WO2008031950A2 - Procédé de génération d'une source d'énergie à partir d'un flux gazeux humide - Google Patents
Procédé de génération d'une source d'énergie à partir d'un flux gazeux humide Download PDFInfo
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- WO2008031950A2 WO2008031950A2 PCT/FR2007/001486 FR2007001486W WO2008031950A2 WO 2008031950 A2 WO2008031950 A2 WO 2008031950A2 FR 2007001486 W FR2007001486 W FR 2007001486W WO 2008031950 A2 WO2008031950 A2 WO 2008031950A2
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- water vapor
- hydrogen
- gas stream
- process according
- combustion
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- 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
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- 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
- C10J3/06—Continuous processes
- C10J3/10—Continuous processes using external heating
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- 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
- C10J3/80—Other features with arrangements for preheating the blast or the water vapour
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- 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
- C10J2300/0903—Feed preparation
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- 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
- C10J2300/0903—Feed preparation
- C10J2300/0909—Drying
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- 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
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- 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
- C10J2300/0956—Air or oxygen enriched air
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- 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
- C10J2300/0959—Oxygen
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- 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
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- 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
- C10J2300/12—Heating the gasifier
- C10J2300/1253—Heating the gasifier by injecting hot gas
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- 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
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1606—Combustion processes
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- 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
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1643—Conversion of synthesis gas to energy
- C10J2300/1646—Conversion of synthesis gas to energy integrated with a fuel cell
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- 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
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- 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
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas
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- 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
- C10J2300/1861—Heat exchange between at least two process streams
- C10J2300/1892—Heat exchange between at least two process streams with one stream being water/steam
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02E60/30—Hydrogen technology
- Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis
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- 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
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
Definitions
- the present invention relates to a method of generating a renewable energy source from a gas stream and the application of this energy source for the production of high efficiency electricity. It also relates to a system implementing the method according to the invention.
- the field of the invention is the field of generating an energy source.
- the invention is more particularly applicable to the generation of a source of energy from a gaseous flow, comprising water vapor, and having served in any treatment, or produced by any method or system .
- An object of the invention is to provide a method and a system for generating an energy source from a gas stream comprising steam with better performance than current methods and systems.
- Another object of the invention is to propose a method and a system that make it possible to generate a source of energy from a gas stream in a simpler way.
- the invention proposes to remedy the aforementioned problems by a method of generating energy from a gas flow, said initial, comprising water vapor, the process comprising deoxidation of at least a portion of the steam of water by passage of the initial gas flow through a layer of redox material at high temperature, called thermal base, essentially comprising carbon elements at high temperature, the deoxidation to obtain a first gas stream comprising the hydrogen obtained by reaction of water vapor with high temperature carbon elements.
- the process according to the invention makes it possible to generate hydrogen from the water vapor present in the initial gas stream, thanks to carbon elements at high temperature. Hydrogen generated is the source of energy, which represents a very important energy value.
- the process according to the invention makes it possible to recover not only a large part of the thermal energy of the water vapor present in the initial flow, but also a large part of the deoxidation energy of the H 2 O molecule by the generating hydrogen from this water vapor.
- the method according to the invention makes it possible to generate more energy than current methods and systems.
- hydrogen, vector of this energy is exploitable in many known industrial systems.
- the initial gas flow may comprise water vapor originating from an industrial process of the implantation site, the recycling of water vapor after combustion of hydrogen, or thermomechanical means for vaporizing a volume of water. water when starting the system.
- the thermal base essentially comprises carbon elements at high temperature, and makes it possible to provide in a single system, the thermal energy and the carbon elements to achieve the deoxidation of the water vapor and the production of H 2 .
- the carbon elements can be those of the chemical composition known raw materials such as coal, lignin, peat, plant or animal biomass.
- the process according to the invention makes it possible to achieve a higher exploitable energy yield than that of the processes and current systems.
- the thermal base comprising carbon at high temperature makes it possible on the one hand to raise the temperature of the water vapor contained in the initial flow to create the temperature necessary for the deoxidation of this steam. water, and on the other hand to provide the carbon elements that are involved in this deoxidation.
- the temperature at the thermal base is such that the water vapor passing through this thermal base is in reaction with the carbon elements at high temperature so as to produce hydrogen by the following deoxidation reactions:
- the method according to the invention may further comprise a step separating hydrogen from the other elements contained in the gas stream after deoxidation of the water vapor. This separation can be achieved by commercially available devices that can be easily implemented.
- the process according to the invention may comprise a storage of hydrogen, obtained during the separation step.
- the method according to the invention may comprise generating electricity in a fuel cell from at least part of the hydrogen, this generation further producing a reaction gas.
- the reaction gas essentially comprises water vapor which can be recycled and deoxidized through the base to produce hydrogen, which will be used again to generate electricity in the fuel cell, in a continuous cycle.
- the process according to the invention may advantageously also comprise a combustion of at least a portion of the hydrogen in a gas boiler, said combustion producing thermal energy and a combustion gas comprising water vapor at room temperature. high temperature and low pressure.
- the combustion of hydrogen can also be carried out in a gas turbine, a gas engine, or a conventional boiler for steam production.
- the combustion of hydrogen in the steam boiler can be carried out under O 2 .
- the gas flow of combustion substantially comprises only water vapor at very high temperature and low pressure.
- the combustion of hydrogen can be carried out under air.
- thermodynamic fluid essentially comprising water vapor at high temperature and high pressure.
- At least part of the high temperature and high pressure water vapor can also be used in a system dedicated to the production of mechanical and / or electrical energy.
- at least a portion of the water vapor contained in the second gas stream is used to produce electricity in a steam turbine, or a turboalternator, this generation of electricity further comprising a generation of a third gas stream comprising low pressure and low temperature water vapor.
- the temperature / pressure pair that can be obtained in the system and method according to the invention can reach very high levels that allow electricity production to be achieved, at the highest efficiency of the existing and future systems and of increase the efficiency of electricity production compared to the thermal potential originally implemented.
- the method according to the invention may further comprise a compression of at least a portion of the low temperature and low pressure water vapor contained in the third gas stream causing said water vapor to a condensation pressure.
- This compression can be achieved in compressor means disposed at the outlet of a steam turbine.
- the process according to the invention may comprise a recovery of at least a portion of the condensation energy of the water vapor obtained after compression.
- the method may further comprise raising the temperature of at least a portion of the water vapor contained in the third stream.
- the method according to the invention may comprise a recycling of at least a portion of the combustion gas comprising water vapor, by passing at least a portion of this gas through the redox thermal base. , for a new deoxidation of said vapor in this gas, this deoxidation again producing hydrogen.
- the permanent recycling of the gas flows logically restores the entirety of the energy potential that they contain less the losses inherent in the systems and materials used for the invention.
- the entire residual heat capacity of the water vapor can thus be recovered at the thermal base and deduces the energy to be supplied to condition the redox carbon elements and allow the disproportionation or deoxidation. water vapor.
- the hydrogen obtained is again transferred to the energy cogeneration system, and this in a continuous cycle.
- the thermal base In this recycling mode, the thermal base must be able to deoxidize water vapor continuously, the amount of carbon at high temperature must therefore be sufficient. High temperature carbon supply must be continuous.
- At least a portion of the water vapor contained in the flue gas may be mixed with at least a portion of the water vapor obtained in a peripheral system.
- the mixture can then be deoxidized through the thermal base and start a new cycle in the process according to the invention, and this in a continuous cycle.
- At least part of the water vapor of the third stream, compressed at a condensation pressure and then raised in temperature, can be recycled and used to produce electricity in a steam turbine, after a rise in its temperature and his pressure.
- the rise in temperature of the water vapor can be achieved by the thermal energy present at the thermal base or by the thermal energy obtained by combustion of hydrogen in a gas boiler, or both. .
- the method according to the invention may comprise a generation of the thermal base by combustion of plant biomass or coal.
- the combustion of biomass can be carried out under O 2 or under air.
- the biomass whose combustion makes it possible to generate the thermal base may comprise plant biomass whose moisture has been previously reduced, such as air-dried biomass, dried biomass in a processing unit, roasted biomass, etc.
- the initial gas flow may comprise at least a portion of a gaseous flow for treating a biomass feedstock, such as the gaseous dehumidification, drying or roasting flux of a biomass feedstock.
- a gaseous flow for treating a biomass feedstock such as the gaseous dehumidification, drying or roasting flux of a biomass feedstock.
- the water vapor present in the initial gas stream comes from the dried, dehumidified or roasted biomass.
- the initial gas flow may comprise CO 2 or any other neutral gas which has served as a dehydration and treatment heat transfer vector.
- the thermal base comprises high temperature carbon elements, it is preferable that the initial gas flow comprises CO 2 .
- the separation of hydrogen and CO 2 at least a portion of the CO 2 can also pass through at least one heat exchanger to reach a temperature required for a predetermined treatment and be used directly in the treatment in question.
- the treatment in question may be roasting, drying, dehumidification, etc. a load of wood for example.
- the thermal base used in the process according to the invention can be ignited at a temperature which is controlled by injecting oxygen into the core of said base. This oxygen injection can be used to control the temperature at the heart of the base, upstream of the base or downstream of the thermal base.
- a system for generating energy from an initial gas flow comprising water vapor comprising:
- thermal base means for generating a layer of high temperature material, called thermal base, essentially comprising carbon at high temperature
- the generation means comprise a thermal generator designed to generate at least a portion of the thermal base, the generator being also provided for deoxidizing at least a portion of the water vapor that passes through the thermal base.
- the thermal base can be within the thermal generator.
- the thermal generator may comprise a thermal reactor or a solid fuel fireplace or a hybrid device, allowing the combustion of a solid fuel, in particular plant biomass. whose moisture has been reduced by prior treatment. This combustion produces carbon elements at high temperature, at least a portion of which can be used to make the thermal base, and used as a high temperature redox carbon.
- the heat generator may be provided with a system for regulating the temperature of the walls, by circulating a coolant.
- the generator may comprise double walls between which the coolant, for example pressurized water, can circulate.
- the heat transfer liquid can also be projected on the walls of the thermal generator.
- the heat generator may comprise a grate hearth adapted to receive the thermal base and arranged to carry out the transfer of the combustion gases from a biomass feedstock that at least partly provides the thermal base and the initial gas flow.
- the grate hearth may advantageously be provided with a cooling system by circulating a heat transfer fluid in the grids of the fireplace.
- the thermal generator may also include means for injecting oxygen.
- the injection of oxygen can, on the one hand, be used to achieve the combustion of a solid fuel for the generation of the thermal base, and on the other hand, the regulation of the temperature at the thermal base .
- the generator may also comprise means for capturing and separating the hydrogen obtained by deoxidation of the water vapor.
- the thermal generator may in particular comprise a gas flow expansion chamber having passed through a high temperature thermal base.
- This relaxation chamber is implemented in particular to complete the disproportionation of residual water vapor molecules in H 2 in contact with carbon monoxide elements from the incomplete combustion of carbon at high temperature.
- the heat generator may comprise at least one heat exchanger, this heat exchanger being provided for making heat exchanges between the first gaseous flow, consisting of essentially CO 2 and H 2 at high temperature and a heat transfer fluid, which may be that of a cooling circuit of a portion of the thermal generator system.
- This fluid takes charge of the thermal energy of said gaseous assembly to transfer it to an electricity cogeneration system, for example a turboalternator.
- the system according to the invention may further comprise a device for producing water vapor, by valuing the thermal energy from any element of the system.
- the system may further comprise means for storing and / or dispensing O 2 and / or CO 2
- FIG. 1 is a schematic representation of a first embodiment of the method according to the invention using a steam boiler
- Figure 2 is a schematic representation of a second embodiment of the method according to the invention using a steam boiler
- Figure 3 is a schematic representation of a third embodiment of the method according to the invention using a fuel cell
- FIG. 4 is a schematic representation of a fourth embodiment of the method according to the invention using a fuel cell.
- FIG. 1 shows schematically a first embodiment of the method according to the invention.
- the system represented in FIG. 1 comprises a unit 1 for storing a solid fuel comprising carbon, and more particularly combustible carbon.
- the fuel carbon may be coal or plant biomass whose moisture has been reduced by prior treatment, such as dehumidification.
- the unit 1 is a unit for storing a feedstock of combustible raw material with a high carbon content B 1. introduced by a regulating system B into the reactor R where it is burned under O 2 .
- This combustible raw material is intended, on the one hand to form the thermal base and on the other hand to carry and maintain this thermal base at the process temperature. The complete combustion of this raw material under O 2 produces CO 2 .
- the reactor R also receives an initial gas stream F1 comprising high-temperature and low-pressure water vapor from an exchanger E2 and a mixing chamber Cm.
- the water vapor from E2 undergoes the redox reaction as it passes through the thermal base.
- This disproportionation produces the first gas stream FgI at high temperature and low pressure.
- This first gas flow FgI is composed essentially of H 2 and CO 2 . H 2 and CO 2 are then separated in an industrial gas separator system SG.
- the CO 2 obtained by separation is a neutral gas flow Fn, too hot to be operated as it is, it is cooled in an air cooler E3. An Fnr part of the cooled CO 2 is rejected and the rest Fns compressed in Cl compressor means and stored in storage means Sl. Part Fnsl stored CO 2 can be used as a cooling stream of the system according to the invention or for the safety of the system.
- the hydrogen obtained is burned under O 2 in a gas boiler Ch.
- the combustion of hydrogen under O 2 makes it possible on the one hand to generate a GcI combustion gas stream at a very high temperature, essentially comprising steam. water H 2 O low pressure, and secondly to generate a second gas stream Fg2 essentially comprising water vapor obtained by heating a thermodynamic fluid Fth essentially comprising water.
- this second gas flow Fg2 essentially comprises high temperature and very high pressure water vapor.
- the GcI combustion gas which has yielded most of its thermal potential to the second gas stream Fg2, still has a significant thermal load, when it leaves the boiler Ch: about 10 to 20% of the calorific value of the combustion of H 2 under O 2 in the system.
- This combustion gas comprising steam is recycled to the reactor R after passing through an exchanger / mixing chamber E2 and Cm where it can be mixed with a liquid Fl-I of H 2 O which serves as a supplement .
- the liquid H 2 O is evaporated in the exchanger / mixing chamber E2 and Cm, a Pch system coupled to a heating system for the start-up phase vaporizes the filler water.
- the second gas stream Fg2 comprising superheated and very high pressure steam obtained at the outlet of the gas boiler Ch drives a TAV steam turbine which generates electricity by an alternator A coupled to the system.
- the turbine makes it possible to exploit most of the mechanical energy of the steam.
- a third gas stream Fg3 is obtained comprising steam at a very low pressure and at a low temperature. This steam is compressed by a steam compressor C2, at a pressure sufficient for its physical change in the liquid state in the preparer / exchanger VAP.
- the permanent recycling of the water vapor and the combustion of the thermal base can generate excess water vapor, which will then be extracted from the recycling circuit.
- FIG. 2 is a schematic representation of a second embodiment of the method according to the invention.
- the system according to the invention is used for the recycling of a treatment gas flow Ft of a biomass load B1 and for the energy recovery of the gaseous flow used for the treatment of the biomass feedstock.
- the biomass B1 is dehydrated or roasted in the treatment unit 1. After treatment, the gaseous mixture extracted comprises:
- This gaseous assembly then becomes the initial gas stream Fl which will be recycled in the system and method according to the invention.
- Part B3 of the treated biomass B1, for example roasting or drying, is stored.
- Another part B2 of the biomass B1 is introduced by a regulator system B into the reactor R where it is thermally reacted under O 2 to form the thermal base, part of which is intended to carry and maintain this thermal base at the process temperature.
- the complete combustion of the biomass under O 2 produces CO 2 which can be used as heat transfer fluid Ft for the treatment of the biomass of origin B1.
- the initial gas stream F1 comprising heat-transfer CO 2 used in the treatment of the biomass B1 and the water vapor extracted from the original biomass, is recycled to the reactor R after heat exchange in an E2 heat exchanger and a transit in a mixing chamber Cm, explained below.
- the initial gas flow is thus at a high temperature when it is introduced into the reactor R.
- the CO 2 is neutral for the deoxidation reaction of the water vapor, but the steam undergoes the reaction. redox of the thermal base.
- This disproportionation produces a first gas flow FgI essentially comprising H 2 and CO 2 .
- H 2 is separated from the other components of the first gas stream, and in particular CO 2 , in an industrial gas separator system SG, known to those skilled in the art.
- CO 2 can be reused as heat transfer gas Ft which will transmit its thermal capacity to the biomass to be dehydrated or roasted.
- the CO 2 has yielded part of its heat load in the heat exchanger El.
- the GcI combustion gas which has yielded most of its thermal potential to the second gas stream Fg2, still has a significant thermal load: 10 to 20% of the heating value of the combustion of H 2 under O 2 .
- the water vapor contained in the combustion gas is recycled to the reactor R after passing through the mixing chamber Cm where it will be mixed with the initial gas flow F1, that is to say, with the gaseous treatment unit of the biomass of origin: CO 2 + H 2 O resulting from the dehydration of the biomass B1.
- the gaseous mixture thus formed becomes the new initial flow Fl which will be recycled in the reactor R, it is at a high temperature and participates in the useful heat exchange within the thermal base. All the thermal energy contained in this gas mixture is recycled.
- the water vapor is again deoxidized at the passage of the thermal base and in a continuous cycle.
- the second gas stream Fg2 comprising superheated steam at very high pressure, obtained at the outlet of the gas boiler Ch, drives a steam turbine TAV which generates electricity by alternator A coupled to the system.
- the turbine makes it possible to transform most of the "temperature / pressure" pair of the steam into mechanical energy that will drive the alternator A.
- a third gas stream Fg3 is obtained, essentially comprising steam. water at a very low pressure and at a low temperature.
- This water vapor is then compressed by a steam compressor C2, at a pressure sufficient for its physical change in the liquid state in the VAP preparer: the water obtained in this preparer (at the pressure relative to the enthalpy of the residual steam) is superheated in the exchanger El before being reintroduced into the secondary circuit of the gas boiler Ch. A large part of the residual energy at the outlet of the steam turbine is thus recycled. Electricity used for compression generates thermal energy by the "Joule" effect that is exploited by the system, thus neutralizing part of the impact of the compressor's electricity consumption on the operating balance.
- FIG. 3 is a representation of a third embodiment of the method according to the invention involving a fuel cell PAC.
- unit 1 is a unit for storing a charge of combustible raw material B1 with a high carbon content.
- This raw material is a fuel for generating, at the same time, the physical and chemical conditions of the disproportionation of the water vapor contained in the initial gas flow.
- the fuel will preferably be solid, to create the best homogenization conditions for the H 2 O disproportionation reaction.
- the choice of fuel will be based on a combustible raw material that will preferably be renewable, either dehydrated or roasted vegetable biomass, or peat or any other fuel with a high carbon content.
- the charge of high carbon feed material B2 is introduced, by a regulating system B, into the reactor R where it is burned under O 2 .
- the combustible raw material thus forms the thermal base, part of which is intended to carry and maintain said thermal base at the process temperature.
- the complete combustion of this raw material under O 2 produces CO 2 .
- the reactor R also receives the initial gas stream F1 comprising water vapor at high temperature and low pressure.
- the water vapor coming from the exchanger E undergoes the oxido-reducing reaction during the passage through the thermal base.
- This disproportionation produces a first gas flow FgI composed essentially of H 2 and CO 2 of the thermal reaction and disproportionation.
- the first gas flow FgI is at high temperature and low pressure.
- H 2 and CO 2 are separated in a system "gas separator" industrial SG.
- the separator SG can be an integral part of the fuel cell which it is then one of the constituent.
- the CO 2 obtained Fn is cooled in an air cooler E3. A part
- the stored CO 2 can be used for cooling system according to the invention or for the safety of the system.
- the hydrogen obtained is introduced into the fuel cell PAC where it will be chemically reacted by the physical means of the system and an injection of industrial O 2 .
- This reaction makes it possible, on the one hand, to generate electricity with a very high efficiency compared to the energy potential implemented initially and, on the other hand, to generate a gaseous reaction stream Fgr comprising essentially steam water at high temperature and low pressure.
- the gaseous reaction stream Fgr is therefore essentially composed of high temperature and low pressure water vapor which has a high thermal load.
- This gaseous reaction stream Fgr comprising water vapor is recycled to the reactor R after passing through an exchanger / mixing box E2 and Cm where it is mixed with a supply of H 2 O liquid that serves Fl-I.
- the liquid H 2 O is evaporated in the exchanger / mixing chamber E2 and Cm, a Pch system, coupled to a heating system for the start-up phase, vaporizes the supply water.
- the gaseous mixture thus formed at the outlet of the mixing chamber Cm, constitutes at least in part the initial gas flow Fl.
- This gaseous mixture is at high temperature and low pressure and participates in the useful heat exchange within the thermal base. All the thermal energy contained in this gas mixture is recycled.
- the steam is recycled to the reactor R, it is again deoxidized at the passage of the thermal base and this in a continuous cycle.
- the permanent recycling of the water vapor and the combustion of the thermal base can generate excess water vapor, which will then be extracted from the recycling circuit.
- Figure 4 is a representation of a fourth embodiment of the method according to the invention involving a fuel cell PAC.
- the system according to the invention is used for the recycling of a treatment gas flow Ft of a biomass load B1 and the recycling (for the energetic and elemental recovery) of the gaseous flow used for the treatment biomass load.
- the biomass B1 is dehydrated or roasted in the treatment unit 1.
- the gaseous mixture extracted comprises: the treatment gas flow Ft, the heat-transfer CO 2 of the biomass charge B 1, and
- This gaseous assembly then becomes the initial gas stream Fl which will be recycled in the system and method according to the invention.
- Part B3 of the treated biomass B1 for example roasting or drying, is stored.
- Another part of the B2 biomass is introduced, by a regulator system B, into the reactor R where it is thermally reacted under O 2 to form the thermal base.
- Part of this biomass B2 is intended to carry and maintain this thermal base at the process temperature.
- the complete combustion of the biomass under O 2 produces CO 2 which can be used as heat transfer fluid Ft for the treatment of the biomass of origin B1.
- the initial gas stream F1 comprising heat-transfer CO 2 used in the treatment of the biomass B1 and the water vapor extracted from the original biomass, is recycled in the reactor R after a heat exchange in a heat exchanger E1 and a transit in a mixing chamber Cm, explained below.
- the initial gas stream F1 is thus at a high temperature when it is introduced into the reactor R.
- the CO 2 is neutral for the thermal reaction, but the water vapor undergoes the oxido-reducing reaction of the thermal base.
- This disproportionation produces a first gas flow FgI essentially comprising H 2 and CO 2 .
- H 2 is then separated from the other gaseous elements comprising the first stream, and in particular CO 2 , in an industrial gas separator system SG, known to those skilled in the art.
- the CO 2 can be reused as heat transfer gas stream Ft which will transmit its thermal capacity to the biomass to be dehydrated or roasted.
- the CO 2 At the outlet of the separator SG, the CO 2 has yielded part of its heat load in the heat exchanger El, but it may still be too hot to be used in the treatment gas Ft, a cold CO 2 injection Then it will regulate it.
- the hydrogen obtained is introduced into the fuel cell PAC where it will be chemically reacted by the physical means of the system and an injection of industrial O 2 .
- This reaction makes it possible, on the one hand, to generate electricity with a very high efficiency compared to the energy potential implemented at the base and, on the other hand, to generate a gaseous reaction flow Fgr essentially comprising steam of water at high temperature and low pressure. Electricity is directly exploitable by all conventional means.
- the gaseous reaction stream Fgr essentially comprises high temperature and low pressure water vapor which has a high thermal load.
- This gaseous stream comprising water vapor is introduced into a mixing chamber Cm where it is mixed with the gas stream extracted from the unit 1 for treating the biomass, and which has passed through the heat exchanger E1 where it has acquired a significant thermal capacity.
- the gaseous mixture thus formed at the outlet of the mixing chamber Cm constitutes, at least in part, the initial gas flow Fl and is at high temperature and low pressure and participates in the useful heat exchange within the thermal base. All the thermal energy contained in this gas mixture is recycled.
- the steam is recycled and deoxidized again at the passage of the thermal base and this in a continuous cycle.
- An Fn part of the CO 2 obtained is cooled in an air cooler E3.
- a part Fnr of CO 2 cooled is rejected and the rest Fns is compressed by means of compressors C1 and stored in storage means Sl.
- Part Fnsl stored CO 2 can be used for cooling the system according to the invention or for the safety of the system. Excess water is also released to the ecosystem at the outlet of the PAC fuel cell.
- the CO 2 which will be used as heat transfer fluid Ft, is at a very high temperature at the outlet of the separator. It exchanges the greater part of its thermal load, the gas stream extracted from the biomass treatment unit, in the heat exchanger El. This heat transfer flow will then be regulated, at the temperature useful to its operation, by a contribution of CO 2 cold Fnsl.
- the invention is not limited to the examples just described and can be used for energy generation from any gas stream comprising water vapor.
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- Engineering & Computer Science (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
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Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US12/441,230 US20090320369A1 (en) | 2006-09-13 | 2007-09-13 | Method of generating an energy source from a wet gas flow |
JP2009527855A JP2010503746A (ja) | 2006-09-13 | 2007-09-13 | 湿性ガス流からエネルギー源を発生させる方法 |
EP07848226A EP2071928A2 (fr) | 2006-09-13 | 2007-09-13 | Procédé de génération d'une source d'énergie à partir d'un flux gazeux humide |
CA002663583A CA2663583A1 (fr) | 2006-09-13 | 2007-09-13 | Procede de generation d'une source d'energie a partir d'un flux gazeux humide |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0607983A FR2905691B1 (fr) | 2006-09-13 | 2006-09-13 | Procede de generation d'une source d'energie a partir d'un flux gazeux humide. |
FR0607983 | 2006-09-13 |
Publications (2)
Publication Number | Publication Date |
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WO2008031950A2 true WO2008031950A2 (fr) | 2008-03-20 |
WO2008031950A3 WO2008031950A3 (fr) | 2008-07-17 |
Family
ID=37907520
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2007/001486 WO2008031950A2 (fr) | 2006-09-13 | 2007-09-13 | Procédé de génération d'une source d'énergie à partir d'un flux gazeux humide |
Country Status (7)
Country | Link |
---|---|
US (1) | US20090320369A1 (fr) |
EP (1) | EP2071928A2 (fr) |
JP (1) | JP2010503746A (fr) |
CA (1) | CA2663583A1 (fr) |
FR (1) | FR2905691B1 (fr) |
RU (1) | RU2009113605A (fr) |
WO (1) | WO2008031950A2 (fr) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
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FR2929955B1 (fr) * | 2008-04-09 | 2012-02-10 | Saint Gobain | Gazeification de materiaux organiques combustibles |
FR3007829A1 (fr) * | 2013-06-26 | 2015-01-02 | Air Liquide | Procede de chauffe avec generation et combustion de syngaz et installation pour sa mise en œuvre |
FR3043689B1 (fr) * | 2015-11-13 | 2017-12-22 | L'air Liquide Sa Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et installation de production d'energie electrique et d'energie thermique a partir de biomasse lignocellulosique |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2084749A (en) * | 1932-08-06 | 1937-06-22 | Earl L Tornquist | Method of manufacturing water gas |
EP0087954A1 (fr) * | 1982-03-01 | 1983-09-07 | The Energy Equipment Company Limited | Installation pour la production de gaz combustible |
EP0550401A1 (fr) * | 1989-02-14 | 1993-07-07 | Manufacturing And Technology Conversion International, Inc. | Procédés et appareil pour réactions endothermiques |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH11270352A (ja) * | 1998-03-24 | 1999-10-05 | Mitsubishi Heavy Ind Ltd | 吸気冷却型ガスタービン発電設備及び同発電設備を用いた複合発電プラント |
JP3700512B2 (ja) * | 2000-01-25 | 2005-09-28 | 日産自動車株式会社 | 燃料電池システム |
US20050064577A1 (en) * | 2002-05-13 | 2005-03-24 | Isaac Berzin | Hydrogen production with photosynthetic organisms and from biomass derived therefrom |
US7056487B2 (en) * | 2003-06-06 | 2006-06-06 | Siemens Power Generation, Inc. | Gas cleaning system and method |
US20060029893A1 (en) * | 2004-08-09 | 2006-02-09 | Kuai-Teng Hsu | Process and system of power generation |
US7569204B2 (en) * | 2006-02-27 | 2009-08-04 | Zeropoint Clean Tech, Inc. | Apparatus and method for controlling the gas composition produced during the gasification of carbon containing feeds |
-
2006
- 2006-09-13 FR FR0607983A patent/FR2905691B1/fr not_active Expired - Fee Related
-
2007
- 2007-09-13 WO PCT/FR2007/001486 patent/WO2008031950A2/fr active Application Filing
- 2007-09-13 RU RU2009113605/05A patent/RU2009113605A/ru not_active Application Discontinuation
- 2007-09-13 EP EP07848226A patent/EP2071928A2/fr not_active Withdrawn
- 2007-09-13 CA CA002663583A patent/CA2663583A1/fr not_active Abandoned
- 2007-09-13 US US12/441,230 patent/US20090320369A1/en not_active Abandoned
- 2007-09-13 JP JP2009527855A patent/JP2010503746A/ja active Pending
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2084749A (en) * | 1932-08-06 | 1937-06-22 | Earl L Tornquist | Method of manufacturing water gas |
EP0087954A1 (fr) * | 1982-03-01 | 1983-09-07 | The Energy Equipment Company Limited | Installation pour la production de gaz combustible |
EP0550401A1 (fr) * | 1989-02-14 | 1993-07-07 | Manufacturing And Technology Conversion International, Inc. | Procédés et appareil pour réactions endothermiques |
Also Published As
Publication number | Publication date |
---|---|
FR2905691B1 (fr) | 2009-07-03 |
WO2008031950A3 (fr) | 2008-07-17 |
CA2663583A1 (fr) | 2008-03-20 |
JP2010503746A (ja) | 2010-02-04 |
RU2009113605A (ru) | 2010-10-20 |
FR2905691A1 (fr) | 2008-03-14 |
US20090320369A1 (en) | 2009-12-31 |
EP2071928A2 (fr) | 2009-06-24 |
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