WO2007081296A1 - Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides - Google Patents

Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides Download PDF

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Publication number
WO2007081296A1
WO2007081296A1 PCT/TR2006/000001 TR2006000001W WO2007081296A1 WO 2007081296 A1 WO2007081296 A1 WO 2007081296A1 TR 2006000001 W TR2006000001 W TR 2006000001W WO 2007081296 A1 WO2007081296 A1 WO 2007081296A1
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WO
WIPO (PCT)
Prior art keywords
gasifier
zone
downdraft
syngas
solid waste
Prior art date
Application number
PCT/TR2006/000001
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English (en)
Inventor
Omer Salman
Coskun Mancuhan
Nilufer Selen Onal
Mustafa Tolay
Original Assignee
Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti.
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Application filed by Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti. filed Critical Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti.
Priority to PCT/TR2006/000001 priority Critical patent/WO2007081296A1/fr
Publication of WO2007081296A1 publication Critical patent/WO2007081296A1/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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • 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
    • 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
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • 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
    • C10J2300/0959—Oxygen
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the present invention relates to a new type gasifier which can run by downdraft or updraft to produce syngas from sorted / unsorted municipal solid wastes (MSW), refuse-derived fuel (RDF), industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass.
  • MSW municipal solid wastes
  • RDF refuse-derived fuel
  • industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass.
  • the present invention more particularly, relates to a new type gasifier which can run by updraft or downdraft for minimization of municipal solid wastes (MSW), refuse- derived fuel (RDF) and biomass.
  • the gasifier within the context of the present invention comprises a bottleneck zone, a drying zone, a pyrolysis zone, a reduction and oxidation zone, an ash section, a safety valve, a rotary valve, a vibrator and several igniters.
  • Gasification is the thermochemical conversion of solid material into a gas which can be used to produce electricity by means of a conventional steam-cycle (ie the gas is burned to produce steam in a boiler, to drive a steam turbine) or by direct use in a gas turbine or internal combustion engine.
  • a conventional steam-cycle ie the gas is burned to produce steam in a boiler, to drive a steam turbine
  • This process offers a number of important advantages over the more conventional combustion process: gas has much better burning properties than solids, it is easier to control and it produces less particulate emissions and gaseous pollutants.
  • Power plant based on gasification rather than combustion also have higher overall conversion efficiencies.
  • Updraft reactors are useful for producing gases to be burned at temperature 1000 0 C, but the high tar level up to 10-20% makes them difficult to clean for other purposes.
  • the tar level is intermediate between updraft and downdraft, typically 1-5% in fluidized bed reactors.
  • the low tar levels of downdraft reactors make them more suitable for uses requiring clean gas, which contain 0.1% tar.
  • updraft counterflow gasification
  • the preheated air or oxygen and if it is necessary the steam contacts charcoal on a grate, generating gas temperatures of 1000- 1400 0 C.
  • This hot gas rises through the down coming biomass, pyrolizing it at successively lower temperatures and eventually drying it. All of the types of tar occur in the final gas, with primary tars dominating, typically at a level of 10-20%.
  • Unit capacity restriction is a disadvantage for downdraft gas producers. So, multiple units operating in parallel when higher capacity is desired. A lower overall efficiency and difficulties in handling higher moisture and ash content are also the following disadvantages.
  • crossdraft gas producer high exit gas temperature, poor CO2 reduction, high gas velocity are disadvantages.
  • the ash bin, fire and reduction zone in crossdraft gasifiers are separated. These design characteristics limit the type of fuel for operation to low ash fuels such as wood, charcoal and coke.
  • the relatively higher temperature in cross draft gasifier has an obvious effect on gas composition such as high carbon monoxide, and low hydrogen and methane content when dry fuel such as charcoal is used.
  • WO 2005047435 discloses a gasifier for the gasification of biomass and waste to produce combustible effluent, comprising: a fuel valve for loading solid fuel into a first oxidation zone; a first throat defining the lower edge of the first oxidation zone; a second throat defining the lower edge of a second oxidation zone; a reduction zone linking the first oxidation zone to the second oxidation zone and; two oppositely located (at the reduction zone) vortex discharge pipes for the combustible effluent wherein in the first oxidation zone the gas flow is in the same direction as fuel flow and in the second oxidation zone the gas flow is in the opposite direction to the fuel flow.
  • US 4306506 discloses an apparatus for the conversion of solid fuels and solid organic waste materials by high temperature gasification into gaseous fuel called "producer gas".
  • the apparatus comprises a stacked two-section gasifier defining sequentially descending drying, distillation, oxidation and reduction reaction zones through which a column of the solid fuel descends during its conversion to the gaseous fuel.
  • the lower reactor section is of double-shell construction and defines the lower oxidation and reduction reaction zones.
  • Means are provided for drawing air into the oxidation zone for burning reaction with carbonized fuel passing therethrough and for thereafter drawing reaction gases downwardly through the lower reduction zone of the gasifier and then through the annular space defined by the double-shell structure of the lower section in indirect counter-current heat exchange relationship with the fuel column portion in the oxidation and reduction zones.
  • the inner shell element of the lower section is arranged in hanging manner within its associated outer shell element to allow expansion of the double-shell structure under the high temperature conditions experienced by the gasifier without harmful stress build-up in the apparatus.
  • the inner shell element supports within its lower portion two stacked funnel-shaped transition pieces which form a series of throat-like constrictions for supporting the fuel column in the gasifier and which cause localized increase in the velocity of the gases passing downwardly therethrough and leaving the reduction zone of the reactor.
  • US 4309195 discloses an apparatus for effecting the conversion of solid fuels (including solid organic waste materials having a fuel valve) by high temperature gasification into clean-burning and uniform gaseous fuel called "producer gas.”
  • the apparatus comprises a two-section, stacked double-shell gasifier reactor defining sequentially descending, drying, distillation, oxidation and reduction reaction zones through which a continuously fed column of the solid fuel descends during its conversion to a gaseous fuel.
  • Means are provided for drawing process air into the oxidation zone for burning reaction with carbonized fuel passing therethrough and for thereafter drawing reaction gases in downdraft fashion through the lower fuel reduction zone of the gasifier and thence in sequence through the annular space defined by the double-shell structure of the lower section of the gasifer in indirect countercurrent heat exchange relationship with the fuel column portion in the oxidation and reduction zones and through the annular space defined by the double- shell structure of the upper section of the gasifier in indirect co-current heat exchange relationship with the fuel column portion in the drying and distillation zones.
  • the inner shell elements of the two sections of the stacked double-shell reactor structure are arranged in hanging manner within their respective outer shell elements to allow expansion of the double-shell structure under the high temperature conditions experienced by the gasifier without harmful stress build-up in the apparatus.
  • the gasifier is needed which has unique and optimum design, produces less tar and heavy metals, prevents explosion risk and uncontrolled air leakage. Also it must be harmless to the environment and economically viable. 5 I V ⁇ I / I M -- " " ⁇ - -
  • the main scope of the present invention is to develop a new type gasifier for the sorted / unsorted municipal solid wastes (MSW), refuse-derived fuel (RDF), industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass minimization.
  • MSW sorted / unsorted municipal solid wastes
  • RDF refuse-derived fuel
  • industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass minimization.
  • a further objective of the present invention is to minimize formation of tar and heavy metals.
  • Another objective of the present invention is to produce of synthesis gas (syngas) or fuel gas under atmospheric or elevated pressure.
  • Another objective of the present invention is to develop a new type gasifier which is harmless to the environment and economically viable.
  • a new type gasifier was developed which can run either updraft or downdraft to produce syngas from municipal solid waste (MSW), refuse-derived fuel (RDF) and biomass.
  • MSW municipal solid waste
  • RDF refuse-derived fuel
  • Mentioned gasifier comprises a fuel inlet, a drying zone, a pyrolysis zone, a reduction and oxidation zone, an ash section and igniters, together with necessary equipment for process control.
  • Figurei one example of the gasifier of the present invention.
  • gasifier (1) to produce syngas from sorted / unsorted municipal solid wastes (MSW), refuse-derived fuel (RDF), industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass would typically be as follows:
  • the present invention relates to a new type gasifier (1) which can run updraft or downdraft for the sorted / unsorted municipal solid wastes (MSW), refuse-derived fuel (RDF), industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass minimization.
  • MSW municipal solid wastes
  • RDF refuse-derived fuel
  • industrial wastes including waste water treatment plant sludge, leather industry residues, agricultural wastes and biomass minimization.
  • syngas production is the process of converting biomass and solid waste into combustible gases (carbon monoxide, methane and hydrogen) that ideally contain all the energy originally present in the solid or liquid carbon-based material (feedstock).
  • energy conversion efficiencies lie between 60% and 90%. It can be broadly defined as the thermochemical conversion of a solid or liquid carbon- based material feedstock into a combustible gaseous product (combustible gas) by the supply of a gas production agent (partial oxidation) under the application heat. Oxidation can be done either by using air or oxygen. If oxygen is used, the resulting gas (syngas) will have a higher calorific value.
  • thermochemical conversion changes the chemical structure of the feedstock by means of high temperature.
  • the agent introduced allows the feedstock to be quickly converted into gas by means of different heterogeneous reaction.
  • the combustible gas contains CO 2 , CO, H 2 , CH 4 , H 2 O, N 2 , and trace amounts of higher hydrocarbons, inert gases present in the gas production agent, various contaminants such as small char particles, ash and tars.
  • Direct process occurs when an oxidant agent is used to partially oxidize the feedstock.
  • the oxidation reactions supply the energy to keep the temperature of the process up. If the process does not occur with an oxidizing agent, it is called indirect gas production and needs an external energy source.
  • the moisture content in the feedstock which produces steam is the most commonly used indirect process agent, because it is easily produced and increases the hydrogen content of the combustible gas.
  • This process does produce hydrocarbon liquids, such as tars and oils, limiting the ability to handle fines.
  • dusty tars taken out in downstream separation processes, are recycled back to the top of the gasifier (1 ).
  • the dusty tars are believed to "stick" or conglomerate the smaller fragments of the solid waste and biomass together, obtaining the necessary size requirements of the solid waste gasifier (1 ).
  • parameters that need to be maintained within certain limits. These include: particle size distribution, moisture content, ash content, volatile matter content, heating value, bulk density, feedstock composition.
  • Particle size distribution is important to ensure that the flow of matter through the reactor is uniform and blockage does not occur through agglomeration. It is also necessary to ensure that particle size is not such that heat transfer to the full mass of the feedstock is prevented.
  • the ideal situation is to have a high surface area and a low mass. As the particles get smaller, however, problems of dust formation and pass-out from the gasifier (1 ) can occur.
  • moisture content As it increases the thermal efficiency of conversion decreases. There comes a point at which the amount of heat required for drying becomes excessive and this provides an upper limit to acceptable moisture contents for gasification systems. In practice it is desirable for the moisture content to be between 10% and 20% in the feedstock. Moisture is actually involved in the biomass conversion process, providing the hydrogen molecules for hydrogen gas formation and for very dry feeds may have to be made up with the injection of steam.
  • MSW typically having moisture contents of approximately 50% it is necessary for some drying to occur, before the feedstock is fed into the gasifier (1).
  • the total ash content in the biomass and the chemical composition of the ash are both important.
  • the composition of the ash affects its behavior under the high temperatures of combustion and gas production. For example, melted ash may cause problems in gas producers. Such problems may vary from clogged ash- removal caused by slagging ash to severe operating problems from ash accumulation within the thermal reactor.
  • Volatile matter refers to the part of the biomass that is released when the biomass is heated. During this heating process the biomass decomposes into volatile gases and solid char. Biomass and solid waste typically have a high volatile matter content (up to 80%) whereas coal, for example, has a volatile matter content of less than 20%.
  • the heating value of differing biomass substrates can vary significantly. Biomass and solid waste, for example, can vary from 10MJ/kg to 20MJ/kg. Bulk density will also vary significantly with the type of waste that is being gasified.
  • Uniform feedstock composition is preferable as this ensures that product gas composition will remain stable and provide less difficulty for subsequent usage technologies.
  • the gasifier (1) gasifies pelletized, refuse-derived fuel (RDF).
  • RDF refuse-derived fuel
  • Gasifier (1 ) is used alternately to feed low-energy gas to drive an internal combustion engine (ICE) with 1 MWe and heat (2 MWth) production capacity.
  • ICE internal combustion engine
  • Biomass or coal + O 2 -> CO + H 2 (carbon monoxide and hydrogen) 2. Water gas shift adjusts CO/H 2 ratio
  • Process relies on chemical processes at elevated temperatures >1000°C.
  • the rotary valve (8) integrated to the system which prevents uncontrolled air leakage, for security purposes and control fuel feed rate. Air inlet from the top of the gasifier (1) from the bottleneck zone (2).
  • Vibrator (9) is mantled to the gasifier (1) since the feedstock material in the gasifier (1 ) is not at the same level all the time, but there may become small peaks inside. In order to evenly distribute the feedstock vibrations are applied at certain periods.
  • Gasifier (1) produces syngas which mainly consists of CO, H 2 , CO 2 , CH 4 .
  • Reactant agent for the process to occur is only the air at environmental conditions.
  • the reactor contains air preheater, O 2 supplier and steam generator are activated in case of necessity.
  • Gasifier (1 ) can be operated under the vacuum conditions.
  • gasifier (1 ) can be considered under downdraft (coflow) gasification reactor umbrella where the flame temperatures are 1000- 1400 0 C, but the flame occurs in the interstices of the pyrolysing particles whose temperatures are 500-700 0 C, so that about 0.1 % of the primary tars are converted to secondary tars and the rest are burned to supply the energy for pyrolysis and char gasification. Very few of the compounds found in downdraft gasification are found in updraft reactors and vice-versa. Because of low tar production abilities, the downdraft type has been chosen as the design parameter and in addition to that flexible feedstock properties played a major role for the selection of updraft and downdraft design parameters.
  • the solid waste gasifier (1 ) operates at close to atmospheric pressure at approximately 600 0 C, employing air or O 2 as the process / fluidized agent.
  • the product gas as a result of gasification process is assumed with the below characterization.
  • FIG. 1 Figurei illustrates one example of the gasifier (1 ) which can run either updraft or downdraft of the present invention.
  • Refuse-derived fuel (RDF) or any other solid waste pellets should have diameter of 20 - 100 mm in order to be properly gasified in the gasifier (1).
  • Feedstock input (RDF pellets) before solid waste gas production is assumed to be the best with the below characterization.
  • Fuel that is too large or too moist is generally the cause of feed line plugging, although backpressure may also prevent the fuel from moving forward. Measures should be taken to insulate the line and prevent the system from reaching temperatures at which pyrolysis commences.
  • the fuel-feeding systems convey the fuel from storage bins and hoppers to the gasifier (1 ).
  • An ideal feeding system provides smooth and continuous feeding and allows for accurate control of the feed rate by hopper weighing and rotary valve (8).
  • the system should be relatively insensitive to variations of fuel size and must maintain sufficient pressurization to prevent the backflow of gases from the gasifier (1) to the feeding system.
  • the fuel-feeding system consists of two parts: fuel transport from storage to the gasifier (1 ) and injection into the gasifier (1). Feedstock flow to the gasifier (1) is controlled over the rotary valve (8) and also a safety valve (10) is integrated to the gasifier (1 ).
  • Particles of fuel 20 to 100mm. in diameter are introduced into the gasifier (1) from the top, while the oxidant agent (air or O 2 ) enters from the top oxidation zone and bottleneck zone (2).
  • the solid waste gasifier (1 ) can be broken up into zones, which blows out the uncontrolled gas pressure formed as a result of water vaporization and gas formation from volatile organics.
  • the solid waste is heated and dried while cooling the product gas that is about to leave the gasifier (1 ).
  • This zone may have the temperature up to 400 0 C.
  • the fuePs water evaporates to the vapour phase; which is necessary to produce H 2 in the reaction zone.
  • syngas suction occurs in the syngas zone (3.1 ) of the gasifier (1 ).
  • the hot gas coming upwards from the bottom of the gasifier (1 ) heats up the material inside during its transport.
  • the syngas is taken out from higher syngas outlet zone (3.2) and transferred into cyclones for gas cleaning.
  • the temperature of syngas at the higher syngas outlet zone (3.2) can be up to maximum 400 0 C. This higher syngas outlet zone (3.2) is active when the process is in updraft mode. Pyrolysis
  • Briquetted waste is broken down to coke, tar, CH 4 , H 2 , in the pyrolysis zone (4) which is between 400 - 600 0 C. Tar formation is at highest level.
  • the material is thermally degraded in pyrolysis zone (4) and various types of aromatic hydrocarbons are produced. Depending on the chemical reactions, heavy tars, light tars or water soluble hydrocarbons or aromatic compounds can be produced in this part of the process.
  • air nozzle (4.2) positions can be changed which has an effect on the entrance angle of the air to the gasifier (1 ). This situation increases the efficiency of the process.
  • the air enters the gasifier (1 ) in the atmospheric temperature and heated up in the air chamber (4.3); where the temperature depends on the pyrolysis zone (4) and on the sucked air flow rate. There the optimum air temperature distribution is evenly realized. Homogenization of appropriate air temperature is realized. This zone prevents the heat loss out from the system.
  • the solid waste gas is between 1000 - 1200 0 C
  • the H 2 O and O 2 in the introduced air or O 2 reacts with coke and output gas is called solid waste gas (SWG) which mainly consists of CO, H 2, CO 2 , CH 4 , at temperature between 1000 - 1200 0 C.
  • SWG solid waste gas
  • Steam feeding to the reduction and oxidation zone (5) is optional.
  • the MSW runs through the descendent zone the SWG cools down to 600 - 800 0 C.
  • the gas sucking to the gasifier (1) is realized downwards and at the updraft working conditions the gas is sucked upwards.
  • SWG is sucked to the cleaning system after it reaches 400 - 600 0 C in the gasifier (1).
  • the syngas is taken out from this lower syngas outlet zone (5.1) and transferred into cyclones for gas cleaning.
  • the temperature of syngas at the lower syngas outlet zone (5.1 ) can be up to maximum 400 0 C.
  • This lower syngas outlet zone (5.1 ) is active when the process is in downdraft mode. As a result of the optimization and development, the minimum possible tar and particle material content in a downdraft gasifier (1 ) is reached within the context of the present invention.
  • the air chamber (4.3) functions for the cooling of ash section (6).
  • the temperature of cooling air at the cooling air inlet (5.2) is between 35-7O 0 C.
  • the heated air sucked from this zone during downdraft conditions is used as combustion air in gas burners for the heat economy.
  • the preheated air for gasification purposes is sucked into the gasifier (1 ) by means of lower preheated air or oxygen inlet (5.3).
  • the gasification process produces ash which has to be extracted from the system by means of ash discharger (6.4) located at the ash section (6).
  • ash discharger located at the ash section (6).
  • the formed ash is extracted in certain quantities from the bottom of the gasifier (1).
  • Ash grate (6.1) is made out of a special material which is high temperature resistant; so that the syngas in the accumulated ash content in this portion can be sucked easily. The necessary porosity has been realized at the ash material for the easy gas transfer. In addition to that, ash agglomeration and syntherization have been prevented.
  • Air nozzles (6.2) located at this portion of the gasifier (1 ) are manually opened. These have to be closed during downdraft running, otherwise the syngas is burnt with the help of the inlet air coming from these air nozzles (6.2) which is not appreciated at all.
  • the air chamber (6.3) functions for the cooling of ash section (6).
  • the temperature of cooling air is between 35-70 0 C.
  • the heated air sucked from this zone during downdraft conditions is used as combustion air in gas burners for the heat economy.
  • Gasifier (1 ) ash residues could be used to fertilize the ground (rarely if the feedstock is not agricultural waste), as the concrete material or disposed in a sanitary landfill. Instead, solid residues of gas pre-treatment and air pollution control systems are typically disposed in landfills, because of their high heavy metal concentration level. Sometimes, solid residues can be used in industrial processes, such as cement mills, for a complete integration between gasification and industrial processes.
  • the present gasifier (1 ) is currently putting on efforts on necessary mechanical changes so that it will be possible to change the mode from downdraft to updraft or from updraft to downdraft working conditions during the process, without any interruptions.
  • Igniters (7) are located in the middle air chamber (6.3) which are used for start up of the process and to heat up the systems.
  • the two igniters (7) on both sides of the gasifier (1) are using propane gas initially and once the system reaches its steady state these are switched off, and from that point on system is ran by its own product syngas.
  • the number of igniters (7) can be increased in case of necessity.

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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

La présente invention concerne un nouveau type de gazogène (1) qui peut fonctionner par écoulement descendant/ascendant pour produire du gaz de synthèse à partir de déchets solides urbains (DSU) triés ou non triés, de combustible dérivé de déchets (CDD), de déchets industriels, y compris de boues d'usine de traitement des eaux usées, de résidus de l'industrie du cuir, de déchets agricoles et de biomasse. Ledit gazogène comprend une zone d'étranglement (2), une zone de séchage (3), une zone de pyrolyse (4), une zone de réduction et d'oxydation (5), une section pour les cendres (6), une vanne de sûreté (10), une vanne rotative (8), un vibreur (9) et plusieurs allumeurs (7).
PCT/TR2006/000001 2006-01-16 2006-01-16 Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides WO2007081296A1 (fr)

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Cited By (26)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009020442A1 (fr) * 2007-08-03 2009-02-12 Detes Maden Enerji Ve Cevre Teknoloji Sistemleri Limited Sirketi Système de gazéification de combustible solide et de nettoyage du gaz produit
WO2009040573A2 (fr) 2007-09-25 2009-04-02 Refgas Limited Gazéification
WO2009066187A1 (fr) 2007-11-19 2009-05-28 Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti. Gazéificateur et procédés de gazéification l'utilisant
WO2010019662A1 (fr) * 2008-08-12 2010-02-18 4A Technologies, Llc Système modulaire et procédé de production d'urée à l'aide d'une charge d'alimentation formée d'une biomasse
FR2937333A1 (fr) * 2008-10-17 2010-04-23 Jean Xavier Morin Procede et dispositif d'extraction de dioxyde de carbone de l'atmosphere
EP2537911A1 (fr) 2011-06-21 2012-12-26 Stirling.DK ApS Gazogène vertical doté de moyens d'humidification
WO2013034608A1 (fr) 2011-09-05 2013-03-14 Xylowatt S.A. Gazeifieur de combustible solide carbone
EP2589870A1 (fr) 2011-11-07 2013-05-08 Stirling.DK ApS Gazogène ascendant et grille de gazogène
GB2499329A (en) * 2013-02-26 2013-08-14 Slg Technology Ltd Thermal energy plant for utilising waste from the tanning process
US8574325B2 (en) 2010-07-21 2013-11-05 Responsible Energy Inc. System and method for processing material to generate syngas
CN103756729A (zh) * 2014-02-19 2014-04-30 内蒙古科技大学 脉冲下吸式固定床高温气化炉
CN103773505A (zh) * 2014-01-27 2014-05-07 淄博太沣环保工程有限公司 生物质双段式燃气发生炉
CN103797095A (zh) * 2011-07-14 2014-05-14 瑞普可再生能源产品有限责任公司 用于气化生物质的装置及方法
ITTO20130332A1 (it) * 2013-04-23 2014-10-24 Solidia S R L Impianto per la trasformazione di un materiale a base organica in gas di sintesi
CN104588388A (zh) * 2013-10-30 2015-05-06 河北赢丰再生资源利用有限公司 一种含铬皮革废弃物的综合利用方法
US9170019B2 (en) 2008-08-30 2015-10-27 Dall Energy Holdings ApS Method and system for production of a clean hot gas based on solid fuels
US9352329B2 (en) 2008-08-12 2016-05-31 4A Technologies, Llc Modularized system and method for urea production using a bio-mass feedstock
US9803150B2 (en) 2015-11-03 2017-10-31 Responsible Energy Inc. System and apparatus for processing material to generate syngas in a modular architecture
CN108059979A (zh) * 2017-12-15 2018-05-22 湖南阳东生物洁能科技有限公司 一种生物质气化方法及装置
WO2018146179A1 (fr) * 2017-02-13 2018-08-16 Ecoloop Gmbh Production de gaz de synthèse à partir de substances riches en carbone au moyen d'un procédé combiné de co-courant et contre-courant
CN110395865A (zh) * 2019-07-23 2019-11-01 华北水利水电大学 一种自动控制及监测的污泥低温阴燃热解装置
CN110791324A (zh) * 2019-11-18 2020-02-14 湖南省林业科学院 一种微波耦合液氧辅助木本油料剩余物热解气化方法
WO2020058865A1 (fr) * 2018-09-19 2020-03-26 Sicit Chemitech S.P.A. Procédé de traitement de déchets organiques émanant d'un cycle de tannage
RU199402U1 (ru) * 2020-01-17 2020-08-31 Федеральное государственное автономное образовательное учреждение высшего образования "Сибирский федеральный университет" (ФГАОУ ВО СФУ) Двухрежимный газогенератор
WO2023102579A1 (fr) 2021-12-01 2023-06-08 Cochrane William Thomas Gazogène
RU220055U1 (ru) * 2023-03-01 2023-08-23 Федеральное государственное автономное образовательное учреждение высшего образования "Сибирский федеральный университет" Многостадийный газогенератор комбинированного дутья

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EP1167492A2 (fr) * 2000-06-23 2002-01-02 Gesellschaft für Nachhaltige Stoffnutzung mbH Procédé et installation pour la production d' un gaz combustible à partir de biomasse
WO2005095551A1 (fr) * 2004-04-02 2005-10-13 Kbi International Ltd. Reacteur de traitement thermique de dechets comportant un canal d'alimentation

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EP0118929A1 (fr) * 1983-02-14 1984-09-19 Shell Internationale Researchmaatschappij B.V. Méthode pour transporter des matières sous forme de particules
WO2001051591A1 (fr) * 2000-01-10 2001-07-19 Fuerst Adrian Dispositif et procede pour produire des gaz combustibles
EP1167492A2 (fr) * 2000-06-23 2002-01-02 Gesellschaft für Nachhaltige Stoffnutzung mbH Procédé et installation pour la production d' un gaz combustible à partir de biomasse
WO2005095551A1 (fr) * 2004-04-02 2005-10-13 Kbi International Ltd. Reacteur de traitement thermique de dechets comportant un canal d'alimentation

Cited By (38)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009020442A1 (fr) * 2007-08-03 2009-02-12 Detes Maden Enerji Ve Cevre Teknoloji Sistemleri Limited Sirketi Système de gazéification de combustible solide et de nettoyage du gaz produit
AU2008303334B2 (en) * 2007-09-25 2012-09-27 Refgas Limited Downdraft refuse gasification
WO2009040573A2 (fr) 2007-09-25 2009-04-02 Refgas Limited Gazéification
WO2009040573A3 (fr) * 2007-09-25 2009-08-13 Refgas Ltd Gazéification
GB2453111B (en) * 2007-09-25 2010-12-08 Refgas Ltd Gasification
WO2009066187A1 (fr) 2007-11-19 2009-05-28 Gep Yesil Enerji Uretim Teknolojileri Ltd. Sti. Gazéificateur et procédés de gazéification l'utilisant
EA017588B1 (ru) * 2007-11-19 2013-01-30 Геп Есил Энерджи Уретим Текнолоджилери Лтд. Сти. Газификатор и способы газификации с его использованием
US20110005135A1 (en) * 2007-11-19 2011-01-13 Omer Salman Gasifier and gasification methods using thereof
WO2010019662A1 (fr) * 2008-08-12 2010-02-18 4A Technologies, Llc Système modulaire et procédé de production d'urée à l'aide d'une charge d'alimentation formée d'une biomasse
US9738598B2 (en) 2008-08-12 2017-08-22 Trimec Biogas Technology Ltd. Modularized system and method for urea production using a bio-mass feedstock
US9352329B2 (en) 2008-08-12 2016-05-31 4A Technologies, Llc Modularized system and method for urea production using a bio-mass feedstock
US8618325B2 (en) 2008-08-12 2013-12-31 4A Technologies, Llc Modularized system and method for urea production using a bio-mass feedstock
RU2510391C2 (ru) * 2008-08-12 2014-03-27 4А Текнолоджис, Ллс Модульная система и способ получения мочевины из биомассы
US9170019B2 (en) 2008-08-30 2015-10-27 Dall Energy Holdings ApS Method and system for production of a clean hot gas based on solid fuels
FR2937333A1 (fr) * 2008-10-17 2010-04-23 Jean Xavier Morin Procede et dispositif d'extraction de dioxyde de carbone de l'atmosphere
US9080116B2 (en) 2010-07-21 2015-07-14 Responsible Energy Inc. System and method for processing material to generate syngas using water injection
US9505996B2 (en) 2010-07-21 2016-11-29 Responsible Energy Inc. System and method for processing material to generate syngas using plurality of gas removal locations
US8574325B2 (en) 2010-07-21 2013-11-05 Responsible Energy Inc. System and method for processing material to generate syngas
EP2537911A1 (fr) 2011-06-21 2012-12-26 Stirling.DK ApS Gazogène vertical doté de moyens d'humidification
CN103797095A (zh) * 2011-07-14 2014-05-14 瑞普可再生能源产品有限责任公司 用于气化生物质的装置及方法
JP2014525489A (ja) * 2011-09-05 2014-09-29 キシロワット エス．エー． 固体炭素燃料用ガス化装置
WO2013034608A1 (fr) 2011-09-05 2013-03-14 Xylowatt S.A. Gazeifieur de combustible solide carbone
EP2589870A1 (fr) 2011-11-07 2013-05-08 Stirling.DK ApS Gazogène ascendant et grille de gazogène
GB2499329A (en) * 2013-02-26 2013-08-14 Slg Technology Ltd Thermal energy plant for utilising waste from the tanning process
GB2499329B (en) * 2013-02-26 2014-01-01 Slg Technology Ltd A thermal energy plant for and process of utilising waste from the tanning process
ITTO20130332A1 (it) * 2013-04-23 2014-10-24 Solidia S R L Impianto per la trasformazione di un materiale a base organica in gas di sintesi
CN104588388A (zh) * 2013-10-30 2015-05-06 河北赢丰再生资源利用有限公司 一种含铬皮革废弃物的综合利用方法
CN103773505A (zh) * 2014-01-27 2014-05-07 淄博太沣环保工程有限公司 生物质双段式燃气发生炉
CN103756729A (zh) * 2014-02-19 2014-04-30 内蒙古科技大学 脉冲下吸式固定床高温气化炉
US9803150B2 (en) 2015-11-03 2017-10-31 Responsible Energy Inc. System and apparatus for processing material to generate syngas in a modular architecture
WO2018146179A1 (fr) * 2017-02-13 2018-08-16 Ecoloop Gmbh Production de gaz de synthèse à partir de substances riches en carbone au moyen d'un procédé combiné de co-courant et contre-courant
CN108059979A (zh) * 2017-12-15 2018-05-22 湖南阳东生物洁能科技有限公司 一种生物质气化方法及装置
WO2020058865A1 (fr) * 2018-09-19 2020-03-26 Sicit Chemitech S.P.A. Procédé de traitement de déchets organiques émanant d'un cycle de tannage
CN110395865A (zh) * 2019-07-23 2019-11-01 华北水利水电大学 一种自动控制及监测的污泥低温阴燃热解装置
CN110791324A (zh) * 2019-11-18 2020-02-14 湖南省林业科学院 一种微波耦合液氧辅助木本油料剩余物热解气化方法
RU199402U1 (ru) * 2020-01-17 2020-08-31 Федеральное государственное автономное образовательное учреждение высшего образования "Сибирский федеральный университет" (ФГАОУ ВО СФУ) Двухрежимный газогенератор
WO2023102579A1 (fr) 2021-12-01 2023-06-08 Cochrane William Thomas Gazogène
RU220055U1 (ru) * 2023-03-01 2023-08-23 Федеральное государственное автономное образовательное учреждение высшего образования "Сибирский федеральный университет" Многостадийный газогенератор комбинированного дутья

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