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
  • C10J3/02—Fixed-bed gasification of lump fuel
  • C10J3/20—Apparatus; Plants
  • C10J3/32—Devices for distributing fuel evenly over the bed or for stirring up the fuel bed
• • 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
  • C10J3/16—Continuous processes simultaneously reacting oxygen and water with the carbonaceous material
• • 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
  • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
  • C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
  • C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
• • 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
  • C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
  • C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
• • 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
  • C10J2200/00—Details of gasification apparatus
  • C10J2200/15—Details of feeding means
  • C10J2200/158—Screws
• • 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
• • 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
• • 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
  • C10J2300/092—Wood, cellulose
• • 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
• • 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
  • C10J2300/16—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
  • C10J2300/1621—Compression of synthesis gas
• • 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
  • C10J2300/165—Conversion of synthesis gas to energy integrated with a gas turbine or gas motor
• • 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
  • C10J2300/1838—Autothermal gasification by injection of oxygen or 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
  • C10J2300/18—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
• • 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
  • Y02E20/00—Combustion technologies with mitigation potential
  • Y02E20/14—Combined heat and power generation [CHP]
• • 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
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/10—Biofuels, e.g. bio-diesel
• • 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
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
• • 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
• • 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 the general technical field of valorization of biomass, in particular of vegetable and / or animal waste or by-products, in order to produce electricity and heat.
• the present invention relates to a method of producing electrical energy from biomass including autothermal gasification of biomass to produce synthesis gas, treatment of this synthesis gas, and injection of the gas into at least one an internal combustion engine coupled to an electric generator, for producing electrical energy.
• the process according to the present invention also advantageously makes it possible to produce thermal energy.
• the present invention also relates to an installation for producing electrical energy from biomass suitable for implementing such a method.
• the installation according to the present invention also advantageously makes it possible to produce thermal energy.
• renewable energy contributes to sustainable energy development. since they do not emit greenhouse gases.
• the development of renewable non-fossil energy sources is therefore a major environmental issue.
• Bio-mass and bio-fuels have the dual advantage of being high-quality fuels and fuels, and not adding to the greenhouse gas emissions. Indeed, biomass contributes to the fight against global warming, since the CO2 generated by the combustion of bioenergy is offset by the CO2 absorbed by the plants during their growth.
• the present invention satisfies this need.
• the Applicant has thus discovered a new method of producing electrical energy and thermal energy from biomass by gasification of said biomass.
• the process according to the present invention allows the treatment and recovery of all kinds of biofuels, such as vegetable waste, not requiring a prior step of extraction of particular plant compounds or isolation of specific plant parts. .
• all the biomass such as plant biomass can be used in the context of the present invention, and the whole mass of plants, including by-products of plants, such as stems, leaves, shells, herbs. needles, or straw, which are generally rejected, can be energetically enhanced in the process according to the present invention.
• the method of producing electrical energy from biomass according to the present invention is relatively inexpensive, since the starting compounds are biomass such as waste or by-products of industries. Furthermore, the method according to the present invention makes it possible to contribute to the reduction of fossil fuel imports contributing to a significant saving in Tonnes of Petroleum Equivalent (PET). Finally, the method of producing electrical energy according to the present invention, comprising the gasification of the biomass to obtain a synthesis gas, the washing of the gas, and then the injection of the synthesis gas into at least one gas engine. coupled with an electric generator, is an environmentally friendly process, since it contributes to the reduction of greenhouse gas emissions. No atmospheric pollutant is released during the gasification stage.
• the subject of the present invention is therefore a method for producing electrical energy from biomass comprising the following successive steps: a) autothermal gasification of the biomass in air in a reactor, under low vacuum, advantageously at a temperature greater than 800 ° C., to obtain a synthesis gas, b) cooling of the synthesis gas at a temperature of not less than 300 ° C., (c) washing of the synthesis gas in order to eliminate substantially the tars and / or the ammonia, d ) injection of the washed gas into at least one gas engine coupled to an electric generator, for producing electrical energy.
• the bio mass is at least one vegetable waste, such as agricultural or forestry waste, or a by-product or co-product of agro-food industries of the distilleries type.
• the biomass may contain grape marcs and / or wood chips, or bark.
• the method further comprises a step of drying the biomass in order to obtain a mass moisture content of less than 25% on total mass, prior to the gasification step a) biomass.
• the method further comprises a step of grinding and / or calibration of the biomass, prior to the gasification step a) of the biomass.
• water vapor is also injected into the gasification reactor a) of the biomass in order to increase the gasification yield.
• the gasification a) of the biomass is carried out in a non-fluidized moving bed gasifier, with stirring in order to avoid stagnation of the ash in the gasification reactor.
• the cooling b) of the synthesis gas is carried out by passage of said gas in a thermal recuperator containing a thermal fluid, such as thermal oil.
• a thermal fluid such as thermal oil.
• said heat recovery unit is coupled to a vaporizer for producing steam, said water vapor being then advantageously used to drive a steam turbine to produce electrical energy.
• the method according to the invention makes it possible to produce thermal energy in the form of hot water or of water vapor during the cooling step b) of the synthesis gas using thermal recuperator.
• thermal energy in the form of hot water or of water vapor during the cooling step b) of the synthesis gas using thermal recuperator.
• water vapor is not recovered in a steam turbine.
• At least a portion of the ashes and dusts entrained in the synthesis gas are separated from the gas by passage in at least one cyclone, downstream of the gasification a) of the biomass, prior to the washing step c) synthesis gas.
• the process also comprises at least one step of compressing the synthesis gas downstream of the gasification a) of the biomass, advantageously before and / or after the washing step c) of the synthesis gas .
• the washing c) of the synthesis gas is carried out in at least one organic liquid washer by counter-current organic liquid spraying, in order to purify the gas by trapping the heavy tar. and / or light in the organic liquid.
• the organic liquid is typically selected depending on the tars produced according to the type of biomass.
• this specific organic liquid can be called synthetic oil.
• the purification of heavy tar is carried out in a first organic liquid scrubber stage by trapping heavy tar in this organic liquid, then the heavy tar is separated from the organic liquid, for example by centrifugation, before being reinjected as fuels in the gasification reactor.
• the purification of light tars is carried out in a second organic liquid scrubber stage by trapping light tars in this organic liquid, this organic liquid being identical to or different from the organic liquid used for purifying the heavy tars, then the light tars are separated from the organic liquid in an air / liquid organic air separator by hot air injection against the current, and the hot air charged with light tars is then reinjected into the oxidation zone of the gasification reactor.
• the washing c) of the synthesis gas is carried out in at least one water washer by countercurrent water spraying, in order to purify the gas by trapping ammonia in water, advantageously after washing the gas of heavy and / or light tar.
• the ammonia is separated from the water in an air / water separator by injection of hot air against the current, and the hot air charged with ammonia is then reinjected into the reactor. gasification.
• said gas has a lower heating value between 4 and 7.
• MJ / Nm 3 is at a pressure between 60 and 100 mbar, and at a temperature between 40 and 80 0 C, preferably between 40 and 60 0 C.
• the energy of the exhaust gases from the combustion in said gas engine is recovered in order to supply a fuel. boiler for producing water vapor, said water vapor being then advantageously used to drive a turbine coupled to a generator to produce electrical energy.
• the energy of the gases exhaust from combustion in said gas engine can also be recovered as thermal energy.
• the subject of the present invention is also an installation for the production of electrical energy from biomass comprising, in series, an autothermal gasification reactor (1) for the biomass containing means for continuously injecting air throughout the entire period of time. duration of the gasification reaction, generating a synthesis gas, a cooling device (2) of the synthesis gas, - a washing device (3) of the synthesis gas in order to eliminate substantially the tars and / or the ammonia , and at least one gas engine (4) coupled to an electric generator, for producing electrical energy.
• This installation is suitable for implementing the method according to the present invention.
• the installation also contains a means (5) for drying the biomass, such as a low-temperature dryer, upstream of the biomass gasification reactor (1).
• the plant according to the present invention further contains a grinding means and / or a means for calibrating the biomass, upstream of the biomass gasification reactor (1).
• the biomass gasification reactor (1) is a non-fluidized moving bed gasifier containing counter-current air injection means.
• the reactor (1) for gasification of biomass further contains means for injecting water vapor.
• the reactor (1) for gasification of the biomass contains, in its lower part, at least one stirring means, such as a rotary stirring arm provided with deflectors.
• the cooling device (2) of the synthesis gas is typically a thermal recuperator containing a thermal fluid, such as thermal oil, said thermal recuperator being advantageously coupled to a vaporizer for producing water vapor, said vaporizer itself being advantageously coupled to a steam turbine (6) in order to produce electrical energy.
• the plant according to the present invention also contains at least one cyclone (7), downstream of the reactor (1) for gasification of the biomass.
• the installation according to the present invention also contains at least one compression device (8) for the synthesis gas downstream of the reactor (1) for gasification of the biomass, advantageously upstream and / or downstream. of the washing device (3) of the synthesis gas.
• the washing device (3) of the synthesis gas contains at least one tar washing means (3a), such as an organic liquid scrubber, in order to extract the tars from the synthesis gas.
• the organic liquid is synthetic oil.
• the synthesis gas washing device (3) contains two series-associated organic liquid washers (3a), in particular a first organic liquid washer for trapping heavy tar in the organic liquid, followed by a second scrubber with organic liquid to trap light tar in the organic liquid.
• the synthesis gas washing device furthermore contains, at the bypass outlet of the first organic liquid washer (3a), a means for separating heavy tar from the organic liquid, as well as means for recirculating the heavy tars recovered at the outlet of the separation means to the gasification reactor (1).
• the washing device of the synthesis gas further contains, at the bypass outlet of the second organic liquid washer (3a), an air / organic liquid separator containing air injection means. counter-current hot for separating light tars from the organic liquid, as well as means for recirculating the hot air charged with light tars recovered at the outlet of the air / liquid organic separator to the reactor (1) for gasification.
• the washing device (3) of the synthesis gas contains at least one means for eliminating ammonia (3b), such as a water scrubber, for purifying the gas by trapping ammonia in the water.
• the synthesis gas washing device furthermore advantageously contains, at the bypass outlet of the water washer (3b), an air / water separator containing means for injecting hot air against the current. for separating the ammonia from the water, as well as means for recirculating the hot air charged with ammonia recovered at the outlet of the air / water separator to the reactor (1) for gasification.
• the installation furthermore contains, at the outlet of the gas engine (4), means for recovering the exhaust gases from the combustion in said gas engine in order to supply a boiler to produce water vapor, and the installation further contains, at the outlet of the boiler, a turbine (6) coupled to a generator to produce electrical energy.
• FIG. 1 is a schematic view of an electrical power generation plant from biomass comprising associated with series: - means for drying (5) the biomass, an autothermal gasification reactor (1) partially dried biomass, containing means for continuous air injection to generate a synthesis gas, a cooling device (2) synthesis gas, said device (2) being coupled in parallel with a steam turbine (6), - a cyclone (7) to separate from synthesis gas a portion of the ashes and dusts entrained in the gas, a first booster (8) for compressing the synthesis gas prior to washing the gas, a washing device (3) of the synthesis gas to extract gas tars and ammonia, said device (3) contena in series a tar washing means (3a) and an ammonia washing means (3b), a second booster (8) for compressing the synthesis gas after washing the gas, and a gas engine (4) coupled to an electric generator, for producing electric energy, said gas engine (4)
• the installation also comprises a flare (9), at the bypass outlet of the two boosters (8), in order to periodically burn off the surplus synthesis gas if necessary, and thus to regulate the flow of gas before it enters the system. gas engine.
• the heat produced by the hot water circuit and the residual energy of the engine fumes are used for the drying of the biomass.
• the method according to the present invention makes it possible to produce electrical energy by gasification of the biomass.
• biomass in the sense of the present invention any organic matter biodegradable from a natural process, capable of energy recovery.
• biomass can be any biodegradable carbonaceous waste.
• Biomass can be of plant or animal origin, or can be produced by human activity.
• Biomass can be: - wood, for example in the form of logs, pellets and platelets; wood by-products which cover all the waste produced by logging (branching, bark, sawdust ...), sawmills (sawdust, chips, etc.), by the wood-processing industries ( joineries, furniture manufacturers, flooring) and panel manufacturers, as well as packaging such as pallets; by-products of the industry, such as sludge from pulp (black liquor) and waste from agri-food industries (grape and coffee grounds, pulp and grape seeds, etc.); products from traditional agriculture (cereals, oilseeds), residues such as straw, rice husks, bagasse (ligneous residues from sugar cane) and new energy plantations such as short rotation coppices (willow, miscanthus, etc.); organic waste such as urban waste including sewage sludge, household waste, and waste from agriculture such as agricultural effluents; or waste from livestock such as manure, litter, dung, slurry, etc.
• the biomass in the context of the invention is a waste or a plant by-product, which can decompose, including agricultural waste or forest, such as leaves, stems, pods, pods or shells, barks, needles, straw, grasses, and mixtures thereof.
• agricultural waste or forest such as leaves, stems, pods, pods or shells, barks, needles, straw, grasses, and mixtures thereof.
• grape marcs, wood chips, or mixtures thereof can be used.
• roots such as endive roots, flax waste, fruit stones, bagasse, etc.
• slurry of pigs, animal meal, or composts such as sewage sludge mixed with green waste.
• the biomass is dried prior to the gasification step a) of the biomass.
• all of the biomass products naturally have a moisture content of approximately 35 to 55% on total material, for example of the order of 40% on total material.
• the biomass is dried in order to obtain a mass moisture content of less than 25% on total material, advantageously less than 20% on total material, before being introduced into the reactor (1) for gasification. Drying is advantageously carried out by injection of hot air.
• the drying of the biomass is carried out at low temperature, ie at a temperature of less than 100 ° C., in particular of approximately 80 ° to 95 ° C., in a low temperature dryer.
• the dryer contains a micro-perforated belt that transports the product from the feed silo to the point of discharge of the product. Hot air is advantageously injected onto the micro-perforated carpet, thereby plating the product to be dried on the carpet, and therefore avoiding the flights at the end of drying.
• the hot air is typically generated by the passage of ambient air from an air / water exchanger preferably located in the upper part of the dryer.
• a fan usually circulates this air inside the dryer.
• hot water and / or fumes recovered from gas engines (4) are used in order to provide the energy necessary to heat the air which will be used for drying the biomass.
• the air saturated with water can then be rejected by an exhaust duct (chimney) at the top of the dryer.
• a regulation system can be used to follow and adapt the operating speed of the dryer to guarantee a constant humidity rate at the outlet, ie of the order of 20% or 25% moisture content. total.
• the outlet air is not odorous: in fact, the temperature being low and the air flow important, no combustion of the biomass is carried out during the drying, and the discharges are very diluted (dilution of VOC exiting the dryer).
• the dried products then generally transit to a buffer silo pending conversion to synthesis gas in the gasifier.
• the transport of the dried biomass to the buffer storage silo can be carried out by a mechanical conveyor.
• the biomass Before drying, the biomass can be ground if necessary, especially when the biomass contains platelets or bark of plants. Generally, grinding is carried out in order to calibrate the biomass.
• the crushed particles typically have a particle size of less than 1 cm 3 .
• the biomass After drying, the biomass is advantageously weighed by a metering unit, in order to constantly supply the gasification reactor (1).
• the product is conveyed continuously to the gasification reactor (1), for example by means of a variable speed feed screw and a bucket elevator.
• a last feed screw advantageously brings the fuel to the reactor core (1).
• the biomass which is a solid fuel is converted into syngas.
• the gasification is typically carried out in a poor atmosphere O 2 .
• the admission of the products and the evacuation of ashes are generally carried out continuously.
• the synthesis gas produced is generally sucked up and evacuated continuously.
• the injection of air into the reactor is advantageously carried out by air injection continuously throughout the duration of the gasification reaction for generating the synthesis gas.
• the gasification a) of the biomass is carried out at a gas outlet temperature of greater than 700 ° C., still more advantageously at a temperature above 800 ° C., still more advantageously at a temperature above 850 ° C. C, still more advantageously at a temperature above 900 ° C., in particular at a temperature above 950 ° C.
• the temperature of the biomass bed can reach and exceed 1100 ° C.
• the gasification reactor (1) that can also be called gasifier, advantageously operates at a pressure close to atmospheric pressure.
• the gas generator operates under a low vacuum, which limits any risk of leakage to the outside.
• the pressure in the reactor (1) is typically of the order of -10 to -5 mbar. This depression is preferably maintained by a booster fan (8) placed after the gasification reactor (1). This fan is typically driven by a variable frequency motor.
• the temperature of the reactor (1) can be done through a gas burner, which is preferably installed at the bottom of the reactor for the duration of the heating phase of the hearth.
• the burner is equipped with its ignition and flame detection system and generally runs on propane gas. It makes it possible to heat the reactor to a necessary and sufficient temperature (self-ignition temperature of the order of 500 ° C.) so that the gasification can begin alone.
• the gasification a) of the biomass is advantageously an autothermal gasification, in air, unlike allothermal gasification requiring external heat input.
• the gasification a) of the biomass is a combustion of the biomass, taking place by controlled admission of air into the reactor (1).
• the injected air flow rate is typically of the order of 1.5 to 2.5 relative to the biomass flow rate at 20% by total mass (MT).
• the injected air flow rate is of the order of twice the mass flow rate at 20% by total mass (MT).
• the gasification is advantageously controlled by the gasification temperature in the reactor (1).
• This gasification temperature is advantageously adjusted by regulating the amount of air introduced preferably by a supply air fan located in the lower part of the reactor (1).
• the distribution of air in the reactor is advantageously carried out through a perforated support plate.
• several air intakes can be provided in order to evenly distribute the air injection.
• Manually adjustable valves can be installed at each air injection point.
• the gasifier contains countercurrent air injection means constituted by a multitude of nozzles distributed homogeneously under the surface of the bed.
• the gasification temperature makes it possible to reach a stage of "cracking" the carbon chains to generate a gas mainly containing nitrogen, CO 2 , carbon monoxide, hydrogen, methane, etc.
• This poor gas called synthetic gas, is of low energy value, but is compatible with the use of an internal combustion engine.
• the synthesis gas is advantageously free of dioxins and furans.
• 1050 ° C., and in particular of the order of 1100 ° C. is greater than 10 seconds, typically of the order of 10 to 15 seconds, and the residence time of the synthesis gas is generally greater than 3 seconds, typically of the order of 3.5 seconds.
• the gasification reactor (1) is for example a vertical reactor, of the order of 15 to 20 m.
• the gasification reactor (1) is advantageously a non-fluidized moving bed gasifier of constant height for a given fuel. It advantageously contains means for injecting air against the current. Biomass is typically introduced in the middle and central part of the reactor (1) gasification, while the injection of air is performed in the lower part of the reactor (1).
• the gasification reactor (1) is advantageously equipped with an agitator, preferably in its lower part. It allows mixing the product, maintain a bed of fuels of constant height (approximately twenty centimeters), and conveys the ashes to the low point or points of ash recovery at the bottom of the reactor (1).
• the rotational speed of the stirrer and the rate of ash removal can affect the gasifier's performance.
• This agitator is typically powered by a variable speed motor.
• the operating mode can be automatic or manual.
• the gasification reactor (1) contains, in its lower part, a rotary agitator arm provided with deflectors.
• the baffles are advantageously arranged along the arm. A slow and steady movement of the ash bed from the center to the periphery of the gasifier thus avoids the stagnation of the ashes, their agglomeration and therefore their vitrification.
• This embodiment is particularly suitable when the biomass contains grape marc.
• the marc of grapes contains a significant part of potassium (about 2%), unlike other fuels such as wood that contain much less.
• This portion of potassium adversely affects the ashes which have a strong tendency to vitrify (caking with formation of glass).
• This vitrification disrupts airflow by blocking air inlets and therefore degrades the operation of the gasifier.
• the use of a rotary agitator arm provided with deflectors in the gasifier thus makes it possible to avoid vitrification of the ashes.
• steam is injected into the reactor (1) during the step of gasification a) of the biomass.
• the Applicant has discovered that the injection of water vapor into the gasification reactor (1), in particular into the intake air, tends to "crack" the last% of carbon contained in the ashes, and thus significantly improve the gasification efficiency.
• the yield of the gasifier is typically of the order of 60 to 75%, for example around
• the yield of the gasogen is typically of the order of 70 to 80%, in particular of the order of 75 to 80%, for example around 77%.
• the gasification reactor (1) essentially generates the synthesis gas, which is preferably discharged by a sheath placed in the upper part of the reactor and connected to the gas washing device.
• the reactor advantageously does not have a chimney in the exhaust rejection sense.
• the temperature of the gas leaving the reactor is typically about 700 to 1000 ° C., for example of the order of 850 ° C.
• the synthesis gas mainly contains carbon monoxide, carbon dioxide, methane, hydrogen and nitrogen.
• the synthesis gas is devoid of dioxins and furans.
• the synthesis gas contains (% by volume): 10 to
• the synthesis gas is suitable for combustion in internal combustion engines, and advantageously has a methane number greater than 70.
• the synthesis gas has the following composition (% by volume):
• the gas is also loaded with tars that will be removed during the washing phases.
• the ash collected at the bottom of the gasifier (1) is advantageously cooled and then transported, for example in a closed conveyor, to a silo for storing bottom ash. These ashes can then be used for agricultural application or for agricultural amendments.
• the gas can be advantageously subjected to primary purification by controlled air injection into the gasogen, typically at the top of the gasifier.
• the air injection is performed in the upper part of the gasifier, typically above the feed screw of the biomass.
• the injected air can be heated or at room temperature. Most of the air is injected into the reactor, but it can also be enriched in O 2 and / or steam.
• the primary purification of the synthesis gas makes it possible to crack the tars generated in the bottom of the reactor to unload the downstream gas scrubber, to react the carbon of the ash entrained by the generation of the gas to transform it into a combustible gas (improvement of the yield), and reduce the amount of ash collected by the cyclone (7).
• the synthesis gas obtained is subjected to a cooling step b), typically using a heat exchanger (2).
• the gas advantageously passes through a thermal recuperator (2), like countercurrent flue gas tubes.
• This recuperator (2) makes it possible to cool the synthesis gas to a temperature greater than 300 ° C., advantageously greater than about 320 ° C., in particular greater than about 350 ° C., for example using a fluid thermal such than thermal oil.
• the temperature of the synthesis gas after cooling b) must not be too low, in order to prevent the tars from settling and clogging the circulation lines.
• the cooling device (2) of the synthesis gas is specific to the product gas. It is typically a vertical device, in which the gas passes from top to bottom, and the thermal fluid from bottom to top.
• Temperature sensors make it possible to control the temperature of the thermal oil in the recuperator and at the outlet of this recuperator.
• the cooling device (2) of the synthesis gas is coupled to a vaporizer to produce steam driving a steam turbine (6), to produce electrical energy.
• the cooling device (2) of the synthesis gas can also make it possible to produce thermal energy in the form of hot water or steam.
• at least part of the ashes and dusts entrained in the synthesis gas are separated from the gas by passage through at least one cyclone (7), downstream of the gasification a) of the biomass, beforehand in the washing step c) synthesis gas.
• the synthesis gas passes through a cyclone (7) to remove the fine dust contained in the gas.
• the synthesis gas is then advantageously compressed, prior to the washing step c).
• the gas is sucked by a first booster (8), making it possible to maintain the gasifier (1) in slight depression (of the order of -5 mbar), and thus to suck the gas through the heat recuperator (2) and the cyclone (7).
• the gas is compressed between approximately 50 and 75 mbar, advantageously between 60 and 70 mbar, above atmospheric pressure, in order to operate at a slight overpressure in the washing system (3) of the gas .
• the gas is then washed to substantially remove tars and / or ammonia.
• the tar content at the entrance to washing is typically 25 g / Nm 3 and is reduced to 100 mg / Nm 3 at the end of the wash.
• the ammonia content at the inlet of the scrubber is typically 4000 to 5000 mg / Nm 3 and is reduced to 40-50 mg / Nm 3 at the outlet.
• the washing c) of the gas advantageously comprises a first tar extraction step in at least one tar washing device (3a).
• the washing of the tars is typically carried out in at least one oil scrubber by spraying synthesis oil (organic liquid) in countercurrent.
• synthesis oil organic liquid
• the synthesis oil will be described as oil below.
• the heavy tar are first removed in a first scrubber stage, typically at a temperature of the order of 300 to 350 ° C.
• the oil scrubber ( scrubber) is typically supplied with oil from a small buffer storage tank.
• the gas enters the lower part and circulates from bottom to top, while the oil is sprayed through nozzles, against the current, in the upper part of the column.
• the synthesis gas is thus purified of most of the heavy tar which is trapped in the oil.
• the oil loaded with heavy tar is then sent to a means for separating heavy tar from the oil, this separating means being connected to the bypass outlet of the oil scrubber.
• the means for separating heavy tar from the oil may for example be a centrifuge.
• the oil is then generally re-injected into the buffer storage tank.
• Recovered tars for their part, are advantageously reinjected as fuels in the reactor (1) for gasification to be burned completely.
• the light tars are advantageously washed.
• the synthesis gas is thus transferred to a second scrubber, placed downstream of the first oil scrubber that was used to purify the heavy tar.
• an organic liquid synthetic oil
• the oil may be the same as or different from the oil used to purify heavy tar.
• the synthesis gas is thus purified of most of the light tars which are trapped in the oil.
• the oil loaded with light tar is then sent to a means for separating the light tars from the oil, this separation means being connected to the bypass outlet of the second oil scrubber.
• the means for separating the light tars from the oil is typically an air / oil separator (air / oil stripper) into which hot air is injected countercurrently.
• the hot air is typically injected into this air / oil separator at a temperature of the order of 160 to 200 ° C., in particular at a temperature of between 180 ° C. and 190 ° C.
• the hot air is preferably injected at the bottom of the air / oil separator, while the oil is injected at the top.
• the tars are then transferred to the air, and the clean oil can then be returned to the second stage of the oil scrubber.
• the column of the air / oil separator is advantageously filled with packing to maximize the exchange surface.
• the hot air charged with light tars can then be reinjected into the gasification reactor (1) as combustion air.
• the purified gas of the tars is then advantageously directed to a washing system (3b) in order to remove a large part of the NH 3 (ammonia).
• the gas Prior to introducing the gas into the ammonia washing device (3b), the gas is advantageously cooled to a temperature of the order of 20 to 30 ° C., for example around 25 ° C. for example in a double-stage condenser. Condensate charged with NH 3 can then be sent to an air / water separator (air / water stripper) for pre-treatment of this deconcentration water.
• air / water separator air / water stripper
• the ammonia washing device (3b) is a washing device with water, such as a water scrubber (water scrubber), by water spraying against a current.
• water scrubber water scrubber
• the principle of water washing involves absorbing the ammonia (NH 3 ) contained in the gas with water.
• the gas advantageously circulates upwards in the water scrubber, while the water is sprayed against the current.
• the column of the water washer is advantageously equipped with a lining (small elements arranged in an ordered structure) which allows better absorption of NH 3 by water: the gas is then obliged to borrow from sinuous paths, and therefore more in contact with water (increase of the exchange surface).
• the water washing system (3b) makes it possible to reduce the concentration of NH 3 in the gas from approximately 4000 - 5000 mg / Nm 3 of gas to 25 mg / Nm 3 of gas.
• the synthesis gas is thus purified of most of the ammonia which is trapped in water.
• the clean gas can then be sent to the power plant, also called cogeneration plant, for the supply of gas engines (4).
• the gas Prior to the injection d) of the gas in the gas engines (4), the gas is compressed using a booster (8) at a pressure greater than atmospheric pressure, typically at a pressure of between 50 and 50.degree. 140 mbar, advantageously between 60 and 100 mbar.
• the water charged with ammonia is then sent to a means for separating ammonia and water, this separation means being connected to the bypass outlet of the water scrubber.
• the means for separating the ammonia from the water is typically an air / water separator (air / water stripper) into which hot air is injected countercurrently.
• the hot air is typically injected into this air / water separator at a temperature of the order of 30 to 70 ° C., in particular at a temperature of between 35 ° C. and 55 ° C.
• the hot air is preferably injected at the bottom of the air / water separator, while the water is injected at the top.
• the ammonia dissolved in the water is captured by the hot air, the hot air causing a fall in the partial pressure of the NH 3 and thus allowing its degassing.
• the column of the air / water separator is advantageously filled with a porous lining, making it possible to increase the exchange surface as much as possible.
• the hot air containing the NH 3 then exits through the top of the column of the air / water separator before being reinjected into the gasification reactor (1) as combustion air.
• the hot air charged with ammonia is first sent to the lower part of the air / oil separator (stripper air / oil) which is then used to separate the light tar from the oil. Then, the hot air charged with ammonia and light tar is reinjected into the gasification reactor (1).
• the clean water recovered at the bottom of the column of the air / water separator is advantageously cooled, then reused in the water scrubber (scrubber water).
• a bypass system Prior to washing c) of the synthesis gas, preferably at the outlet of the first booster (8), a bypass system is installed in particular for the start-up phase of the installation. On this bypass system, a flare (9) can burn episodically excess synthesis gas if necessary. During the rise in temperature and power (0 to 100%) of the gasifier
• the first gases produced are advantageously burned by flaring until the gasifier has reached 70% load, the washing system (3) can function properly from this load.
• This bypass is also used in case of malfunction of the washing system (3) or the second booster (8).
• a second bypass system is installed in particular in the event of a partial or total shutdown of the booster unit. cogeneration (shutdown of engines). Indeed, the inertia of the gasification system is such that the system can not respond instantly. The gas produced in excess is then flared, thereby regulating the flow of gas before entering the gas engine (4).
• a bypass duct is thus preferably connected to the bypass outlet of each of the two boosters (8) which are advantageously upstream and downstream of the washing device (3a, 3b) of the gas (see FIG. 1).
• the flare (9) is a gas burning device used very episodically, a temporary solution necessary in the start-up phase or to compensate for the lack of reactivity of the gasifier (1) during an emergency stop or during sudden changes in the load of the motors (4).
• said gas After the washing c) of the synthesis gas, and prior to its injection d) in the gas engine (4), said gas has a lower heating value (PCI) of between 4 and 10 MJ / Nm 3 , advantageously between 4 and 6 MJ / Nm 3 .
• PCI heating value
• the injection of the washed gas into at least one gas engine (4) coupled to an electric generator makes it possible to produce electrical energy.
• the efficiency of the gas engine (4) is of the order of 32 to 38%, in particular of the order of 33 to 36%.
• the efficiency of steam turbines (6) is of the order of 21 to 27%, for example of the order of 24 to 25%.
• the overall efficiency of the process (electrical and thermal energy) is of the order of 75 to 85%, for example of the order of 80% with a turbine.
• the engine (4) may be a spark ignition internal combustion engine or a pilot fuel injection engine.
• the installation according to the present invention contains several gas engines (4).
• brine flows in a closed circuit in the pipes in order to cool the gas engines (4).
• the exhaust gases resulting from the combustion in said gas engine are recovered in order to supply a boiler for producing water vapor, said water vapor being then advantageously used to drive a turbine (6) coupled to a generator to produce electrical energy.

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