WO2013140418A1 - Réacteur thermochimique à gaz multi-conditions - Google Patents

Réacteur thermochimique à gaz multi-conditions Download PDF

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Publication number
WO2013140418A1
WO2013140418A1 PCT/IN2013/000172 IN2013000172W WO2013140418A1 WO 2013140418 A1 WO2013140418 A1 WO 2013140418A1 IN 2013000172 W IN2013000172 W IN 2013000172W WO 2013140418 A1 WO2013140418 A1 WO 2013140418A1
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WIPO (PCT)
Prior art keywords
gasification
zone
current
gas reactor
counter
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PCT/IN2013/000172
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English (en)
Inventor
A Saravanakumar
K Vinoth Kumar
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Nsp Green Energy Technologies Private Limited
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Publication of WO2013140418A1 publication Critical patent/WO2013140418A1/fr

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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
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • 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
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • 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
    • C10J2200/36—Moving parts inside the gasification reactor not otherwise provided for
    • 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
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • 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 gas reactors, and more particularly to an improved thermochemical biomass gas reactor for efficient conversion of biomass materials into usable heat energy, by incorporating the combined modes and operational advantages of counter-current and co-current gasification.
  • Gasification is an established technology for power generation where the process facilitates to overcome many of the limitations of the conventional combustion systems with highest efficiency which converts solid fuels into a clean gas that can be used in a 100% Gas Engine mode for power generation.
  • the conventional power generation is mostly concentrated and centralized. Realizing the heavy power transmission loss, a policy of Distributed Power Generation system was formulated. In "Distributed Decentralized Power Generation Scheme, many small-scale gasifier based Power Plants are encouraged against the demand. The steam generation from the waste heat recovery and process optimisation apart from power generation from gas with enhanced efficiency abets in plummeting the all-scale processing factory's steam consumption in radical approach.
  • Gas reactors are usually classified as counter-current, co-current, or side-draft (cross-current) reactors.
  • Fig. 1 and 2 shows the counter current sand co-current gasification for the thermochemical gas reactors in accordance to the prior art of the invention.
  • air is blown or drawn up through a grate supporting the feedstock, and the producer gas passes up through the combustion zone and the unburned fuel and out an exit at the top for energy consumption.
  • Co-current gas reactors force the producer gas down through the combustion area by means of air pressure or air suction to an exit for use as energy consumption.
  • Co-current gas reactors were developed in an effort to reduce tar content in gas used to power internal combustion engines.
  • the air enters through peripheral jets directed toward the center of the airtight cylindrical fuel and combustion chamber just above a funnel-shaped or conical bottom to initiate gasification.
  • the feedstock is devolatilized by combustion and heat, it shrinks into pieces of carbon or char which accumulate in a conical bottom and are supported on a grate below the throat.
  • the char forms a red-hot bed which reduces CO 2 to combustible CO and also cracks the tars into stable gases.
  • This gas can be cleaned and cooled for use in an engine to generate power by mitigating emissions compared over conventional route.
  • One of the most common techniques of providing a conversion of biomass material to gas involves the use a dumping of the material into container which has a grate near the bottom.
  • the material is mixed with combustible air which is force-fed and the burning product produces the gas which is pumped away from the source.
  • the purpose of the grate is to provide a surface which allows for a complete burn up of the product and the removal of the ash away from the combustion area so that the heat is not wasted on completely combusted material.
  • the US4452611 discusses about co-current channel gasifier for the efficient conversion of biomass materials to generate heat energy, which includes two generally triangularly shaped air ducts positioned longitudinally across an enclosed housing defining a combustion chamber.
  • the air ducts have sloping sides which downwardly converge towards one another to define a open-bottom V-shaped channel, the sloping sides primarily supporting the biomass fuel which will be combusted to derive producer gas.
  • the air ducts are hollow and are in fluid communication with a high pressure air source at one end, and with the gasification chamber through air jet openings near their apexes.
  • the high pressure air exits out through the air jet openings placed along the top edges of the air ducts which provides primary air for gasification of the biomass in the channels.
  • the producer gas passes down between the channels and horizontally to an exit.
  • these convention gas reactors works under either counter current gasification or co current gasification and when processing the feedstock results a substantial high ash and tar content.
  • reactors In particular when processing the feedstock at higher temperatures and pressures, the operation of the gasification process becomes more difficult. Further, these reactors cannot be adapted to produce heat and power for all scales of industries to meet the energy requirements. Moreover the above discussed reactors requires feedstock in a specified powdered form or small particulate form of biomass for gasification, and are unable to gasify the large pieces of biomass materials to produce usable heat energy and to suit all levels of industries.
  • the main object of the present invention is to provide an improved gas reactor having combined or selected operation modes of counter current and co current gasification modes to produce tar free gas.
  • Another object of the present invention is to provide a gas reactor which gasify the large pieces of biomass materials and produce usable heat energy to suit all levels of industries.
  • Further object of the present invention is to provide a gas reactor producing usable heat energy which can be scaled up to the of end users demand.
  • a still further object of the invention is to produce heat and power at all levels of industries from multi-flexible conditions.
  • a still further object of the invention is to combine the use of a pre-heater that is self-sustained to give greater gasification efficiency and to allow the use of a moist fuel.
  • the present invention which achieves the objectives relates to a gasification system comprising a stratified counter-current gasification assisted co-current type gasifier operating simultaneously on both modes.
  • the gasification system includes a hopper at the top of the reactor, a top slide door and a bottom slide door arranged with the hopper for ascertaining a leak proof environment inside the gas reactor.
  • An inspection door is provided above the drying zone and this inspection door arrangement enables for maintenance process of the gas reactor and easy access for troubleshooting and inspections.
  • the gas reactor has drying zone, carbonization zone and pyrolysis zone.
  • the hopper is placed above the drying zone with motorized slide valves for feedstock through conveyor system. The feedstock for gasification enters the gasification zone after passing through drying zone and Pyrolysis zone of the gas reactor.
  • the gas reactor is designed to utilize the sensible heat which enhances the process of drying, torrefaction and carbonization and pyrolysis of the feedstock for gasification before entering the gasification zones.
  • the gas reactor comprises of counter current gasification zone and co-current gasification zone.
  • the torrefied carbonized and pyrolyzed feedstock first enters the counter-current gasification zone.
  • the counter-current gasification zone is made with single rows of nozzles arrangements distributed uniformly along the length of the reactor.
  • This counter-current gasification zone is constructed in such a way that, the counter-current air distribution systems and the counter-current fire ignition ports are placed uniformly along the periphery of the reactor.
  • the air from the blower for counter-current gasification enters the zone through counter- current air nozzles having combination of circular and rectangular slot openings.
  • a breaker shaft assembly with shaft arrangement and paddle breakers are placed in between the counter-current zone and the co-current zone.
  • the breaker shaft assembly breaks the larger sized carbonized product to smaller size reduction.
  • the torrefied carbonized and pyrolyzed feedstock then enters the co- current gasification zones with single cyclonic reduction for complete gasification conversion and further reduction to tar-free gases.
  • the co-current gasification zones has a capsule type co-current central buffer chambers with baffles welded on both sides of the reactor along the length of the reactor above the rotating grates for preventing the load of feedstock on the gasification zones.
  • the arrangement of co-current nozzles distribution are made in such a way that the co-current gasification zones is made with multiple rows of side nozzles arrangements distributed uniformly and peripherally all along, the length of the reactor.
  • the air from the blower for gasification enters the co-current gasification zones through co-current air nozzles with circular and rectangular slot openings combination.
  • the gasification system is fully insulated by a special surface lining methodology to achieve maximum thermal efficiency on hot gas condition as well as cold gas efficiency with tar-free gas.
  • Air is introduced into the gasification zone through a manifold along the entire length of the active zone of the reactor supplies sensible heat to be fed through the feedstock material in order to remove the extreme moisture up to 50% before it is fed to the gas reactor.
  • the air which is supplied through the manifold operates in such a manner that the combustion takes place in a co- current environment which prevents the residue and by-products from collecting on the walls of the vessel and completely burns off these products and converts them to hydrocarbon molecules which become part of the fuel.
  • the produced gas from the gas reactor passes through multi cyclone ash separator followed by immersion type venturi scrubber for gas cleaning, vertical column damper with dry filter and finally passing through coarse and fine filters.
  • the cleaned and cooled gases are passed through a buffer tanks and uniformly distributed for power generation.
  • the Counter-current and Co-current gasification air distribution system renders uniform air supply all along the length of the reactor for improved combustion.
  • the gas reactor is fully insulated by a special surface lining methodology to achieve maximum thermal efficiency on hot gas condition as well as cold gas efficiency with tar-free gas.
  • the pressure drop across the rotary grates with adjustable options based on size feedstock for gasification can be uniformly maintained during operation which will help to gasify small particles and pellets also.
  • the load above the cyclonic reduction zone is totally minimised by incorporation of circular and capsule type air distribution ducts and breaker shafts assembly with shaft arrangement and paddle breakers.
  • Fig. 1 shows a schematic diagram of counter current gasification for a thermochemical biomass gas reactor, in accordance to the prior art of the invention.
  • Fig. 2 shows a schematic diagram of co-current gasification for a thermochemical biomass gas reactor, in accordance to the prior art of the invention.
  • Fig. 3 shows a schematic diagram of counter current assisted co-current gasification for a thermochemical biomass gas reactor, in accordance to the exemplary embodiment of the present invention.
  • Fig. 4 shows an illustration of a thermochemical biomass gas reactor constructed for tar free gasification, in accordance to the exemplary embodiment of the present invention.
  • Fig. 5 shows another view of the thermochemical biomass gas reactor, in accordance to the present invention.
  • Fig. 6 shows the gas reactor having counter-current gasification zone and co-current gasification zone, in accordance to the present invention.
  • Fig. 7 shows another view of the gas reactor showing the air nozzles and air distribution system, in accordance to the present invention.
  • Fig. 8 shows left hand side and right hand side views of the air nozzle distribution plate for the gas reactor, in accordance to the present invention.
  • Fig. 9 shows the breaker shaft having paddle breaker for the gas reactor, in accordance to the present invention.
  • Fig. 10 shows the rotary grate assembly for the gas reactor, in accordance to the present invention.
  • the present invention relates to a gas reactor which operates on counter- current assisted co-current gasification to generate tar free gas.
  • Fig. 3 shows a schematic diagram of counter current assisted co-current gasification for a thermochemical biomass gas reactor, in accordance to the exemplary embodiment of the present invention.
  • the gas reactor provides efficient conversion of biomass materials into usable heat energy, by incorporating the combined modes and operational advantages of counter- current and co-current gasification.
  • the gasification system works as a stratified counter-current gasification assisted co-current type gasifier operating simultaneously on both the modes.
  • Fig. 4 and 5 shows views of a thermochemical biomass gas reactor constructed for tar free gasification, in accordance to the exemplary embodiment of the present invention.
  • the gasification system includes a hopper (2) at the top of the reactor, a top slide door (3) and a bottom slide door (4) arranged with the hopper for ascertaining a leak proof environment inside the gas reactor.
  • An inspection door (5) is provided above the drying zone (6) and this inspection door arrangement enables for maintenance process of the gas reactor and easy access for troubleshooting and inspections.
  • the gas reactor has drying zone (6), carbonization zone (7) and pyrolysis zone (8).
  • the hopper (2) is placed above the drying zone (6) with motorized slide valves for feedstock through a conveyor system. The feedstock for gasification enters the gasification zone after passing through the drying zone (6) and Pyrolysis zone (8) of the gas reactor.
  • the feedstock for gasification is conveyed to the hopper (2) through a conveying device from ground level and the hopper gets closed with a top slide door (3) by motorized or pneumatic or hydraulic mechanism based operation on the top after filling the chamber.
  • the bottom slide door (4) is opened after ensuring the closing of top slide door (3).
  • the conveying arrangements are made to ensure uniform charging of feedstock into the gas reactor which prevents feedstock load on the counter-current and co-current gasification zones and the rotary grate assembly (22).
  • the top slide door (3) and the bottom slide door arrangement (4) of the hopper (2) enables leak proof environment inside the gas reactor which is operating under pressure mode. Inspection door arrangements (5) are provided with the gas reactor (1), one above the drying zone (6) and another at reduction zone (1 1).
  • the inspection door arrangements allows for ease of maintenance and easy access for troubleshooting inspections.
  • the gas reactor operates on suction mode for initial start up ignition of charcoal on the counter-current (15) and co-current gasification zones (17) through suction mode for few minutes and changed to pressure mode operation thereafter.
  • the gas reactor is designed to utilize the sensible heat of the process which sequentially enhances the process of drying (6), torrefaction and carbonization (7) and pyrolysis (8) of the feedstock for gasification before entering the gasification zones.
  • the shell of the gas reactor (1) is designed and constructed using Mild Steel (MS) and Stainless Steel (SS) sheet with required thickness on civil foundations or structures or platform (9).
  • the gas reactor comprises of counter current and co-current gasification zone.
  • Ribs (28) are provided to support rectangular flange (27) for strengthening the reactor shell (1) during operation and easy dismantling during cleaning and maintenance.
  • the bottom section of the gas reactor accelerates the gas flow so that the char and ash particles will more likely deposit at the ash collection in conical ash pit with gas cyclonic deflector (1 1) for better settlement of larger particulates through the gas outlet duct (29).
  • the ash collected will be removed from the bottom of the gas reactor using a screw conveyer assembly (12) regulated using a rotary valve (13) for maintaining dry seal below gasification zone. This leak proof arrangement helps discharge the ash continuously from the reactor under dry seal arrangement.
  • FIG. 6 and 7 shows various views of the gas reactor having counter-current gasification zone and co-current gasification zone, in accordance to the present invention.
  • the torrefied carbonized (7) and pyrolyzed (8) feedstock first enters the counter-current gasification zone (15).
  • the counter-current gasification zone (15) is made with single row of nozzle arrangements (14) distributed uniformly along the length of the gas reactor (1).
  • This counter-current gasification zone (15) is constructed in such a way that, the counter- current air distribution systems (25) and the counter-current fire ignition ports (24) are placed uniformly along the periphery of the reactor (1).
  • Fig. 8 shows various views of the air nozzle distribution plate for the gas reactor, in accordance to the present invention.
  • the arrangement of co-current nozzles (23) distribution are made in such a way that the co-current gasification zones (17) is made with multiple rows of side nozzles (23) arrangements distributed uniformly and peripherally all along the length of the reactor.
  • the air from the blower for gasification enters the co-current gasification zones (17) through co-current air nozzles with circular and rectangular slot openings combination (23).
  • the air from the blower for counter-current gasification enters the zone (15) through counter- current air nozzles with circular and rectangular slot openings combination (14).
  • the opposing plurality of nozzles plates are placed such that the nozzles do not face each other throughout the periphery of the reaction zones.
  • the co-current gasification zone (17) are designed in such a way that the co-current air distribution systems (26) and the co-current fire ignition ports (21) are placed uniformly all along the periphery of the smooth-edged rectangular reactor (1).
  • the feedstock for gasification enters the counter- current gasification zone (15) after passing through drying (6) and Pyrolysis (8) zones of the gas reactor to utilize the sensible heat of the process which sequentially enhances the process of drying (6), torrefaction and carbonisation (7) and pyrolysis (8) of the feedstock for gasification before entering the gasification zones (17).
  • the counter-current gasification zone (15) is made with single rows of nozzles (14) arrangements distributed uniformly all along the length of the reactor.
  • counter-current central ducts (18) with baffles are placed along the length of the counter-current gasification zone (15) with single row of counter-current central duct nozzles (14) arrangements focusing side wards.
  • This counter-current gasification zone (15) is constructed in such a way that the counter-current air distribution systems (25) and the counter- current fire ignition ports (24) are placed uniformly all along the periphery of the gas reactor (1).
  • the air from the blower for counter-current gasification enters the gasification zone (15) through counter-current air nozzles with circular and rectangular slot openings combination (14). Charcoal is filled for initial ignition start up inside the counter-current gasification zone (15) above the counter- current nozzles level (14).
  • Fig. 9 shows the breaker shaft having paddle breaker for the gas reactor, in accordance to the present invention.
  • the breaker shaft assembly (16) with shaft arrangement (30) and paddle breakers (31) is incorporated in between the counter-current (15) and co-current (17) gasification zones which are highly effective in breaking the larger sized carbonized product to smaller size.
  • the torrefied carbonized (7) and pyrolyzed (8) feedstock then enters the co-current gasification zones (17) with single cyclonic reduction (1 1) for complete gasification conversion and further reduction to tar- free gases.
  • the co-current gasification zones (17) has capsule type co-current central buffer chambers (18) with baffles welded on both sides of the reactor along the length of the reactor above the rotating grates (22) for preventing the load of feedstock on the gasification zones (17).
  • Fig. 10 shows the rotary grate assembly for the gas reactor, in accordance to the present invention.
  • the rotary grates (22) with horizontal rods assembly (32) operating on rotating shaft arrangements (33) are placed externally below the co-current throat which discharges the ash uniformly preventing clinker formation and bed pressure drop and thus improving the gasification efficiency.
  • the rotating grates (22) are provided with adjustable options based on size feedstock for gasification at low speed rotation which directly supports the gasification zone (17) and made capable of letting ash fall through without excessive loss of fuel conversion.
  • the grates are used to control reactor pressure drop and to maintain the augmented gas production rate.
  • the air from the blower for counter-current gasification enters the counter current gasification zone (15) through counter-current air nozzles with circular and rectangular slot openings combination (14).
  • the gasification system is fully insulated by a special surface lining (20) to achieve maximum thermal efficiency on hot gas condition as well as cold gas efficiency with tar-free gas.
  • charcoal is filled for initial ignition start up inside the counter-current and co current gasification zones (15, 17) above the nozzles level.
  • the small cross sectional area enables radial uniform temperatures, and * uniform air distribution.
  • the feedstock for gasification is conveyed to the hopper (2) through suitable conveying device from ground level and the hopper gets closed with a top slide door (3) by motorized or pneumatic or hydraulic mechanism based operation on the top after filling the chamber.
  • the bottom slide door (4) is opened after ensuring the closing of top slide door (3).
  • the feedstock for gasification enters the counter-current gasification zone (15) after passing through drying (6) and Pyrolysis (8) zones.
  • the gas reactor operates on suction mode for initial start up ignition of charcoal on the counter-current (15) and co- current gasification zones (17) through suction mode for few minutes and changed to pressure mode operation.
  • the air introduced into the gasification zone (17) through a manifold along the entire length of the active zone of the reactor supplies sensible heat to be fed through the feedstock material in order to remove the extreme moisture up to 50% before it is fed to the gas reactor.
  • the air which is supplied through the manifold operates in such a manner that the combustion takes place in a co- current environment (17) which prevents the residue and by-products from collecting on the walls of the vessel and completely bums off these products and converts them to hydrocarbon molecules which become part of the fuel.
  • the torrefied carbonised (7) and pyrolyzed (8) feedstock enters the multi- bed co-current gasification zones (17) with single cyclonic reduction (11) for complete gasification conversion and further reduction to tar-free gases.
  • Capsule type co-current central ducts (18) with baffles are welded on both sides of the reactor along the length of the reactor above the rotating grates (22) that aids in preventing the load of feedstock on the gasification zones (17).
  • the arrangement of co-current nozzles (23) distribution are made in such a way that the co-current gasification zones (17) is made with multiple rows of side nozzles (23) arrangements distributed uniformly and peripherally all along the length of the reactor.
  • side nozzles (23) rectangular pipe with capsule type insulation on the co-current central ducts (18) with baffles are placed along the length of the co-current gasification zones (17) with multiple rows of co-current central duct nozzles (23) arrangements.
  • the char and ash are removed by the rotating paddle breakers (16), grate (22) and rotary valve (13) fitted below the reduction zone. This minimizes the chances of clinker formation in the char ash bed or combustion of the generated producer gas below the reduction zone itself.
  • the Counter-current and Co-current gasification air distribution system renders uniform air supply all along the length of the reactor for improved combustion.
  • the producer gas is passed to the cleaning and cooling devices followed by series of filters and buffer tanks.
  • the produced gas from the gas reactor is passed through multi cyclone ash separator (10) followed by immersion type venturi scrubber for gas cleaning, vertical column damper with dry filter and finally passed through coarse and fine filters.
  • the cleaned and cooled gases are passed through buffer tanks for usage.
  • the interior of the gas reactor shell inner surface is lined with multi- composition layers of firecrete grade, glass powder, wood ash, refractory brick powder and whytheat-A (90% Alumina) dense castable to a suitable thickness.
  • the exterior of the shell is lined glass wool (20), ceramic blanket supported by chicken mesh enclosed in an aluminium cladding.
  • the gas reactor is fully insulated by this special surface lining methodology to achieve maximum thermal efficiency on hot gas condition as well as cold gas efficiency with tar-free gas.
  • the pressure drop across the rotary grates with adjustable options based on size feedstock for gasification can be uniformly maintained during operation to gasify small particles and pellets.
  • the design of the gas reactor is flexible to scale-up for any rated capacity.
  • the length, width and height of the rector can be scaled up to any proportions.
  • the shell of the gas reactor is constructed using Mild Steel (MS) and Stainless Steel (SS) sheet with suitable thickness.
  • MS/SS plate is either rectangular type or rolled in bending machine on four sides to have a single joint welding. This instigates production cost and time reduction, and augments the feedstock and pyrolyzed products to flow freely downwards in stratified reactor avoiding edge losses and prevents clinker formation on sharp edges.
  • the gas reactor according to the present invention allows for sustained gasification at ambient temperature regimes and even at extreme temperatures below 8°C also without any pre-heating process.
  • the rating capacity with feedstock can be doubled while using wood chips or pellets.
  • the gas reactor can also works under pressure below 600 mm of water column.
  • the load above the cyclonic reduction zone is totally minimised by incorporation of circular and capsule type air distribution ducts and breaker shafts assembly with shaft arrangement and paddle breakers. This helps in efficient agitation of char bed avoiding void spaces and clinker formation.
  • the gas reactor can be a square, rectangular, smooth-edged rectangular or smooth edged square shape which can be operated on all types of firewood, coal, refused derived fuel, rubber waste, leather waste, coconut husk, coconut shell, coconut fronds, mango seed and any powdery bio-fuel or agro-wastes in bailed, briquetted or pellet form that generates tar free gas while removing ash and particulate in the proficient manner.
  • the improved gas reactor can handle high bulk density or low bulk density feed materials like leafy/powdery feedstock e.g. sugarcane trash and bagasse, and other agro-waste materials in bailed or briquetted forms.
  • This reactor operates on stratified counter-current assisted co-current gasification mode operating slightly above atmospheric pressure for flexible rating with multi-bed gasification and single cyclonic reduction bed.
  • the gasification zone temperatures are maintained above 1400°C and above to achieve tar-free gas.
  • the gas reactor can accommodate any type of feedstock feed on very larger size (from 50mm of length X 50mm of diameter to 1200mm of length X 300mm of diameter) even with higher bulk density (from 350 to 1500 kg/m 3 ) that is highly comparable over woody feedstock (i.e., around 400kg/ m 3 ) and powdery feedstock (i.e., around 60 kg/ m3) and acceptable even with large woods and long sticks with higher moisture (up to 50%) acceptability.
  • very larger size from 50mm of length X 50mm of diameter to 1200mm of length X 300mm of diameter
  • higher bulk density from 350 to 1500 kg/m 3
  • woody feedstock i.e., around 400kg/ m 3
  • powdery feedstock i.e., around 60 kg/ m3

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention se rapporte à un réacteur à gaz qui comprend une zone de séchage (6), une zone de carbonisation (7) et une zone de pyrolyse (8) pour préparer la charge de biomasse pour la gazéification. La charge de biomasse à gazéifier pénètre dans la zone de gazéification à contre-courant (15) puis dans une zone de gazéification à co-courant (17) après un passage à travers la zone de séchage (6), la zone de carbonisation (7) et la zone de pyrolyse (8) du réacteur à gaz. Le réacteur à gaz est conçu pour fonctionner dans un mode combiné ou dans un mode sélectionné de gazéification à contre-courant et de gazéification à co-courant. Un ensemble d'arbre de broyeur (16) comprenant des systèmes d'arbres (30) et des broyeurs à palettes (31) sont placés entre la zone de gazéification à contre-courant (15) et la zone de gazéification à co-courant (17). Des grilles rotatives (22) et un ensemble de convoyeur à vis (12) sont placés sous la zone de gazéification à co-courant (17) pour décharger les cendres produites dans le réacteur à gaz. Le réacteur thermochimique à gaz travaille dans différentes conditions de charge, de forme, de dimension, de niveaux d'humidité, de densité apparente et est mis en œuvre pour tous les types de biomasse pour les convertir en un gaz exempt de goudron en évacuant les cendres et les particules de manière efficace.
PCT/IN2013/000172 2012-03-19 2013-03-18 Réacteur thermochimique à gaz multi-conditions WO2013140418A1 (fr)

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IN993/CHE/2012 2012-03-19
IN993CH2012 2012-03-19

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2675576C1 (ru) * 2018-04-28 2018-12-19 Федеральное государственное бюджетное образовательное учреждение высшего образования "Российский химико-технологический университет имени Д.И. Менделеева" Способ получения активного угля на основе растительных отходов
CN110184092A (zh) * 2019-07-02 2019-08-30 宁波鑫亮环境科技有限公司 一种汽化炉
WO2021191925A1 (fr) * 2020-03-21 2021-09-30 Amol Carbon Private Limited Conception d'un système de gazéification et procédé de réduction de la formation de goudron

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2638183A1 (de) * 1976-08-25 1978-03-09 William J Vanslyke Verfahren und vorrichtung zur herstellung eines schwefelfreien brennbaren gases
DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
US4452611A (en) 1982-05-24 1984-06-05 Richey Clarence B Downdraft channel biomass gasifier
US5607487A (en) * 1993-03-17 1997-03-04 Taylor; Leland T. Bottom feed - updraft gasification system
DE19718184A1 (de) * 1997-04-30 1998-11-05 Inst Umwelttechnologie Und Umw Verfahren und Vorrichtung zur energetischen Nutzung von Brennstoffen, insbesondere Biobrennstoffen
DE19734343A1 (de) * 1997-08-08 1999-02-11 Wackermann Volker Dipl Forstwi Festbettvergaser im Gleichstromverfahren mit rechteckigem Vergaserquerschnitt in Längsbauweise zur Erzeugung von Schwachgas aus kohlenstoffhaltigen Materialien, insbesondere aus Holz
WO2002046332A2 (fr) * 2000-12-08 2002-06-13 Luterek, Janusz, Franciszek Procede et generateur de gaz destines a la production de gaz de combustion
WO2007102032A2 (fr) * 2006-03-07 2007-09-13 Lampros Elefsiniotis Unité de gazéification combinée à deux étages à cocourant/contre-courant

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2638183A1 (de) * 1976-08-25 1978-03-09 William J Vanslyke Verfahren und vorrichtung zur herstellung eines schwefelfreien brennbaren gases
US4452611A (en) 1982-05-24 1984-06-05 Richey Clarence B Downdraft channel biomass gasifier
DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
US5607487A (en) * 1993-03-17 1997-03-04 Taylor; Leland T. Bottom feed - updraft gasification system
DE19718184A1 (de) * 1997-04-30 1998-11-05 Inst Umwelttechnologie Und Umw Verfahren und Vorrichtung zur energetischen Nutzung von Brennstoffen, insbesondere Biobrennstoffen
DE19734343A1 (de) * 1997-08-08 1999-02-11 Wackermann Volker Dipl Forstwi Festbettvergaser im Gleichstromverfahren mit rechteckigem Vergaserquerschnitt in Längsbauweise zur Erzeugung von Schwachgas aus kohlenstoffhaltigen Materialien, insbesondere aus Holz
WO2002046332A2 (fr) * 2000-12-08 2002-06-13 Luterek, Janusz, Franciszek Procede et generateur de gaz destines a la production de gaz de combustion
WO2007102032A2 (fr) * 2006-03-07 2007-09-13 Lampros Elefsiniotis Unité de gazéification combinée à deux étages à cocourant/contre-courant

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2675576C1 (ru) * 2018-04-28 2018-12-19 Федеральное государственное бюджетное образовательное учреждение высшего образования "Российский химико-технологический университет имени Д.И. Менделеева" Способ получения активного угля на основе растительных отходов
CN110184092A (zh) * 2019-07-02 2019-08-30 宁波鑫亮环境科技有限公司 一种汽化炉
WO2021191925A1 (fr) * 2020-03-21 2021-09-30 Amol Carbon Private Limited Conception d'un système de gazéification et procédé de réduction de la formation de goudron

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