out in the same manner as the above impregnation method.
  • Catalyst production method using a kneading method [3] and [6] catalysts can be produced using a kneading method.
  • a method for producing the catalyst of [3] using the kneading method for example, water is added to alumina and / or aluminum hydroxide and magnesium oxide, magnesium hydroxide and / or magnesium salt, for example, if necessary, The mixture obtained by mechanical mixing can be dried, and further subjected to a firing treatment under the same conditions as in the impregnation method to obtain the spinel crystalline composite oxide.
  • the amount of aluminum and magnesium is preferably such that aluminum has an atomic ratio of 2 or more with respect to magnesium, and magnesium is preferably contained in an amount of 0.1 to 20.0% by mass of the total catalyst in terms of metal atoms. .
  • At least a portion of the aluminum thus obtained carries a rhodium salt on a fired body that forms a spinel-type crystalline composite oxide with magnesium.
  • the method, the amount supported, and the subsequent treatment method are the same as the above impregnation method. This method can be used.
  • the rhodium salt may be added in advance when alumina or the like is mechanically mixed.
  • Examples of the method for producing the catalyst of [6] using the kneading method include at least one oxide selected from the group consisting of alumina and / or aluminum hydroxide and zinc, iron, manganese and nickel, and hydroxylation.
  • at least one oxide selected from the group consisting of alumina and / or aluminum hydroxide and zinc, iron, manganese and nickel, and hydroxylation For example, water is added to the product and / or metal salt, if necessary, and the mixture obtained by mechanical mixing is dried, and further subjected to a firing treatment under the same conditions as in the impregnation method. An oxide can be obtained.
  • the amount of at least one metal selected from the group consisting of aluminum and zinc, iron, manganese and nickel is such that aluminum is based on at least one metal selected from the group consisting of zinc, iron, manganese and nickel.
  • the atomic ratio is preferably 2 or more, and at least one metal selected from the group consisting of zinc, iron, manganese and nickel is 0.1 to
  • At least a portion of the aluminum thus obtained carries a rhodium salt on a fired body that forms a spinel-type crystalline composite oxide with at least one metal selected from the group consisting of zinc, iron, manganese, and nickel.
  • a rhodium salt may be added in advance when alumina or the like is mechanically mixed.
  • the decomposition reaction of nitrous oxide is performed using the decomposition catalyst of the present invention, it can be performed in a temperature range of 200 to 600 ° C.
  • the decomposition catalyst of the present invention and nitrous oxide may be contacted in the gas phase, preferably in the temperature range of 300 to 500 ° C, more preferably in the temperature range of 350 to 450 ° C. If the temperature is lower than 200 ° C., decomposition of nitrous oxide is not sufficient, and if it is 600 ° C. or higher, the catalyst life tends to be short, which is not preferable.
  • the catalyst bed system is not particularly limited, but a fixed bed is generally preferably used.
  • the catalytic activity of the conventional palladium catalyst decreases due to the influence of moisture and does not return to the original activity even when the moisture is removed, whereas the cracking catalyst of the present invention has 1 to 3% moisture coexistence. Although the activity may slightly decrease depending on the condition, it has a characteristic of returning to the original activity again when moisture is removed.
  • the concentration of nitrous oxide contained in exhaust gas discharged from factories and incineration facilities is 10% or less.
  • the concentration of nitrous oxide discharged from the operating room by the surplus anesthetic gas exclusion device may be as high as 3 to 70%.
  • the reaction when decomposing nitrous oxide contained in the anesthetic gas, the reaction usually involves 13 to 20% oxygen, and the reaction is performed under conditions that are severe for the decomposition catalyst.
  • the concentration of nitrous oxide to be decomposed is not particularly limited, but the reaction in which nitrous oxide decomposes into nitrogen and oxygen is an exothermic reaction.
  • the concentration of nitric oxide is preferably 3 to 50%, preferably 3 to 25%, more preferably 3 to 10%.
  • Space velocity is the amount of gas supplied per unit catalyst (SV: Space Velocity) may be in the range of 10hr -1 ⁇ 20000hr -1, preferably in the range of 100hr -1 ⁇ 10000hr -1.
  • the nitrous oxide decomposition catalyst of the present invention is a catalyst capable of decomposing a low concentration to a high concentration nitrous oxide.
  • the concentration of nitrous oxide contained in the surplus anesthetic gas discharged from the operating room is 70% or less, although it is somewhat diluted with compressed air, and is very high. This can be achieved by using a decomposition catalyst for nitrogen oxides.
  • the nitrous oxide decomposition catalyst of the present invention can recover its activity by activating regeneration even when it is deteriorated by the volatile anesthetic contained in the excess anesthetic gas. Moreover at a relatively low temperature can decompose nitrous oxide, less subject to deactivation due to water even when water coexists, it is possible to suppress the generation amount of the NO x to less than the allowable concentration, conventional cracking catalysts respect, it is possible to reduce the generation amount of the NO x to about 1 / 10-1 / 100 following levels.
  • the nitrous oxide decomposition catalyst of the present invention contains at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium as an essential component, and is any one of the following (1) to (3) A catalyst can be used.
  • a catalyst comprising (a) at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium on a carrier selected from silica or silica alumina.
  • the silica support includes (a) at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium, (b) aluminum, and (c) at least one metal selected from the group consisting of zinc, iron and manganese. And a catalyst.
  • the support used for the catalyst of (1) is silica or silica alumina, and these supports are not particularly limited, but those having a surface area of about 50 to 300 m 2 / g can be used.
  • the carrier used for the catalyst of (2) is silica and is not particularly limited, but those having a surface area of about 50 to 300 m 2 / g can be used. Although there is no restriction
  • At least one metal selected from the group (c) consisting of zinc, iron and manganese is preferably contained in an amount of 0.1 to 5.0% by mass of the total catalyst mass, more preferably Is preferably contained in an amount of 0.2 to 1.0% by mass. Even if the metal selected from the group (c) is contained in an amount of 5.0% by mass or more based on the total mass of the catalyst, the effect may be saturated.
  • the aluminum supported on the silica support is preferably contained in an atomic ratio of at least 2 to at least one metal selected from the group (c) consisting of zinc, iron and manganese. Further, it is preferable that at least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group (c), and the spinel crystalline composite oxide includes, for example, aluminum, zinc, iron And can be produced by firing a support on which at least one metal selected from the group consisting of manganese is supported.
  • a spinel structure is a structure found in an oxide having a chemical formula of XY 2 O 4 , belongs to a cubic system, and Al, Zn, Fe, and Mn are ZnAl 2 O 4 , FeAl 2 O 4 , and MnAl 2 O, respectively. It is known to form four spinel structures.
  • at least a part of aluminum is a part or all of at least one metal selected from the group (c) and a spinel-type crystalline composite oxide. It is considered that by forming, the effect of improving the resolution of nitrous oxide and reducing the amount of NO x generated is exhibited.
  • the carrier used for the catalyst of (3) is silica alumina and is not particularly limited, but those having a surface area of about 50 to 300 m 2 / g can be used.
  • the at least one metal selected from the group (d) consisting of magnesium, zinc, iron and manganese supported on the silica-alumina carrier is preferably contained in an amount of 0.1 to 5.0% by mass of the total catalyst mass, and more preferably Is preferably contained in an amount of 0.2 to 1.0% by mass. Even if the metal selected from the group (d) is contained in an amount of 5.0% by mass or more of the entire catalyst mass, the effect may be saturated.
  • the aluminum contained in the catalyst is preferably contained in an atomic ratio of at least 2 to at least one metal selected from the group (d) consisting of magnesium, zinc, iron and manganese. Further, it is preferable that at least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group (d).
  • the spinel type crystalline composite oxide can be produced by supporting at least one metal selected from the group (d) on a silica alumina support and firing the support.
  • the at least one noble metal selected from the group (a) consisting of rhodium, ruthenium and palladium contained in the nitrous oxide decomposition catalyst of the present invention may be any of the above-mentioned catalysts (1) to (3).
  • the content is preferably 0.05 to 10% by mass, more preferably 0.1 to 6.0% by mass based on the total mass of the catalyst.
  • nitrous oxide decomposition catalyst of this invention is demonstrated.
  • Various production methods can be used for the nitrous oxide decomposition catalyst of the present invention.
  • methods such as (1) impregnation method, (2) coprecipitation method, and (3) kneading method can be used.
  • a method for producing the catalyst (2) using the impregnation method will be described, but it is needless to say that the present invention is not limited thereto.
  • the method of producing the catalyst of (2) using the impregnation method can include the following three steps. [1] A step of supporting (b) aluminum and (c) at least one metal selected from the group consisting of zinc, iron and manganese on a silica support. [2] A step of calcining the carrier obtained from step [1] at 400 to 900 ° C. [3] A step of (a) supporting at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium on the calcined carrier obtained from the step [2].
  • step [1] an inorganic acid salt of aluminum and at least one metal inorganic acid salt selected from the group (c) consisting of zinc, iron and manganese (nitrate, hydrochloride, sulfate, etc.) Alternatively, impregnation with an organic acid salt (oxalate, acetate, etc.).
  • both the aluminum and the salt of at least one metal selected from the group (c) are nitrates.
  • the amount of aluminum and at least one metal selected from group (c) supported on the carrier is preferably such that aluminum is supported at an atomic ratio of at least 2 with respect to at least one metal selected from group (c).
  • the supported amount of at least one metal selected from the group (c) is 0.1 to 5.0% by mass of the entire catalyst mass.
  • the support is dried and further subjected to calcination step [2] to contain at least one metal selected from the group consisting of aluminum and group (c).
  • a carrier in which a part forms a spinel crystalline composite oxide with at least one metal selected from the group (c) consisting of zinc, iron and manganese can be obtained.
  • the drying temperature after step [1] is not particularly limited, but is preferably in the temperature range of 80 to 150 ° C, more preferably in the temperature range of 100 to 130 ° C.
  • the drying atmosphere is not particularly limited, but air is preferably used.
  • the drying time is not particularly limited, but when using the impregnation method, it may usually be about 2 to 4 hours.
  • the firing step [2] can be performed in a temperature range of 400 to 900 ° C., preferably 500 to 700 ° C.
  • the firing time is not particularly limited, but may be about 1 to 10 hours, preferably about 2 to 4 hours, and the firing temperature may be changed stepwise. Long-time firing may be saturated economically because the effect may be saturated, and short-time firing may be less effective.
  • baking can be performed using a baking furnace, a muffle furnace, etc., and any of nitrogen or air may be used as a distribution gas at this time.
  • At least a part of the aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group (c) consisting of zinc, iron and manganese.
  • a salt of at least one noble metal selected from the group (a) consisting of rhodium, ruthenium and palladium As the salt of at least one noble metal selected from the group (a), an inorganic acid salt (nitrate, hydrochloride, sulfate, etc.) or an organic acid salt (oxalate, acetate, etc.) can be used. Preference is given to using the nitrate salt.
  • the step [3] is performed on the support obtained in the step [2] in which at least a part of aluminum forms a spinel crystalline complex oxide with at least one metal selected from the group (c). Although it is preferable, it may be performed simultaneously with the step [1]. In that case, the process [1] and the process [3] are performed at the same time, and then the process [2] is performed. At least a part of the aluminum is at least one metal selected from the group (c) and the spinel crystalline composite. It is preferable to form an oxide. In any case, it is preferable that the supported amount of at least one noble metal selected from the group (a) consisting of rhodium, ruthenium and palladium is 0.05 to 10% by mass based on the total mass of the catalyst. .
  • the catalyst precursor subjected to step [3] is dried under the same drying conditions as described above.
  • the dried catalyst precursor is preferably subjected to a reduction treatment, and a catalyst containing at least one noble metal selected from the group (a) having high activity can be obtained by the reduction treatment.
  • the reduction treatment can be performed by, for example, (1) a method of re-drying after hydrazine reduction and firing, or (2) a method of hydrogen reduction, and a method of hydrogen reduction is preferably used.
  • the reduction temperature is preferably 200 to 500 ° C., more preferably 300 to 400 ° C.
  • the reduction time is not particularly limited, the treatment can be performed in about 1 to 10 hours, preferably about 2 to 4 hours.
  • the dried catalyst precursor may be calcined in nitrogen or air without the reduction treatment (1) or (2).
  • the firing temperature at this time is preferably 200 to 500 ° C., more preferably 300 to 400 ° C.
  • the nitrous oxide decomposition method of the present invention includes the following four methods.
  • the nitrous oxide decomposition method (1) of the present invention is characterized in that a gas containing nitrous oxide is brought into contact with the catalyst at 200 to 600 ° C.
  • the nitrous oxide decomposition method (2) of the present invention is a catalyst in which at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium is supported on a support made of silica or silica alumina. Yes, the gas containing nitrous oxide and the catalyst are brought into contact with each other at 200 to 600 ° C.
  • the supply of the gas containing nitrous oxide is stopped and 500 ° C. It is characterized by restarting the supply of gas containing nitrous oxide after heating to ⁇ 900 ° C. to activate and regenerate the catalyst.
  • the catalyst is silica and the support includes (a) at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium, and (b) aluminum. And (c) a catalyst carrying at least one metal selected from the group consisting of zinc, iron and manganese, contacting the gas containing nitrous oxide with the catalyst at 200 to 600 ° C. for decomposition
  • the supply of the gas containing nitrous oxide is stopped and heated to 500 ° C. to 900 ° C., and the catalyst is activated and regenerated. The supply is resumed.
  • the catalyst is a silica alumina carrier, and (a) at least one noble metal selected from the group consisting of rhodium, ruthenium and palladium, and (D) A catalyst which carries at least one metal selected from the group consisting of magnesium, zinc, iron and manganese, which is brought into contact with the gas containing nitrous oxide at 200 to 600 ° C. for decomposition.
  • the supply of the gas containing nitrous oxide is stopped and heated to 500 ° C. to 900 ° C., and the catalyst is activated and regenerated. The supply is resumed.
  • the contact temperature between the nitrous oxide-containing gas and the decomposition catalyst is 200 to 600 ° C., preferably 300 to 500 ° C., more preferably 350 ° C. to 450 ° C. It is desirable to do.
  • the contact temperature is lower than 200 ° C., decomposition of nitrous oxide may not be sufficient, and when it is 600 ° C. or higher, the catalyst life tends to be short.
  • the catalyst bed system is not particularly limited, but a fixed bed can be employed.
  • the concentration of nitrous oxide contained in the exhaust gas discharged from factories and incineration facilities is usually 1000 ppm or less, but it is discharged by the surplus anesthetic gas exclusion device in the operating room.
  • the concentration of nitrous oxide is very high, about 8-50%.
  • 13 to 20% of oxygen is usually present in the excess anesthetic gas, it is a severe condition for the decomposition catalyst. If heat removal is possible and the temperature can be controlled, the concentration of nitrous oxide contacted with the cracking catalyst is not particularly limited.
  • nitrous oxide The concentration is preferably 50% or less, preferably 25% or less, and more preferably about 5%.
  • Space velocity is the amount of gas supplied per unit catalyst (Space Velocity) is preferably in the range of 10hr -1 ⁇ 20000hr -1, more preferably from 100 hr -1 ⁇ 10000 hr -1 is preferred.
  • the gas containing nitrous oxide may contain a volatile anesthetic, but the nitrous oxide decomposition catalyst of the present invention is not easily poisoned by the volatile anesthetic and is also poisoned by the volatile anesthetic. Even when the catalytic activity is reduced due to the above, by using the decomposition method of the present invention, the catalytic activity can be recovered and nitrous oxide can be decomposed over a long period of time. Therefore, when a decrease in the activity of the nitrous oxide decomposition catalyst is observed, the supply of the gas containing nitrous oxide is once stopped, the catalyst is activated to regenerate by calcination, and then the nitrous oxide is contained. The supply of gas can be resumed.
  • the calcination treatment for activating and regenerating the catalyst can be performed at a temperature of 500 to 900 ° C., preferably a decomposition catalyst whose activity is reduced at a temperature of 600 to 800 ° C., more preferably 650 to 750 ° C. .
  • an inert gas such as helium or nitrogen or air can be circulated through the catalyst layer, and oxygen may be contained in the inert gas. It is convenient and preferable to use air.
  • the firing treatment time is 10 minutes to 12 hours, preferably 20 minutes to 6 hours, more preferably about 30 minutes to 2 hours.
  • the catalyst supporting at least one noble metal selected from the group (a) consisting of rhodium, ruthenium and palladium
  • the catalyst is less susceptible to poisoning by volatile anesthetics and the activity of the catalyst is easily recovered. It is a catalyst containing ruthenium, and there is a tendency that the activity decreases in the order of rhodium and palladium. Therefore, it is desirable to use at least ruthenium as the noble metal component selected from the group (a). Further, after the baking treatment, a reduction treatment with hydrogen may be performed.
  • the catalyst used in the decomposition method (3) of the present invention comprises at least one metal selected from the group (c) consisting of zinc, iron, and manganese among the components supported on the silica support, in an amount of 0.1% of the total catalyst mass. It is preferably contained in an amount of ⁇ 5.0% by mass, more preferably 0.2-1.0% by mass. Even if the metal selected from the group (c) is contained in an amount of 5.0% by mass or more based on the total mass of the catalyst, the effect may be saturated.
  • the aluminum supported on the silica support is preferably contained in an atomic ratio of at least 2 to at least one metal selected from the group (c) consisting of zinc, iron and manganese. Further, it is preferable that at least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group (c), and the spinel crystalline composite oxide includes, for example, aluminum, zinc, iron And can be produced by firing a support on which at least one metal selected from the group consisting of manganese is supported.
  • the catalyst used in the decomposition method (4) is a catalyst comprising at least one metal selected from the group (d) consisting of magnesium, zinc, iron and manganese supported on a silica-alumina carrier in an amount of 0.1 to The content is preferably 5.0% by mass, more preferably 0.2 to 1.0% by mass. Even if the metal selected from the group (d) is contained in an amount of 5.0% by mass or more of the entire catalyst mass, the effect may be saturated.
  • aluminum is contained in an atomic ratio of at least 2 with respect to at least one metal selected from the group (d) consisting of magnesium, zinc, iron and manganese. Further, it is preferable that at least a part of aluminum forms a spinel crystalline composite oxide with at least one metal selected from the group (d).
  • the spinel type crystalline composite oxide can be produced by supporting at least one metal selected from the group (d) on a silica alumina support and firing the support.
  • At least one noble metal selected from the group (a) consisting of rhodium, ruthenium and palladium contained in the catalyst used in the nitrous oxide decomposition method of the present invention is any of the decompositions (1) to (4) above Even when the method is used, it is preferably contained in an amount of 0.05 to 10% by mass, more preferably 0.1 to 6.0% by mass based on the total mass of the catalyst. Although it is possible to improve the catalytic activity at low temperature by increasing the amount of at least one noble metal selected from the group (a), it is not preferable to support 10% by mass or more in view of the cost of the catalyst, Further, if it is 0.05% by mass or less, sufficient nitrous oxide decomposition activity may not be obtained.
  • a catalyst for decomposing nitrous oxide made by Showa Denko KK, alumina carrier (manufactured by JGC Universal Co., Ltd.) with 5% rhodium and 1% zinc, granular, average particle size: 3 .2 mm
  • 2.12 g (4 ml) decomposition reactor nickel reaction tube, 1/2 inch diameter, catalyst layer height 57 mm
  • the nitrous oxide gas was decomposed while supplying a nitrous oxide (N 2 O) gas having a concentration of 100% by downflow to the decomposition reactor.
  • the flow rate was adjusted in a range of 20 to 2422 cc / min by a flow rate adjusting valve. Then, the linear velocity (LV: Linear Velocity) [m / min] and the space velocity (SV) [hr ⁇ 1 ] of the nitrous oxide gas supplied to the decomposition reactor at that time are measured, and The maximum value max [° C.] of the exothermic temperature (catalyst temperature) in the reaction vessel after decomposing the nitrogen oxide gas was measured with a temperature measuring device. Further, the amount of the NO X after decomposing nitrous oxide gas [ppm] was measured to determine the degradation rate of the nitrous oxide gas [%].
  • LV Linear Velocity
  • SV space velocity
  • Table 1 shows a summary of the measurement results. Moreover, the graph which put together the relationship between the linear velocity (LV) of nitrous oxide gas, the exothermic temperature in reaction container, and the decomposition rate of nitrous oxide gas from the measurement result of Table 1 is shown in FIG.
  • nitrous oxide has the same decomposition rate (98.7%) as that during heating while maintaining the heat generation temperature in the reaction vessel by the decomposition heat generated by the decomposition of nitrous oxide gas even after the heater is stopped. It turns out that the decomposition of the gas can be continued. For this reason, about 1 hour (hr) after the heater stopped, the supply of the nitrous oxide gas was stopped and the decomposition of the nitrous oxide gas was forcibly terminated. From this, it was found that the decomposition heat generated by the decomposition of the nitrous oxide gas can continue the decomposition of the nitrous oxide gas supplied thereafter without heating by the heater.
  • nitrous oxide by using energy generated by decomposition of nitrous oxide, it is possible to use nitrous oxide as energy friendly to the global environment. Further, since nitrous oxide is finally decomposed into nitrogen and oxygen as a decomposition gas, this decomposition gas can be utilized as a new resource. Furthermore, since nitrous oxide can also be industrially produced, its industrial utility value is very high in the present invention.
  • nitrous oxide is a stable gas at normal temperature and atmospheric pressure, and since it has low toxicity, it is highly safe and easy to handle.
  • a liquefied high-pressure gas filled in a high-pressure gas container it can be easily transported and stored before decomposition.
  • nitrous oxide has a low melting point (about ⁇ 90 ° C.) and does not freeze in outer space. Therefore, nitrous oxide does not stop its use on the earth, and other celestial bodies (such as the moon and Mars) and outer space (for example, It can also be used on a space station or spaceship.
  • nitrous oxide can be decomposed into nitrogen and oxygen, for example, in the space environment such as a space station and a spacecraft, and in the sea environment such as a submarine station and a submarine, energy required for space activities and underwater activities is obtained. It can be used not only as a supply source, but also as a supply source of respiratory gas necessary for life support.
  • oxygen obtained by decomposing nitrous oxide can be combined with an appropriate fuel such as hydrogen or methanol to be used for a fuel cell (primary cell), for example. Further, it can be combined with a battery (secondary battery) or the like.
  • Nitrogen gas on-off valve 33 Nitrogen gas supply source 33a ... High pressure gas container DESCRIPTION OF SYMBOLS 100,100A ... Absorption-type heat pump (heat transport apparatus) 101 ... Refrigerant circulation system 102 ... Absorption liquid circulation system 103 ... Condensing part 103a ... Condensing chamber 103b ... Condenser 104 ... Evaporating part 104a ... Evaporating chamber 104b ... Evaporator 105 ... Absorption section 105a ... Absorption chamber 106 ... Regeneration section 106a ... Regeneration chamber 107a-107e ... First to fifth pipes 108 ... Radiator 109 ... Heat pipe 110 ... Heat absorber 111 ...
  • Heat pipe 112 Heater (heating means) 113 ... cooler (cooling means) 114 ... cooler (cooling means) 112a, 113a, 114a ... heat sink (fin) 115 ... first supply line 116 ... second supply line 117 ... third supply line 118 ... discharge line R ... Refrigerant A ... Absorbing liquid W, C ... Cooling liquid TH ... Hot air TL ... Cold air

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Abstract

L'invention concerne un appareil de transport de chaleur et un procédé de transport de chaleur au moyen desquels de l'oxyde nitreux peut être utilisé comme source d'énergie respectueuse de l'environnement. L'appareil de l'invention comprend: un système de circulation de réfrigérant (101) dans lequel un réfrigérant (R) est mis en circulation; un système de circulation de solution d'absorption (102) raccordé au système de circulation de réfrigérant (101) et dans lequel une solution d'absorption (A) du réfrigérant (R) est mis en circulation; un condenseur (103) pour condenser le réfrigérant (R) dans le système de circulation de réfrigérant (101) et, ce faisant, dégager la chaleur de l'agent frigorigène (R); un évaporateur (104) pour évaporer le réfrigérant (R) dans le système de circulation de réfrigérant (101) et, ce faisant, faire absorber la chaleur par le réfrigérant (R); une unité d'absorption (105) pour faire absorber le réfrigérant (R) évaporé par la solution d'absorption (A) dans le système de circulation de solution d'absorption (102); et une unité de récupération (106) pour évaporer le réfrigérant (R) absorbé de la solution d'absorption (A) dans le système de circulation de solution d'absorption (102). Un moyen de chauffage (112) est prévu dans l'unité de récupération (106) pour chauffer la solution d'absorption (A). Le moyen de chauffage (112) accomplit le chauffage en utilisant l'exotherme de décomposition généré par la décomposition d'oxyde nitreux.
PCT/JP2012/054360 2012-02-23 2012-02-23 Appareil de transport de chaleur, et procédé de transport de chaleur WO2013125000A1 (fr)

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH054027A (ja) * 1991-06-28 1993-01-14 Asahi Chem Ind Co Ltd 排一酸化二窒素ガスの処理方法
JPH05285344A (ja) * 1992-04-06 1993-11-02 Osaka Gas Co Ltd 窒素酸化物含有ガスの処理方法
JP2002513907A (ja) * 1998-05-07 2002-05-14 クライオジェン インコーポレイテッド ジュール−トムソンプローブ用の予冷システム
JP2002172171A (ja) * 2000-09-27 2002-06-18 Showa Denko Kk 余剰麻酔ガスの処理方法及び処理装置
JP2005230795A (ja) * 2004-01-21 2005-09-02 Asahi Kasei Chemicals Corp 亜酸化窒素の分解方法およびその反応器
JP2006073416A (ja) * 2004-09-03 2006-03-16 Kansai Electric Power Co Inc:The 吸収式冷凍機複合型燃料電池システム
JP4232820B2 (ja) * 2006-12-06 2009-03-04 独立行政法人 宇宙航空研究開発機構 亜酸化窒素を用いたスラスタ装置

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH054027A (ja) * 1991-06-28 1993-01-14 Asahi Chem Ind Co Ltd 排一酸化二窒素ガスの処理方法
JPH05285344A (ja) * 1992-04-06 1993-11-02 Osaka Gas Co Ltd 窒素酸化物含有ガスの処理方法
JP2002513907A (ja) * 1998-05-07 2002-05-14 クライオジェン インコーポレイテッド ジュール−トムソンプローブ用の予冷システム
JP2002172171A (ja) * 2000-09-27 2002-06-18 Showa Denko Kk 余剰麻酔ガスの処理方法及び処理装置
JP2005230795A (ja) * 2004-01-21 2005-09-02 Asahi Kasei Chemicals Corp 亜酸化窒素の分解方法およびその反応器
JP2006073416A (ja) * 2004-09-03 2006-03-16 Kansai Electric Power Co Inc:The 吸収式冷凍機複合型燃料電池システム
JP4232820B2 (ja) * 2006-12-06 2009-03-04 独立行政法人 宇宙航空研究開発機構 亜酸化窒素を用いたスラスタ装置

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