[go: up one dir, main page]

US20050072152A1 - Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, nd method for generating electric power - Google Patents

Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, nd method for generating electric power Download PDF

Info

Publication number
US20050072152A1
US20050072152A1 US10/501,794 US50179404A US2005072152A1 US 20050072152 A1 US20050072152 A1 US 20050072152A1 US 50179404 A US50179404 A US 50179404A US 2005072152 A1 US2005072152 A1 US 2005072152A1
Authority
US
United States
Prior art keywords
hydrogen
steam
heat
gas
raw material
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Abandoned
Application number
US10/501,794
Other languages
English (en)
Inventor
Minoru Suzuki
Katsuhiro Iwasaki
Takashi Nakayama
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
JFE Engineering Corp
JEE Engr Corp
Original Assignee
JEE Engr Corp
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from JP2002118427A external-priority patent/JP2003313002A/ja
Priority claimed from JP2002212330A external-priority patent/JP4051668B2/ja
Priority claimed from JP2002376249A external-priority patent/JP2004202412A/ja
Application filed by JEE Engr Corp filed Critical JEE Engr Corp
Assigned to JFE ENGINEERING CORPORATION reassignment JFE ENGINEERING CORPORATION ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: IWASAKI, KATSUHIRO, NAKAYAMA, TAKAHASHI, SUZUKI, MINORU
Publication of US20050072152A1 publication Critical patent/US20050072152A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/466—Entrained flow processes
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/04—Cyclic processes, e.g. alternate blast and run
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/78—High-pressure apparatus
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0979—Water as supercritical steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a method for producing hydrogen and a hydrogen-containing fuel gas by subjecting a raw material, such as waste, to chemical reaction using a shock wave which is generated by instantaneously releasing a high-pressure gas prepared using relatively low-temperature waste heat energy discharged from various types of heat processes including waste incineration plants, and to an apparatus for producing hydrogen, a hydrogen supply plant, and a method for generating electric power by burning a hydrogen-containing gas.
  • an environment-conscious method for example, Japanese Unexamined Patent Application Publication No. 2000-272904, pp. 3-4, FIG. 1 , hereinafter referred to as “prior art 1” may be applied to the hydrogen production process, which uses a heating furnace-type, double tube-type steam reforming reactor partitioned with a wall having a specific hydrogen separation membrane.
  • hydrocarbon as a raw material and steam are fed into one part of the double tube filled with a catalyst to perform a reforming reaction, and gas discharged from this part is cooled to be separated into a gas phase and a liquid phase.
  • the resulting hydrogen is allowed to flow continuously into the other part of the double tube through the hydrogen separation membrane.
  • a part of the hydrogen is fed into the heating furnace together with oxygen to burn, so that heat is applied to the reforming reactor.
  • a mixture of steam and hydrocarbon as a raw material such as natural gas and propane gas is brought into contact with a high-temperature reforming catalyst in a reactor to be reformed into gas that contains hydrogen and carbon monoxide, and the hydrogen is separated from the reformed gas.
  • prior art 1 the reactant being a mixture of the raw material and steam must be heated to a high temperature of at least 450° C. in order to perform a reforming reaction of high-temperature steam. Accordingly, prior art 1 requires a constantly available heat source of at least 620° C., generally about 80l ° C., and a fuel for the heat source. This produces not only the problem of consuming fuel inevitably, but also the problem of generating carbon dioxide due to the combustion of the fuel. In addition, since the reactor must maintain a constantly high-temperature field, it is required that at least the internal wall of the reactor is formed of expensive fire-resistant material, and consequently there occurs a problem that the investment cost becomes higher.
  • the apparatus since the temperature in the reactor is maintained high over a long period from the startup time to the suspension time, the apparatus is required to be constituted of a large amount of refractories, and consequently the investment cost becomes undesirably higher. Also, since natural gas or propane gas is used as a raw material, the running cost that is spent on the apparatus increases. Furthermore, carbon dioxide is emitted to an extent of an amount as much as equal or more than an amount of the produced hydrogen. Therefore, from the standing point of preventing global warming, the above-mentioned emission, which has been a worldwide problem in the recent years, is unfavorable.
  • the present invention has been accomplished in order to overcome those disadvantages above.
  • the object of the invention is to provide a method and an apparatus for producing hydrogen and a hydrogen supply plant.
  • the method, apparatus, and plant perform hydrogen production, which requires high temperature, at a low cost using relatively low-temperature waste heat energy discharged from various types of heat processes, and the hydrogen production apparatus is so easy to start and suspend the operation as to reduce running cost and facility cost.
  • the present invention provides the following:
  • a method for producing hydrogen comprising:
  • a method for producing hydrogen comprising:
  • a method for producing hydrogen comprising:
  • the heat source is at least one of heat generating sources installed in thermal power plants, waste incineration plants, waste disposal plants, pig iron making facilities of ironworks, steel making facilities of ironworks, scrap melting facilities, nonferrous metal refining facilities, cement firing facilities, combustion facilities, and facilities using geothermal heat.
  • the heat source is a combustion facility which generates steam from heat generated therefrom and which uses the steam for electric power generation.
  • the heat source is a combustion facility which generates steam from heat generated therefrom and which uses the steam for electric power generation, and the high-pressure gas is surplus steam.
  • An apparatus for producing hydrogen comprising:
  • An apparatus for producing hydrogen comprising:
  • An apparatus for producing hydrogen comprising:
  • the heat source is at least one of heat generating sources installed in thermal power plants, waste incineration plants, waste disposal plants, pig iron making facilities of ironworks, steel making facilities of ironworks, scrap melting facilities, nonferrous metal refining facilities, cement firing facilities, combustion facilities, and facilities using geothermal heat.
  • the apparatus for producing hydrogen according to any one of above 8, 9, and 10 further comprises a separator for separating the hydrogen from other products.
  • the heat source is a combustion facility which generates steam from heat generated therefrom and which uses the steam for electric power generation.
  • the heat source is a combustion facility which generates steam from heat generated therefrom and which uses the steam for electric power generation, and the high-pressure gas is surplus steam.
  • a hydrogen supply plant comprising:
  • a hydrogen supply plant comprising:
  • the heat source is a combustion facility which generates steam from heat generated therefrom and which uses the steam for electric power generation, and at least part of the steam is used for hydrogen production when hydrogen supply is required.
  • a method for generating electric power comprising the steps of:
  • a method for generating electric power comprising the steps of:
  • the method for generating electric power according to above 18 or 19 further comprises the steps of:
  • a method for producing hydrogen comprising the steps of:
  • the method according to above 21 further comprises the step of feeding the steam as a high-pressure gas into the compression chamber.
  • the reactive particles comprise one selected from the group consisting of waste plastic powder, sprayed particles of melted plastic, powdered coal, and coke breeze.
  • An apparatus for producing hydrogen in which a mixture of reactive particles containing a hydrocarbon or carbon and steam is heated to a high temperature to react, thereby producing gas that contains hydrogen and in which the hydrogen is separated from the gas that contains the hydrogen, the apparatus comprising:
  • the apparatus for producing hydrogen according to above 24 further comprises:
  • the apparatus for producing hydrogen according to above 24 or 25 further comprises steam feeding means through which the shock wave generating means accommodates the steam generated by a waste heat boiler as the high-pressure gas in the gas accommodation chamber.
  • the apparatus for producing hydrogen according to any one of above 24, 25, and 26 further comprises a Laval nozzle, a gas tank, a filter apparatus, and a hydrogen separator.
  • FIG. 1 is a structural block diagram of a hydrogen production apparatus according to Embodiment 1 of the present invention.
  • FIG. 2 is a sectional view of the hydrogen production apparatus shown in FIG. 1 .
  • FIG. 3 is a timing chart of the hydrogen production apparatus according to Embodiment 1 of the present invention.
  • FIG. 4 is a structural block diagram of a hydrogen production apparatus according to Embodiment 2 of the present invention.
  • FIG. 5 is a structural block diagram of a hydrogen production facility according to Embodiment 4 of the present invention.
  • FIG. 6 is a structural block diagram of an electric power generation facility burning gas that contains hydrogen according to Embodiment 5 of the present invention.
  • FIG. 7 is a schematic diagram of the structure of a hydrogen production apparatus according to Embodiment 6 of the present invention.
  • FIG. 8A is a schematic illustration showing the structure of a compression chamber provided in the hydrogen production apparatus shown in FIG. 7 .
  • FIG. 8B is a cross-sectional view taken along line I-I in FIG. 8A .
  • FIG. 9 is a sectional view of a shock wave generator for producing hydrogen according to an embodiment of the present invention.
  • FIG. 10 is a structural diagram of a combination of the shock wave generator shown in FIG. 9 and a hydrogen production apparatus connected to each other.
  • FIG. 11 is a diagram showing the operation sequence of the apparatus shown in FIG. 10 .
  • FIG. 12A shows one of the motions of the shock wave generator in order of the operation sequence shown in FIG.
  • FIG. 12B shows another one of the motions of the shock wave generator in order of the operation sequence shown in FIG. 11 .
  • FIG. 12C shows another one of the motions of the shock wave generator in order of the operation sequence shown in FIG. 11 .
  • FIG. 12D shows another one of the motions of the shock wave generator in order of the operation sequence shown in FIG. 11 .
  • FIG. 1 is a structural block diagram of an apparatus for producing hydrogen according to Embodiment 1 of the present invention
  • FIG. 2 is a sectional view of a reactor of the hydrogen production apparatus.
  • reference numeral 1 designates a reactor of a hydrogen production apparatus 20 conducting a reaction in which reactive particles containing hydrocarbon or carbon react with steam at a high temperature to produce hydrogen.
  • the reactor includes a converging tube 2 having a converging portion 2 A with a larger diameter at the upper end and a smaller diameter at the lower end and the cross section of the converging tube 2 thus decreases gradually from the upper end to the lower end.
  • a space at the downstream side of the converging tube 2 defines a compression chamber 3 serving as a reaction chamber.
  • High-pressure steam is instantaneously released to the converging tube 2 to generate shock waves, and the shock waves are converged in the converging portion 2 A to produce a high-temperature, high-pressure converged shock wave. Then, in the compression chamber 3 , a mixture of reactive particles and steam, described later, is impact-compressed by the converged shock wave to heat to a high temperature. Thus, the reactive particles and the steam in the mixture are allowed to react to produce gas that contains hydrogen.
  • the compression chamber 3 of the reactor 1 has a produced gas outlet 6 and an exhaust vent 7 at its bottom, and the produced gas outlet 6 and the exhaust vent 7 respectively have at their ends control valves 8 and 9 which open at predetermined time.
  • a reactive particle feeding port 10 for feeding the reactive particles into the converging tube 2 is provided at a position slightly higher than that of the produced gas outlet 6 and the exhaust vent 7 , and the reactive particle feeding port 10 has at its end a control valve 13 which opens at predetermined time.
  • Reference numeral 11 designates a heat source comprising a large heat processing facility, such as a waste incinerator
  • reference numeral 12 designates a boiler serving as a heat exchanger which recovers the waste heat of exhaust gas from the heat source 11 and which heats a fluid (for example, water) by exchanging heat to generate high-pressure steam being high-pressure gas.
  • the boiler 12 is connected to the upstream side of the reactor 1 and feeds the high-pressure steam into the converging tube 2 of the reactor 1 .
  • the heat source 11 is a heat generating source installed in thermal power plants, waste incineration plants, waste disposal plants, pig iron making facilities of ironworks, steel making facilities of ironworks, scrap melting facilities, nonferrous metal refining facilities, cement firing facilities, combustion facilities, and facilities using geothermal heat.
  • the boiler 12 serving as a heat exchanger heats water (fluid) to generate high-pressure steam by use of exhaust gas from combustion apparatuses, incinerators, blast furnaces, steel converters, lime firing, coke ovens, sintering apparatuses, cupolas, and so forth of those heat generating sources.
  • Reference numeral 14 designates a feeder for separating a raw material containing hydrocarbon or carbon from the other materials and crushing the raw material to pulverize it into reactive fine particles, and for feeding the reactive particles to the reactor 1 .
  • the feeder 14 is connected to the upstream side of the reactive particle feeding port 10 of the reactor 1 and feeds the pulverized reactive particles through the control valve 13 at predetermined time.
  • Reference numeral 15 designates a dust collector for removing impurities, such as unreacted reactive particles, halides and sulfur compounds, from the hydrogen-containing gas generated in the reactor 1 .
  • the dust collector is connected to the downstream side of the produced gas outlet 6 of the reactor 1 and also connected to the feeder 14 so as to feed back the unreacted reactive particles for recycling.
  • Reference numeral 16 is a separator for separating the hydrogen-containing gas from the dust collector 15 into hydrogen gas and CO gas so as to allow these gases to be taken out separately, and is connected to the downstream side of the dust collector 15 .
  • the separator 16 is, for example, a pressure swing adsorption apparatus (PSA).
  • PSA pressure swing adsorption apparatus
  • Reference numeral 17 designates an exhaust pipe connected to the exhaust vent 7 via the control valve 9 and through which the steam remaining in the compression chamber 3 is discharged after the completion of the reaction in the reactor 1 .
  • the high-pressure steam has a temperature in the range of 200° C. or higher to 400° C. or lower.
  • a high-pressure steam temperature of less than 200° C. leads to a low reaction efficiency because it makes unstable the shock wave generated by instantaneously releasing the high-pressure steam, and does not allow a high-temperature, high-pressure field generated by the shock wave to reach a high temperature.
  • the high-pressure steam has a temperature in the range from 300° C. or higher to 400° C. or lower.
  • the heat source 11 is a heat process providing warm heat having a temperature in the range of 50° C. or higher to 600° C. or lower. A warm heat of less than 50° C. makes the pressure of the high-pressure steam low or insufficient. A warm heat of more than 600° C. makes the temperature of the high-pressure steam to more than 400° C., and accordingly, the facility for producing such heat becomes large and the process becomes complicated.
  • the heat source 11 provides warm heat having a temperature in the range from 50° C. or higher to 600° C. or lower so as to produce high-pressure stream having a temperature in the range from 200° C. or higher to 400° C. or lower.
  • the high-pressure steam fed into the reactor 1 has a pressure at least five times as high as the internal pressure of the reactor 1 before the reaction.
  • the shock wave is generated by instantaneously releasing the high-pressure steam into the reaction chamber (the inside of the converging tube 2 ) of the reactor 1 .
  • a pressure ratio of at least 5 of the high-pressure steam to the inside of the reactor 1 before the reaction can provide a shock wave sufficient for compressing the reactive particles and steam to heat them on its impact and thus for bringing them into a reaction.
  • the high-pressure steam has a pressure ratio of at least 10.
  • shock temperature high-temperature field
  • shock high temperature can be further increased to enhance the reaction efficiency.
  • the shock wave generated by instantaneously releasing the high-pressure steam having a pressure ratio of at least 5 to the internal pressure of the reactor 1 before the reaction may be propagated along the converging portion 2 A, whose passage cross section area gradually decreases in the direction of shock wave movement, so that a plurality of shock waves interfere with each other to generate a converged shock wave.
  • the shock high temperature can increase to a still higher level.
  • the ratio (constriction ratio) of the passage cross section area at the downstream side of the converging portion 2 A to that at the upstream side decreases, the convergence density of the shock wave increases, and consequently the shock temperature reaches a high level.
  • the reactor 1 With the inside at atmospheric pressure before the reaction easily helps sealing for preventing ambient gas and the like from interfusing into the reactor 1 (converging tube 2 ).
  • the pressure of the high-pressure steam is set in the range from 10 atmospheres or higher to 40 atmospheres or lower in order to set the pressure ratio of the high-pressure steam to the inside of the reactor 1 before the reaction in the range of 10 or higher to 40 or lower, and the temperature of the high-pressure steam is set in the range from 200° C. or higher to 400° C. or lower.
  • High-pressure steam in this temperature range corresponds to steam generated by waste heat recovery boilers, such as waste heat boilers of waste incinerators; hence, energy can be used effectively.
  • the internal pressure of the reactor 1 may be reduced before the reaction.
  • the pressure ratio can be set high even if the pressure of the high-pressure steam is not sufficiently high.
  • a blower for reducing pressure or a vacuum pump is used for reducing the internal pressure of the reactor 1 .
  • control valve 13 is opened and the reactive particles are fed into the compression chamber 3 of the reactor 1 from the reactive particle feeding port 10 through the feeder 14 .
  • the feeding of the reactive particles is stopped.
  • the gas outlet 6 and the valves 8 and 9 of the exhaust vent 7 are closed (see timing chart ( 1 ) shown in FIG. 3 ).
  • high-pressure steam is instantaneously jetted into the converging tube 2 for an extremely short time of, for example, one to several milliseconds from the boiler 12 , and the instantaneously released high-pressure steam generates shock waves.
  • the shock waves travel toward the lower end of the converging tube 2 .
  • the shock waves are merged and converged into the converging portion 2 A of the converging tube 2 to turn into a converged shock wave (see timing chart ( 2 ) shown in FIG. 3 ).
  • the converged shock wave travels to the compression chamber 3 , and rapidly compresses steam together with the reactive particles fed into the compression chamber 3 to increase temperature.
  • the reactive particles instantaneously react with the high-pressure steam to produce gas that contains hydrogen gas and CO gas due to such ultrahigh temperature.
  • the reaction for producing hydrogen is conducted through the process in which high-pressure steam having a temperature in the range of 200° C. or higher to 400° C. or lower is generated using waste heat of exhaust gas from a heat source 11 being a large heat process facility, such as a waste incinerator; the high-pressure steam is instantaneously jetted into the reactor 1 to generate shock waves; the shock waves are converged to turn into a converged shock wave; and the converged shock wave heats steam and reactive particles to a high temperature so as to react with each other.
  • low-temperature energy which is conventionally disposed of, is used effectively.
  • the converged shock wave is easily produced and used for instantaneously providing a high-temperature field, the operation of the apparatus can be easily started and suspended.
  • the method and apparatus for producing hydrogen induce hydrogen production only when hydrogen supply is required.
  • the reactor 1 produces hydrogen basically by repetition of a batch process, and accordingly the operation of the apparatus can be rapidly started and suspended.
  • the separator 16 repeats a batch operation for separating hydrogen, basically, and accordingly it can be instantaneously operated according to the variation of the heat source by, for example, varying the cycle time.
  • hydrogen is supplied readily and immediately when required, without installing an expensive hydrogen storage facility or the like.
  • the method and apparatus of the present invention provide hydrogen at a low cost.
  • the raw material and the compression chamber may be preheated in advance. In this instance, they are preheated to the degree of 200° C. or more, but it is unnecessary to heat to the degree of 600° C. or more as in the steam reformer process described in prior art 2. By preheating, reaction efficiency in the compression chamber 3 is increased and the amount of steam used is reduced.
  • Impurities contained in the reactive particles such as halides, sulfur compound, foreign matter, and other substances and compounds not involved in or inhibiting the reaction, may be removed before feeding the reactive particles, which are fed into the reactor 1 by the feeder 14 in Embodiment 1.
  • the dust collector 15 can easily remove impurities, and the reactor 1 can produce hydrogen containing few impurities.
  • Part of the CO gas produced together with hydrogen in the reactor 1 may be supplied to the reactor 1 after being separated from the hydrogen, thus reacting with steam to form a raw material for producing hydrogen.
  • the reactive particles to be fed such as powdered coal, can be saved.
  • FIG. 4 is a structural block diagram of a hydrogen production apparatus according to Embodiment 2 of the present invention.
  • the boiler 12 being a heat exchanger of the hydrogen production apparatus 20 of Embodiment 1, which recovers the waste heat of exhaust gas from the heat source 11 and which heats a fluid (for example, water) to generate high-pressure steam by heat exchange, is replaced with a heater 12 A which recovers the waste heat of exhaust gas from the heat source 11 and which heats a low-boiling-point fluid to generate high-pressure gas by heat exchange.
  • a fluid for example, water
  • the low-boiling-point fluid has a boiling point lower than that of water, and may be LNG, LPG, liquefied carbon dioxide, ammonia, DME (dimethyl ether), an alcohol, or an ether.
  • the low-boiling-point fluid itself may serve as a raw material of the reaction (hydrogen production) in some cases.
  • Embodiment 2 provides a method for producing hydrogen at a low cost in which the apparatus can start and suspend operation according to request to supply hydrogen, and an apparatus for the method.
  • the hydrogen production apparatus 20 of Embodiment 1 is installed in a predetermined site to constitute a hydrogen supply plant, and is used as, for example, a hydrogen supply source for fuel-cell vehicles.
  • the hydrogen production apparatus 20 when a fuel-cell vehicle comes in for feeding hydrogen, the hydrogen production apparatus 20 immediately starts operating to produce hydrogen and supply it into the tank of the vehicle. On completing hydrogen supply, the operation of the hydrogen production apparatus 20 is suspended. When another vehicle comes in, the hydrogen production apparatus 20 starts operation to supply hydrogen again as above.
  • the hydrogen production apparatus 20 is installed in a predetermined site to constitute a hydrogen supply plant, hydrogen is supplied to fill the object easily and immediately according to a demand for hydrogen, without providing an expensive hydrogen storage facility or the like.
  • the hydrogen supply plant supplies hydrogen at a low cost.
  • the heat source of Embodiment 3 is a combustion facility for generating electric power by generating steam from generated heat and supplying the steam to a turbine, like an incinerator of a waste incineration plant, at least part of the steam is fed into the hydrogen production apparatus and thus hydrogen can be easily produced and supplied when hydrogen supply is required.
  • the hydrogen supply plant can supply hydrogen at a low cost.
  • Embodiment 3 illustrates a hydrogen supply plant including the hydrogen production apparatus 20 according to Embodiment 1
  • the hydrogen supply plant may include hydrogen production apparatus 20 according to Embodiment 2. Such plant produces the same effects.
  • FIG. 5 is a structural block diagram of a hydrogen production apparatus according to Embodiment 4 of the present invention.
  • a large heat process facility serving as the heat source 11 of the hydrogen production apparatus 20 of Embodiment 1 is defined by a waste incineration plant including a boiler 12 , and steam generated from the waste incineration plant is used for producing hydrogen.
  • the waste incineration plant generates high-pressure steam in the boiler 12 using waste heat from an incinerator 18 for burning wastes.
  • the generated high-pressure steam is switched between the boiler 12 and the reactor 1 by a switching valve 5 , and thus fed to the reactor 1 or a steam turbine 19 described later.
  • the steam turbine 19 On feeding the steam to the steam turbine 19 , the steam turbine 19 is driven by the steam to drive a generator 21 connected to the steam turbine 19 , and thus electric power is generated.
  • a shock wave is generated in the reactor 1 , and the shock wave causes the reactive particles and steam in the reactor 1 to react to produce gas that contains hydrogen.
  • the steam after being used for driving the steam turbine 19 is recycled for a heated effluent facility or the like effectively.
  • the boiler 12 is connected to an exhaust gas-processing apparatus 22 for processing exhaust gas coming through the boiler 12 from the incinerator 18 into a state releasable to the air.
  • Exhaust gas from the incinerator 18 is drawn to the exhaust gas-processing apparatus 22 by an inducing fan 23 connected to the exhaust gas-processing apparatus 22 .
  • the exhaust gas is processed into a state releasable to the air in the exhaust gas-processing apparatus 22 and released to the air through a smokestack 24 .
  • the separator 16 which is a pressure swing adsorption apparatus (PSA) for separating hydrogen gas and CO gas from hydrogen-containing gas from which unreacted reactive particles and the like have been removed by the dust collector 15 , is connected to a hydrogen supply apparatus 25 for supplying the separated hydrogen on an as-needed basis to objects which require hydrogen, and also connected to the incinerator 18 so as to feed back the separated CO gas for effective recycling.
  • PSA pressure swing adsorption apparatus
  • a waste incineration plant serves as the heat source 11 , and at least part of the steam fed into the steam turbine 19 side and used for power generation is supplied to the reactor 1 with a switching valve 5 for switching steam supply between the reactor 1 and the steam turbine 19 , provided between the boiler 12 of the waste incineration plant and the reactor 1 and is thus used for hydrogen production.
  • a switching valve 5 for switching steam supply between the reactor 1 and the steam turbine 19 , provided between the boiler 12 of the waste incineration plant and the reactor 1 and is thus used for hydrogen production.
  • the entirety of steam is used for power generation when hydrogen supply is not required.
  • the entire amount of steam is used for power generation, and when the amount of waste increases to generate a larger amount of steam than the constant amount, the surplus steam may be used for hydrogen production.
  • variable surplus of steam generated from the boiler 12 is used effectively. Also, since an amount of heat sufficient to cause reactive particles and high-pressure steam in the reactor 1 to react can be supplied in a short time, energy loss at the startup and suspension of the operation of the apparatus can decrease. Thus, the equipment cost and running cost of the hydrogen production apparatus 20 are reduced. Furthermore, the CO gas separated by the separator 16 can be used effectively as the fuel of the incinerator.
  • Embodiment 4 at least part of the steam generated from the waste incinerator plant is supplied to the reactor 1 to operate the hydrogen production apparatus 20 only when hydrogen supply is required, product storage means for steadily supplying hydrogen in response to the changes in amount of heat generated from the heat source 11 may be provided to the dust collector 15 , the separator 16 , the hydrogen production apparatus 25 , and so forth.
  • the amount of heat generated from the heat source 11 is controlled at any time between the storage means and the reactor 1 side or the steam turbine 19 side, so that the economical efficiency of the hydrogen production apparatus 20 increases.
  • Embodiment 4 uses a waste incinerator plant as the heat source of the hydrogen production apparatus 20 according to Embodiment 1, the waste incinerator plant may be used as the heat source of the hydrogen production apparatus 20 according to Embodiment 2. Such structure also produces the same effects.
  • FIG. 6 is a structural block diagram of an electric power generation plant, which burns a hydrogen-containing gas, according to Embodiment 5 of the present invention.
  • a hydrogen-containing gas generated by the operation of the hydrogen production apparatus 20 according to Embodiment 1 is fed to a gas turbine power generator as a fuel to generate electric power.
  • High-pressure steam generated in the boiler 12 recovering waste heat from the large heat processing facility 11 is fed to the reactor 1 to generate a shock wave in the reactor 1 .
  • the shock wave causes reactive particles and steam in the reactor 1 to react to produce hydrogen-containing gas.
  • the hydrogen-containing gas produced in the reactor 1 from which unreacted reactive particles and the like are removed by the dust collector 15 also contains CO, which is used as a high-calorie fuel.
  • the hydrogen-containing gas is temporarily stored in a storage apparatus 30 , and then supplied to the gas turbine power generator 31 .
  • Power generation by burning the hydrogen-containing gas in a gas turbine significantly increases the efficiency of power generation in comparison with that of power generation by driving a steam turbine using waste heat recovered from conventional heat processes. Since the hydrogen-containing gas does not contain harmful substances unsuitable for combustion in the gas turbine, such as sulfur compounds and chlorides, pretreatment of the gas is not necessary, including removal of those harmful substances. Thus,facility cost and running cost can decrease.
  • the amount of the hydrogen gas supplied to the gas turbine can be adjusted so as to control the amount of power to be generated, according to the demand for electric power.
  • the balance between the demand and supply of electric power can be equalized.
  • power generation can be performed during time periods when the price of power is high so that profit in selling power increases.
  • the present embodiment realizes a reaction requiring high temperature at a low cost, using relatively low-temperature waste energy discharged from various types of heat processes.
  • the apparatus performing the reaction easily generates a shock wave using the relatively low-temperature waste energy and instantaneously generates a high-temperature field. Therefore it becomes easy to start and suspend the operation of the apparatus, resulting in performing the reaction of the hydrogen production, for example, only when hydrogen supply is required to be supplied.
  • the hydrogen can be produced and supplied at a low cost, simultaneously with reducing the running cost and the investment cost.
  • FIG. 7 is a schematic diagram of the structure of a hydrogen production apparatus according to Embodiment 6 of the present invention.
  • the hydrogen production apparatus of the present embodiment includes a reactor 101 for allowing to react a mixture of steam and fine powder prepared by pulverizing plastic material collected as waste (hereinafter referred to as waste plastics) or powdery waste plastics (hereinafter referred to as waste plastic powder), as shown in FIG. 7 .
  • waste plastics plastic material collected as waste
  • waste plastic powder powdery waste plastics
  • the reactor 101 is connected to a reactive particle feeder 102 for feeding the waste plastic powder into the reactor 101 .
  • the reactive particle feeder 102 includes a pulverizer 102 a for pulverizing waste plastics and a feeder 102 b for feeding the waste plastic powder prepared with the pulverizer 102 a into the reactor 101 through a high-speed switching valve 102 c.
  • the waste plastics are transferred to the pulverizer 102 a by an inert gas, such as N 2 .
  • the reactor 101 is connected to a waste heat boiler 103 a feeding steam to the reactor 101 through a high-speed valve 103 b.
  • the waste heat boiler 103 a generates steam serving as high-pressure gas, using waste heat from a combustion apparatus or heat process apparatus 108 , such as a sintering furnace, a heating furnace, or a waste incinerator.
  • a shock wave is generated by opening switching means, described below, to instantaneously release steam from the waste heat boiler 103 a.
  • the waste heat boiler 103 a and the switching means define a shock wave generator 103 and double as a steam feeder.
  • a shock wave generated by the shock wave generator 103 compresses the mixture in the reactor 101 to heat it, thereby producing hydrogen.
  • a switching member may be provided to the reactor 101 , instead of the high-speed switching valves 102 c and 103 b.
  • a Laval nozzle 104 is also connected to the reactor 101 for jetting high-pressure hydrogen-containing gas produced by a reaction of the mixture of the waste plastic powder and steam, at a high speed.
  • the Laval nozzle 104 communicates with a gas tank 105 for temporarily accommodating the hydrogen-containing gas discharged from the Laval nozzle 104 to reduce the pressure.
  • the gas tank 105 communicates with a bag filter apparatus 106 for removing unreacted reactive particles from the hydrogen-containing gas whose pressure is reduced in the gas tank 105 .
  • the bag filter apparatus 106 is connected to a pressure swing adsorption (PSA) apparatus 107 for separating hydrogen from the hydrogen-containing gas from which unreacted reactive particles have been removed by the bag filter 106 .
  • PSA pressure swing adsorption
  • the bag filter 106 is also connected to the feeder 102 b so as to feed back the removed unreacted reactive particles for recycling.
  • the pressure swing adsorption apparatus 107 is connected to the combustion apparatus or heat process apparatus 108 to feed back the carbon monoxide (CO) remaining after separation as a fuel for recycling.
  • CO carbon monoxide
  • the reactor 101 will now be further described in detail with reference to FIG. 8 .
  • FIG. 8A is a schematic illustration of the reactor 101
  • FIG. 8B is a sectional view taken along line I-I of FIG. 8A .
  • compression chambers 101 a for accommodating the mixture of the waste plastic powder and steam and impact-compressing the mixture to heat it extend along the axis of a revolution body 101 b, in a plurality of positions in the peripheral direction of the revolution body 101 b, and whose ends in the axis direction are open.
  • Switching members 101 C are provided so as to oppose the respective end surfaces in the axis direction of the revolution body 101 b with such a predetermined clearance as to allow the revolution body 101 b to revolve.
  • the spaces between the switching members 101 c and the curved surface of the revolution body 101 b are sealed with sealing members 101 e.
  • the sealing may use a labyrinth seal.
  • One of the switching members 101 c at the side from which the waste plastic powder and steam are fed (hereinafter referred to as the feeding side) is provided with two openings: one opening 101 c 1 communicates with the feeder 102 b of the reactive particle feeder 102 for feeding the waste plastic powder into the compression chamber 101 a; and the other opening 101 c 2 communicates with the waste heat boiler 103 a of the shock wave generator 103 for feeding steam into the compression chamber 101 a.
  • the other switching member 101 c at the side from which the hydrogen-containing gas is discharged (hereinafter referred to as the discharge side) is provided with the Laval nozzle 104 .
  • the revolution body 101 b is rotatably supported by a supporting member 101 d, such as a bearing, and is driven to revolve by driving means (not shown in the figures).
  • the revolution body 101 b intermittently or continuously revolves so that the opening 101 c 2 alternately opposes the openings of the compression chambers 101 a and the end surface of the revolution body 101 b at a position where the radiuses of the opening 101 c 2 and the compression chamber 101 a extend in substantially the same direction.
  • the opening 101 c 2 When the opening 101 c 2 opposes the end surface of the revolution body 101 b, the opening 101 c 2 comes into contact with the end surface of the revolution body 101 b to block the communication between the waste heat boiler 103 a and the compression chambers 101 a, and when the opening 101 c 2 opposes the opening of one of the compression chambers 101 a, the opening 101 c 2 is joined with the opening of the compression chamber 101 a to establish a communication between the compression chamber 101 a and the waste heat boiler 103 a.
  • such collaboration between the opening 101 c 2 and the end surface of the revolution body 101 b defines switching means for establishing and blocking the communication between the compression chambers 101 a and the waste heat boiler 103 a.
  • the other opening 101 c 1 is also joined with the opening of one of the other compression chambers 101 a opposite to the opening 101 c 2 in the radius direction to establish a communication between the compression chamber 101 a and the feeder 102 b.
  • such collaboration between the opening 101 c 1 and the end surface of the revolution body 101 b defines switching means for establishing and blocking the communication between the compression chamber 101 a and the feeder 102 b.
  • the Laval nozzle 4 is joined with the opening of the compression chamber 101 a at the discharge side to establish a communication between the compression chamber 101 a and the gas tank 105 when the opening 101 c 2 opposes the end surface of the revolution body 101 b.
  • the waste plastic powder is intermittently or continuously fed into the plurality of compression chambers 101 a from the feeder 102 b from one after another when the opening 101 c 1 opposes the opening of the compression chamber 101 a during revolution of the revolution body 101 b, and steam is fed into the compression chamber 101 a to which the waste plastic powder has been fed when the opening of the compression chamber 101 a opposes the opening 101 c 2 after the revolution body 101 a has taken a turn of 180°.
  • the opening 101 c 2 closed by the end surface of the revolution body 101 b comes to the position opposing the opening of the compression chamber 101 a to establish a communication
  • the high-pressure steam from the waste heat boiler 103 a is instantaneously released.
  • the steam jetted from the opening 101 c 2 turns into a shock wave and propagates in the compression chamber 101 a.
  • waste plastic powder is fed into the compression chamber 101 a communicating with the opening 101 c 1 through the high-speed switching valve 102 c by the feeder 102 b of the reactive particle feeder 102 .
  • the waste plastic powder is prepared by pulverizing waste plastics with the pulverizer 102 a and fed into the feeder 102 b.
  • the waste plastics are transferred to the pulverizer 102 a by an inert gas, such as N 2 .
  • the reactive particles may comprise coke breeze or powdered coal, and such coke breeze or powdered coal may be fed into the feeder 2 b, instead of waste plastic powder.
  • the revolution body 101 b turns and establishes a communication between the opening 101 c 2 and the compression chamber 101 a to which the waste plastic powder has been fed.
  • the opening 101 c 2 closed by the opposing end surface of the revolution body 101 b is instantaneously opened to establish a communication with the compression chamber 101 a, and thereby high-pressure steam from the waste heat boiler 103 a is instantaneously released to turn into a shock wave.
  • the shock wave is thus fed into the compression chamber 101 a and propagated.
  • the steam in the waste heat boiler 103 a for example, has a temperature of 400° C. and a pressure of 4 MPa.
  • the waste plastic powder On propagating the shock wave of the high-pressure steam into the compression chamber 101 a containing the waste plastic powder, the waste plastic powder is heated by compression against an end of the compression chamber 101 a on the impact of the shock wave, thereby reacting with the steam to produce a hydrogen-containing gas.
  • the mixture in the compression chamber 101 a has a temperature of 1500° C. and a pressure of 4 MPa.
  • the waste plastic powder is generally expressed by the chemical formula C 2n H 4n
  • the reaction in the compression chamber 101 a is principally expressed by C 2n H 4n +2nH 2 O ⁇ 2nCO+4nH 2 .
  • the hydrogen-containing gas produced in the compression chamber 101 a is jetted into the gas tank 105 through the Laval nozzle 104 provided to the reactor 101 , and thus temporarily accommodated.
  • the high-pressure hydrogen-containing gas jetted from the Laval nozzle 104 is rapidly cooled while being heat-insulated, counterreaction is prevented.
  • the gas tank 105 has a relatively large space, the high-pressure hydrogen-containing gas jetted from the Laval nozzle 104 is temporarily accommodated in the gas tank 105 to reduce its pressure.
  • the present embodiment prevents counterreaction and enhances the efficiency of the reaction by reducing the pressure and temperature of the high-pressure, high-temperature hydrogen-containing gas.
  • the hydrogen-containing gas in the gas tank 105 is passed through the bag filter apparatus 106 to remove unreacted reactive particles remaining in the hydrogen-containing gas.
  • the unreacted reactive particles collected by the bag filter apparatus 106 are returned to the feeder 102 b for recycling.
  • the hydrogen-containing gas passed through the bag filter apparatus 106 is separated into hydrogen and carbon monoxide (CO), and thus hydrogen is obtained.
  • the CO separated from the hydrogen-containing gas is used as a fuel in the combustion apparatus or heat process apparatus 108 , and thus recycled effectively.
  • the high-speed switching valve 103 b may be switched, or a film provided between the compression chamber 101 a and the waste heat boiler 103 a may be broken to release the high-pressure steam.
  • the waste plastic powder or coke breeze used as the reactive particles has a particle size of 100 ⁇ m or less from the viewpoint of ensuring the reaction.
  • other materials containing hydrocarbon or carbon may be used as the reactive particles.
  • the conditions of temperature, pressure, and the like are not limited to the above-mentioned values, and any conditions may be applied as long as the reactive particles and steam react in the compression chamber to produce hydrogen.
  • a mixture of steam and reactive particles containing hydrocarbon or carbon is impact-compressed and rapidly heated to cause the reactive particles and the steam to react, by a shock wave generated and propagated by jetting high-pressure gas into a compression chamber containing the steam and the reactive particles, thereby producing hydrogen. Therefore, the heat sufficient for the reaction can be efficiently supplied to the mixture in a short time.
  • the method of the present invention does not require preheating the reactor, and accordingly energy is not lost in the steps of starting and suspending the operation of the apparatus. Temperature is increased in only an area where it is required only when it is require, without maintaining high temperature over a long period continuously from the startup of the operation to the suspension.
  • the apparatus of the present embodiments can efficiently supply to a mixture an amount of heat sufficient for the reaction of the mixture, and accordingly it is not necessary to preheat the reactor.
  • energy loss in the steps of starting and suspending the operation of the apparatus is reduced, and consequently the running cost of the apparatus is reduced.
  • temperature is increased in only an area where it is required only when it is require, without maintaining high temperature over a long period continuously from the startup of the operation to the suspension. Accordingly, many fire-resistant materials are not required and thus the cost of the apparatus is reduced.
  • a cylindrical cylinder 202 having an axis 201 is sealed.
  • a piston 203 is provided in such a manner as to freely slide in the direction of the axis, in the cylinder 202 , thus dividing the space in the cylinder 202 into a pressure space P and a backpressure space B.
  • a converging tube 204 is provided in the pressure space P in the cylinder 201 .
  • the converging tube 204 extends to the outside of the cylinder 202 through one 202 A of the end walls of the cylinder 202 .
  • the converging tube 204 has an inlet opening 204 A with a larger diameter, and an external portion 204 B whose diameter decreases toward the outlet opening outside the cylinder 202 .
  • the diameter gradually decreases from the inlet opening 204 A to the external portion 204 B.
  • the inlet opening 204 A is tapered.
  • the piston 203 in the present invention, is formed in a light weight by pressing a metal plate, and is accordingly so light as to be suitable for quick movement with respect to the cylinder 202 .
  • the piston 203 has a skirt 203 A in contact with the internal wall of the cylinder 2 , capable of sliding on the wall, and a tapered portion 203 B in the position where the pressure space P and the backpressure space B are separated.
  • the tapered portion 203 B is tapered so as to come into close contact with the tapered portion of the inlet opening 204 A of the converging tube 204 .
  • a coiled spring 205 is provided between the piston 203 and the other end wall 202 B of the cylinder 202 and places a backpressure on the piston 203 to press it on the inlet opening 204 A of the converging tube 204 .
  • the cylinder 202 is joined to a high-pressure steam feeding tube 206 communicating with the pressure space P, a backpressure stream feeding tube 207 communicating with the backpressure space B, and an exhaust tube 208 .
  • Such a shock wave generator of the present embodiment is used as shown in FIG. 10 .
  • the high-pressure steam feeding tube 206 , backpressure steam feeding tube 207 , and exhaust tube 208 joined to the cylinder 202 have valves 206 A, 207 A, and 208 A, respectively.
  • the valve 206 A is normally open and valves 207 A and 208 A are opened at a given time according to a sequence.
  • part of the high-pressure steam fed from the high-pressure steam feeding tube 206 is used as backpressure steam, and the backpressure steam feeding tube 207 is therefore diverged from the high-pressure steam feeding tube 206 .
  • the converging tube 204 of the shock wave generator is connected to a reactor 210 at its outlet side.
  • the form of the reactor 210 is not particularly limited, as long as it has a compression chamber suitable for instantaneously compressing the raw material or reactive particles together with high-pressure steam by a shock wave of the high-pressure steam from a shock wave generator.
  • Such a compression chamber is joined to a reactive particle feeding tube 211 for feeding reactive particles into the compression chamber, a produced gas outlet tube 212 , and an exhaust tube 213 , and has a valve (not shown in the figures) opening or closing at a predetermined time.
  • high-pressure steam is fed into the pressure space P of the cylinder 202 from the high-pressure steam feeding tube 206 through the valve 206 A in open state.
  • the valve 206 A is normally open.
  • the high-pressure steam is also fed to the backpressure feeding tube 207 A through the valve 207 A in open state.
  • the valve 208 A is instantaneously opened to reduce the pressure of the backpressure space B (see FIG. 11 ( 2 )). Consequently, the pressure of the pressure space P becomes higher than that of the backpressure space B and the urge of the spring, so that the piston 203 backs off against the backpressure to provide a space between it and the inlet opening 204 A of the converging tube 204 .
  • the high-pressure steam flows into the converging tube 204 from this space (see FIG. 12B ).
  • This instantaneous flow of the high-pressure steam causes a shock wave to occur in the converging tube 204 .
  • the shock wave is propagated to the outlet opening of the converging tube 204 to instantaneously compress the steam entering the compression chamber 210 together with the waste plastic powder and thus to heat them, thereby causing a reaction to produce hydrogen gas.
  • the pressure space P is connected to the valve 207 A with a duct 209 , designated by a dashed line in FIG. 10 , when the high-pressure steam is fed into the backpressure space B, the high-pressure steam to remain in the pressure space flows to the backpressure space B due to the open motion of the valve 207 A. Thus, the pressure space P is always filled with fresh high-pressure steam to maintain high temperature.
  • the reactive particle feeding tube 211 , produced gas outlet tube 212 , and exhaust tube 213 may each have a switching valve, and these valves and valves 207 A and 208 A may be sequentially opened or closed for a period and in order shown in FIG. 11 by a cam mechanism.
  • the operation of the valves may be controlled by a control circuit for controlling the valves so as to sequentially open and close for the period and in order above.
  • the present embodiment achieves the generation of a shock wave in an extremely simple structure in which no member but the piston moves relatively with respect to other members.
  • the apparatus for producing hydrogen using a shock wave can be downsized and simplified, and the price of the apparatus can decrease.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
US10/501,794 2002-04-19 2003-03-28 Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, nd method for generating electric power Abandoned US20050072152A1 (en)

Applications Claiming Priority (9)

Application Number Priority Date Filing Date Title
JP2002118427A JP2003313002A (ja) 2002-04-19 2002-04-19 水素製造方法及び水素製造装置
JP2002-118427 2002-04-19
JP2002-150658 2002-05-24
JP2002150658 2002-05-24
JP2002212330A JP4051668B2 (ja) 2002-05-24 2002-07-22 水素製造装置
JP2002-212330 2002-07-22
JP2002-376249 2002-12-26
JP2002376249A JP2004202412A (ja) 2002-12-26 2002-12-26 衝撃波による化学反応方法およびそれを用いた水素製造方法、並びに化学反応装置およびその装置を備えた水素製造装置、および水素供給施設
PCT/JP2003/003940 WO2003089369A1 (en) 2002-04-19 2003-03-28 Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, and method for generating electric power

Publications (1)

Publication Number Publication Date
US20050072152A1 true US20050072152A1 (en) 2005-04-07

Family

ID=29255488

Family Applications (1)

Application Number Title Priority Date Filing Date
US10/501,794 Abandoned US20050072152A1 (en) 2002-04-19 2003-03-28 Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, nd method for generating electric power

Country Status (4)

Country Link
US (1) US20050072152A1 (ja)
EP (1) EP1498387A1 (ja)
CN (1) CN1642850A (ja)
WO (1) WO2003089369A1 (ja)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007134226A1 (en) * 2006-05-12 2007-11-22 Energy Recovery, Inc. Hybrid ro/pro system
US20100083662A1 (en) * 2008-10-06 2010-04-08 Kalex Llc Method and apparatus for the utilization of waste heat from gaseous heat sources carrying substantial quantities of dust
US20110120137A1 (en) * 2009-11-20 2011-05-26 Ennis Bernard P Carbon capture with power generation
US20140243569A1 (en) * 2013-02-22 2014-08-28 Coolbrook Oy Process and rotary machine type reactor
US20140328749A1 (en) * 2005-10-31 2014-11-06 Bestrong International Limited Use of a process for hydrogen production
US10364398B2 (en) * 2016-08-30 2019-07-30 Thermochem Recovery International, Inc. Method of producing product gas from multiple carbonaceous feedstock streams mixed with a reduced-pressure mixing gas
US11220428B2 (en) 2017-01-31 2022-01-11 New Wave Hydrogen, Inc. Hydrocarbon wave reformer and methods of use
US11649762B2 (en) 2020-05-06 2023-05-16 New Wave Hydrogen, Inc. Gas turbine power generation systems using hydrogen-containing fuel produced by a wave reformer and methods of operating such systems
US11701632B2 (en) 2018-12-10 2023-07-18 Ekona Power Inc. Method and reactor for producing one or more products
US11773777B2 (en) 2020-12-18 2023-10-03 New Wave Hydrogen, Inc. Zero-emission jet engine employing a dual-fuel mix of ammonia and hydrogen using a wave
US11890611B2 (en) 2021-04-27 2024-02-06 New Wave Hydrogen, Inc. Conversion system for wave-rotor reactor system
US12012333B1 (en) 2022-12-19 2024-06-18 Ekona Power Inc. Methods and systems for adjusting inputs to a pyrolysis reactor to improve performance
US12157669B2 (en) 2020-12-15 2024-12-03 Ekona Power Inc. Methods of producing hydrogen and nitrogen using a feedstock gas reactor
US12187969B2 (en) 2020-03-10 2025-01-07 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102023113B (zh) * 2009-09-22 2012-10-31 中国科学院理化技术研究所 一种用于冲击压缩实验的液氦温度低温靶
SE534818C2 (sv) * 2010-05-06 2012-01-10 Cortus Ab Förfarande och anordning för införande av pulverformigt material i en förgasningsreaktor, varvid anordningen innefattar en lavaldysa
CN108411112A (zh) * 2018-03-07 2018-08-17 佛山常百乐机械设计有限公司 一种电子元器件用金属制造设备
CN113955757B (zh) * 2021-11-26 2023-11-03 内蒙古禹源机械有限公司 气化渣制二氧化碳捕捉剂并联产氢气与合金的装置及工艺
JP2023097491A (ja) * 2021-12-28 2023-07-10 賢三 高橋 有機物処理材熱分解処理装置用有機物処理材投入装置

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4813179A (en) * 1986-04-01 1989-03-21 Distrigaz S.A. Process for the cocurrent gasification of coal
US5300216A (en) * 1991-02-15 1994-04-05 Board Of Regents Of The University Of Washington Method for initiating pyrolysis using a shock wave

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS415724B1 (ja) * 1963-11-26 1966-03-29
FR2270201B1 (ja) * 1974-03-08 1976-10-08 Siderurgie Fse Inst Rech
JPH05280373A (ja) * 1992-03-31 1993-10-26 Toshiba Corp 石炭ガス複合発電装置

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4813179A (en) * 1986-04-01 1989-03-21 Distrigaz S.A. Process for the cocurrent gasification of coal
US5300216A (en) * 1991-02-15 1994-04-05 Board Of Regents Of The University Of Washington Method for initiating pyrolysis using a shock wave

Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20140328749A1 (en) * 2005-10-31 2014-11-06 Bestrong International Limited Use of a process for hydrogen production
US9561957B2 (en) * 2005-10-31 2017-02-07 Bestrong International Limited Use of a process for hydrogen production
WO2007134226A1 (en) * 2006-05-12 2007-11-22 Energy Recovery, Inc. Hybrid ro/pro system
US20090071902A1 (en) * 2006-05-12 2009-03-19 Energy Recovery, Inc. Hybrid ro/pro system
US7871522B2 (en) 2006-05-12 2011-01-18 Energy Recovery, Inc. Hybrid RO/PRO system
US20100083662A1 (en) * 2008-10-06 2010-04-08 Kalex Llc Method and apparatus for the utilization of waste heat from gaseous heat sources carrying substantial quantities of dust
US8087248B2 (en) * 2008-10-06 2012-01-03 Kalex, Llc Method and apparatus for the utilization of waste heat from gaseous heat sources carrying substantial quantities of dust
US20110120137A1 (en) * 2009-11-20 2011-05-26 Ennis Bernard P Carbon capture with power generation
WO2011063326A1 (en) * 2009-11-20 2011-05-26 Egt Enterprises, Inc. Carbon capture with power generation
US8850826B2 (en) 2009-11-20 2014-10-07 Egt Enterprises, Inc. Carbon capture with power generation
US20140243569A1 (en) * 2013-02-22 2014-08-28 Coolbrook Oy Process and rotary machine type reactor
US9234140B2 (en) * 2013-02-22 2016-01-12 Coolbrook Oy Process and rotary machine type reactor
US10364398B2 (en) * 2016-08-30 2019-07-30 Thermochem Recovery International, Inc. Method of producing product gas from multiple carbonaceous feedstock streams mixed with a reduced-pressure mixing gas
US11370982B2 (en) 2016-08-30 2022-06-28 Thermochem Recovery International, Inc. Method of producing liquid fuel from carbonaceous feedstock through gasification and recycling of downstream products
US11634650B2 (en) 2016-08-30 2023-04-25 Thermochem Recovery International, Inc. Method of producing liquid fuel from carbonaceous feedstock through gasification and recycling of downstream products
US11220428B2 (en) 2017-01-31 2022-01-11 New Wave Hydrogen, Inc. Hydrocarbon wave reformer and methods of use
US11701632B2 (en) 2018-12-10 2023-07-18 Ekona Power Inc. Method and reactor for producing one or more products
US12151225B2 (en) 2018-12-10 2024-11-26 Ekona Power Inc. Method and reactor for producing one or more products
US12187969B2 (en) 2020-03-10 2025-01-07 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas
US12480061B2 (en) 2020-03-10 2025-11-25 Thermochem Recovery International, Inc. System and method for liquid fuel production from carbonaceous materials using recycled conditioned syngas
US11649762B2 (en) 2020-05-06 2023-05-16 New Wave Hydrogen, Inc. Gas turbine power generation systems using hydrogen-containing fuel produced by a wave reformer and methods of operating such systems
US12157669B2 (en) 2020-12-15 2024-12-03 Ekona Power Inc. Methods of producing hydrogen and nitrogen using a feedstock gas reactor
US11773777B2 (en) 2020-12-18 2023-10-03 New Wave Hydrogen, Inc. Zero-emission jet engine employing a dual-fuel mix of ammonia and hydrogen using a wave
US11890611B2 (en) 2021-04-27 2024-02-06 New Wave Hydrogen, Inc. Conversion system for wave-rotor reactor system
US12012333B1 (en) 2022-12-19 2024-06-18 Ekona Power Inc. Methods and systems for adjusting inputs to a pyrolysis reactor to improve performance

Also Published As

Publication number Publication date
EP1498387A1 (en) 2005-01-19
WO2003089369A1 (en) 2003-10-30
CN1642850A (zh) 2005-07-20

Similar Documents

Publication Publication Date Title
US20050072152A1 (en) Hydrogen production method, hydrogen production apparatus, hydrogen supply facilities, nd method for generating electric power
CN101278034B (zh) 用于将煤转化为特定组分的气体的系统
WO2001042132A1 (en) Hydrogen production from carbonaceous material
CN101233215A (zh) 用于将含碳原料转化为特定成分气体的系统
WO2009013647A2 (en) Method of and a plant for combusting carbonaceous fuel by using a solid oxygen carrier
KR102513906B1 (ko) 가스생성시스템
CA2458589A1 (en) Powder metal hydride hydrogen generator
FR2578237A1 (fr) Procede et dispositif pour manufacturer un gaz contenant principalement co + h2 par reformage thermique d'un hydrocarbure gazeux avec de la vapeur d'eau
RU2004101734A (ru) Магнитогидродинамический способ получения электрической энергии и система для его осуществления
CN107087421A (zh) 用于通过喷洒和/或雾化并且用反应气燃烧电正性金属来制造能量的方法以及用于实施所述方法的设备
RU2294354C2 (ru) Способ плазмотермической переработки органического топлива и установка для его осуществления
EP1227142A2 (en) Method and system for producing hydrogen from solid carbon materials and water
JP2004202418A (ja) 二酸化炭素分解装置及び二酸化炭素分解方法
JP2004231481A (ja) 二酸化炭素分解燃料化装置及び二酸化炭素分解燃料化方法
JP3419292B2 (ja) 廃棄物処理システム
WO2022053537A1 (en) Method for operating a blast furnace installation
JP2004202412A (ja) 衝撃波による化学反応方法およびそれを用いた水素製造方法、並びに化学反応装置およびその装置を備えた水素製造装置、および水素供給施設
RU2802303C1 (ru) Способ эксплуатации доменной печи и вспомогательное оборудование для доменной печи
JP2004292525A (ja) 二酸化炭素分離燃料化の装置及び方法、並びに二酸化炭素分離回収の装置及び方法
JP2016513004A (ja) 二酸化炭素を使用済みガスから分離する方法、及び装置
KR102513905B1 (ko) 가스생성시스템
JP2954585B1 (ja) 水素製造方法及び装置
AU2005237098B2 (en) Method for thermal plasma processsing or organic fuel materials as well as an arrangement for carrying out the method
JP2006008461A (ja) 水素製造方法及び水素製造装置
JP6957198B2 (ja) ガス化炉設備およびこれを備えたガス化複合発電設備

Legal Events

Date Code Title Description
AS Assignment

Owner name: JFE ENGINEERING CORPORATION, JAPAN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:SUZUKI, MINORU;IWASAKI, KATSUHIRO;NAKAYAMA, TAKAHASHI;REEL/FRAME:015217/0357

Effective date: 20040922

STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION