EP0055440A1 - Procédé et installation pour la production continue de gaz combustible à partir de déchets organiques - Google Patents

Procédé et installation pour la production continue de gaz combustible à partir de déchets organiques Download PDF

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Publication number
EP0055440A1
EP0055440A1 EP81110618A EP81110618A EP0055440A1 EP 0055440 A1 EP0055440 A1 EP 0055440A1 EP 81110618 A EP81110618 A EP 81110618A EP 81110618 A EP81110618 A EP 81110618A EP 0055440 A1 EP0055440 A1 EP 0055440A1
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EP
European Patent Office
Prior art keywords
shaft
gasification
shaft furnace
discharge
gasified
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP81110618A
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German (de)
English (en)
Inventor
Heinz Mallek
Manfred Dr. Laser
Dorothee Ermisch
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Forschungszentrum Juelich GmbH
Original Assignee
Forschungszentrum Juelich GmbH
Kernforschungsanlage Juelich GmbH
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Filing date
Publication date
Priority claimed from DE19803049251 external-priority patent/DE3049251A1/de
Priority claimed from DE19813112975 external-priority patent/DE3112975A1/de
Application filed by Forschungszentrum Juelich GmbH, Kernforschungsanlage Juelich GmbH filed Critical Forschungszentrum Juelich GmbH
Publication of EP0055440A1 publication Critical patent/EP0055440A1/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • 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
    • C10J3/30—Fuel charging 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
    • C10J3/32—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
    • 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
    • C10J2300/0913—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
    • 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
    • C10J2300/0969—Carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as 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
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • 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

Definitions

  • the invention relates to a process for the continuous production of fuel gas from organic waste, in which the waste in the continuous flow of material is first dried and degassed in the absence of air at temperatures rising up to about 550 ° C. and then gasified at higher temperatures.
  • the invention relates to two alternative procedures for performing the method and devices for performing these alternative procedures.
  • T rocknungs-, degassing, gasification and V erbrennungsreae run continuously thereby from l i ch.
  • An embers bed is formed from the degassing products entering the gasification chamber, into which air is conducted in sufficient quantities so that it has a sufficient volume and also a sufficient temperature level.
  • the gasification gases produced in this process do not have such a uniform composition that transport to a consumer in another location is worthwhile.
  • the production of fuel gas from wood, coal or coke is known.
  • the fuel gas is formed by incomplete combustion of the material in a generator designed like a shaft furnace, in which air and oxygen are used as gasifying agents and / or water vapor is introduced.
  • the resulting generator gas essentially contains carbon monoxide and hydrogen and a small proportion of methane as combustible gas components.
  • the remaining gas components of the generator gas are nitrogen and carbon dioxide.
  • the gas generation process is endothermic. The aim is to generate the generator gas at the highest possible temperatures in order to obtain high levels of carbon monoxide and hydrogen.
  • the invention has for its object to provide procedures which make it possible to produce a gas of uniform composition, which is suitable for external use, in continuous operation by gasifying organic waste.
  • the generation of the fuel gas should be easy to regulate, in particular with regard to the different waste materials available, which in many cases also arise in a heterogeneous flow of material during continuous operation, and thereby result in good efficiency. It is also an object of the invention to provide technically simple facilities for performing the method.
  • a solution (claim 1) of the task is that the degassed Good, of the goods during the material flow corresponding amounts rgasungsmitteln to its gasification, which takes place at temperatures up to about 1000 ° C at the latest at the start of the gasification phase to the changes of the composition of Ve as Air, steam, CO 2 , p 2 or a mixture of these substances is added.
  • the invention represents a further development of the known methods in that the gasification agents are supplied to the substances to be gasified from the start during the gasification process in direct current. It is thereby achieved that the gasification process is much easier to control than before, because the addition of gasification agents can be controlled in a simple manner depending on the composition of the gases formed during gasification and the solid, combustible substances.
  • An alternative solution (claim 2) is that the drying, degassing and gasification of the waste materials is carried out in two procedurally separate steps, by drying and degassing the waste materials in the first step and the material resulting from the degassing is gasified in the second step, the substances being guided in such a way that the material flow between the first and the second process step can be interrupted for the purpose of mechanical treatment of the material resulting from the degassing and that the degassed material is used for the same Gasification, which takes place at temperatures up to about 1000 ° C, at the beginning of the gasification phase, corresponding amounts of gasification agents such as air, steam, CO 2 , 0 2 or a mixture of these substances are added to the changes in the composition of the material during the material flow.
  • gasification agents such as air, steam, CO 2 , 0 2 or a mixture of these substances are added to the changes in the composition of the material during the material flow.
  • the gasification agent is supplied to the material to be gasified in the direction of flow of the material together with gases formed during drying and degassing (claim 3).
  • the released during drying steam to form water gas for the gasification of carbon and emissions from the degassing of the waste carbonization gases is the A of the long-chain hydrocarbon molecules ufcracken in low molecular weight compounds in the gasification temperature above the formed during degassing coke passed and so waste material to a non-insignificant portion implemented in high quality connections. It is useful that in the gasification itself training ember bed for cracking carbonization gases air and / or oxygen is added (claim 4).
  • the gasification agent is added depending on the temperature to the glowing bed formed during the gasification (claim 5).
  • the gasification agent is preferably introduced into the zone to be gasified in a zone in which the zone has a temperature of approximately 200 ° C (claim 6).
  • the fuel gas developed during the gasification is removed via a gap-shaped passage, the material being held above the gap until it is gasified (claim 7). It is also advantageous that the fuel gas formed is used in recuperative heat exchange for preheating the material to be gasified (claim 8).
  • a shaft furnace is provided with a filling device arranged at the top of the shaft, with a device for emitting heat, for drying and degassing the material located in the upper part of the shaft and a device for emitting heat for gasifying the material in the lower part of the shaft, at the bottom of the shaft a discharge for the ashes is provided.
  • a device for emitting heat, for drying and degassing the material located in the upper part of the shaft and a device for emitting heat for gasifying the material in the lower part of the shaft, at the bottom of the shaft a discharge for the ashes is provided.
  • a device is known for example from DE-PS 26 54 o41.
  • this device is designed in such a way that a feed for the gasification agent to be added to the degassed material for its gasification is arranged at such a distance above the passage located at the lower end of the shaft in the lower part of the shaft that the gasification means reach the degassed material at the beginning of the gasification phase and that the gasification space is separated from the downstream space by a passage narrowing in cross section for the passage of the non-combustible residues remaining after the gasification and that a deduction for the combustion-- -gas is arranged.
  • the passage is advantageously designed as an annular or longitudinal gap (claim 13).
  • the flow rate for gasification agents in the supply can be adjusted by a controller which is controlled as a function of the reaction temperature in the ember bed (claim 14).
  • the ember bed is supported by a conically shaped discharge device, which is arranged centrally in the shaft at the ash discharge of the shaft furnace.
  • the discharge device is rotatably mounted and cooled to prevent material overheating.
  • At the bottom of the discharge device there is a discharge gap as a passage formed, the gap width is dimensioned depending on the lumpiness of the good that forms in the ember bed and on the required good throughput.
  • the gap width is determined so that the residence time of the material to be gasified in the ember bed is sufficient to largely gasify the material before it is discharged from the ember bed.
  • the conical shape of the discharge device supports even material transport to the discharge gap.
  • the discharge can be regulated by turning the discharge device.
  • a fuel gas line is connected to the ash discharge of the shaft furnace.
  • the gas formed in the bulk material layer is thus removed directly from the ember bed formed in the shaft furnace.
  • the fuel gas contains only a small amount of oil and tar. It flows via the fuel gas line, preferably into a recuperative heat exchanger, which serves to preheat the material to be gasified in the shaft furnace (claim 151.
  • the gasification agent flowing into the bulk material layer is preferably used to cool the discharge device (claim 16).
  • the supply of the gasification agent expediently runs through the discharge device and ends centrally in the shaft (claim 17).
  • a largely homogeneous reaction zone in the shaft furnace to produce the fuel gas is ergasungsffens in connection with the central supply of the V achieved in that the discharge gap is formed as an annular gap between the lower edge of the discharge and the shaft furnace wall (claim 18:).
  • the gasification agent then flows through the reaction zone of the shaft furnace from the inside to the outside.
  • the discharge of the largely gasified material through the conical discharge device is influenced by the angle of inclination of the conical surface.
  • the angle of inclination between the base surface of the discharge device and the conical surface should not exceed 30 degrees and is preferably 20 degrees (claim 19).
  • guide ribs are attached to the cone surface facing the ember bed (claim 2o). When the discharge device rotates, the material in the ember bed is guided from the guide ribs to the discharge gap.
  • One or more blades reaching to the bottom of the shaft furnace are also fastened to the discharge device, which forcibly promote ashes collecting on the bottom of the shaft furnace when the discharge device rotates (claim 21).
  • the fuel gas flowing out of the ember bed is drawn off via the afterglowing ash for subsequent reaction with the remaining carbon.
  • the bulk material layer above the mouth of the feed for the gasification agent has such a height that the flow resistance of the bulk material layer above the feeder is greater than the flow resistance in the feed for the gasification agent (claim 2 2 ).
  • This is particularly advantageous when air is introduced as the gasification agent into the bulk material layer by generating a negative pressure at the mouth of the feed.
  • the higher flow resistance in the bulk material layer above the mouth then prevents the ingress of secondary air through the bulk material layer into the reaction zone even if the shaft furnace is open to the atmosphere for the task of material to be gasified.
  • the feed for the gasification agent has a flow controller that is controlled in operative connection with the temperature in the ember bed (claim 23).
  • the discharge device in the shaft furnace is preferably arranged interchangeably (claim 24).
  • discharge devices specially adapted to the material properties can also be used.
  • the alternative procedure is advantageously carried out by means of a device with a shaft furnace which has a device for emitting heat for gasifying the material located in the shaft, a discharge for the ash being provided at the bottom of the shaft furnace.
  • a closure flap is expediently provided below the feed.
  • the passage is advantageously designed as an annular or longitudinal gap
  • exhaust gas ducts are connected to the shaft, which in their Course surround the outer wall of the first chamber (claim. 27).
  • the intended gasification agents are supplied in cocurrent to the material to be gasified right at the beginning of the gasification process. This enables dosing according to the composition of the gases generated during gasification and the solid, flammable substances that pass through the gasification chamber. It is thus possible to continuously adapt to the constantly changing circumstances by modulating it.
  • the separation of the drying and degassing zone (first chamber) from the gasification zone (second chamber or shaft) creates two temperature ranges. Temperatures in the drying and degassing zone are up to a maximum of 500 ° C , in the gasification zone the temperatures are around 800 ° C (possibly up to 1000 ° C), i.e. only the gasification zone is to be made from temperature-resistant materials for the production of the first Chamber, on the other hand, requires simple, commercially available materials.
  • a preferred embodiment of the device with a shaft furnace according to the invention is that the first chamber intended for pre-treatment of the waste by drying and degassing is formed as compared to the horizontal, inclined opposite rotary drum with a gastight lock system at the loading s chic kung end, the other end of the Upper part of the shaft forming the gasification chamber opens, so that the material subjected to the heat treatment after it has been discharged from the rotary drum into the furnace shaft (claim 28).
  • the device with a shaft furnace is used to implement the alternative solution, the substantial volume reduction takes place in the rotary drum. It is also advantageous that coke is predominantly fed to the shaft furnace, thereby achieving a bed which is much more gas-permeable than normal waste, so that the gasifying agents added in cocurrent at the entrance to the shaft lead to a uniform and complete gasification process.
  • the waste from organic substances is fed into a shaft furnace 4 via a filling lock 1, which is arranged on a nozzle 2.
  • the waste is heated to about 55 0 ° C and thereby dried and degassed.
  • the drying and degassing zone can be heated.
  • This can either directly by arrangement of burners, of which only one is shown in the drawing, or may be done by the fuel gas discharged via the discharge line 11 is guided via the line path 3 that surrounds the drying and E ntgasungszone.
  • a burner 8 for direct heating can be arranged at the upper entrance to the shaft furnace 4. If necessary, both types of heating can therefore be used at the same time.
  • both types of heating can therefore be used at the same time.
  • the gasification chamber 6 adjoins the drying and degassing chamber; it is separated from the space adjoining it downwards in the shaft of the shaft furnace 4 by one or more lock elements 7.
  • a feed line 5 for the gasification agent to be added opens into the upper part of the gasification chamber 6.
  • a part of the derivative 11 can be used as the gasifying agent withdrawn fuel gas can be used.
  • the lock elements 7 have a closed upper side opposite the gasification chamber 6 and are mounted on a shaft or axle which, when they move, releases through openings designed as a longitudinal gap for discharging the solid and gaseous products from the gasification chamber 6 into the space below.
  • the exhaust gas line 11 opens below the lock elements 7 for the fuel gas which arises during the gasification and enters the space below the gasification space 6.
  • closure flap 10 The non-combustible constituents entering the space below the gasification space 6 are initially stored on a closure flap 10.
  • the arrangement of a closure flap has the advantage that it facilitates the complete further transfer of the ash formed during the gasification in accordance with the respective waste to the ash discharge 12.
  • FIG. 2 shows a shaft furnace 4, the organic material to be gasified, in particular organic waste through a funnel-shaped aterialaufgabe M can be fed.
  • a screw conveyor 13 transports the material to the good entrance 14 of the shaft furnace.
  • a bulk material layer 15 is formed from the material brought in.
  • the material moves down under the influence of gravity. It is located in the upper area of the shaft furnace in a preheating zone A heated by a recuperative heat exchanger 16.
  • the heat exchanger 16 is formed in the simplest manner by a double-walled tube delimiting the upper part of the shaft furnace, the cavity of which is flowed through by the fuel gas generated in the shaft furnace as a heating medium in counterflow to the direction of flow of the material in the shaft furnace.
  • the material to be gasified is dried by heat exchange with the fuel gas and heated up to approx. 200 ° C.
  • a rotatably mounted discharge device 17 is inserted into the shaft furnace 4 from below, which supports a glow bed 18 formed in the lower region of the bulk material layer 15.
  • the discharge device 17 is arranged centrally in the shaft and tapers conically towards the bulk material layer 15.
  • a discharge gap 19 is provided at the lower edge of the cone, the gap width of which is determined as a function of the lump size of the material forming in the ember bed 18 and of the required throughput of the material.
  • a gap between the edge of the cone and the shaft furnace wall of about 3 to 5 mm has proven to be advantageous.
  • gasifying fine-grained material at least 10% by weight of coarse material is added.
  • the size of the coarse material is selected so that bridging in the shaft is avoided.
  • a sieve-like structure is formed, so that only sufficiently small material particles, which are largely degassed, are discharged through the discharge gap 19.
  • a feed 21 is guided for gasifying agent, the layer of material above the ember bed 18 in the S chütt- 15 opens.
  • the gasification medium flowing through the discharge device 17 acts as a coolant and prevents the material from overheating. At the same time, the gasification agent warms up before entering the bulk material layer.
  • a cover 22 at the end of the feed 21 prevents bulk material from entering the feed line.
  • Discharge device 17 and feed 21 form a unit. Via the feed 21, the gasification agent is introduced into a zone designated 23 in the drawing in the bulk layer.
  • the material to be gasified has a temperature of about 200 ° C. in this zone after heat exchange with the fuel gas.
  • the gasification agent flows together with water vapor formed during drying of the material to be gasified and with the other gases formed in the protective material layer in the direction of flow of the material in a reaction zone B through the bulk material layer and with the formation of fuel gas through the ember bed.
  • a fuel gas line 24 which discharges the fuel gas is connected to the ash discharge 25 of the shaft furnace.
  • the fuel gas is in the Exemplary embodiment of a suction train, not shown in the drawing, subtracted from the ember bed. It flows through the heat exchanger 16 and is cooled there, giving off heat to the bulk material layer.
  • the maximum temperature in the ember bed 18 is preferably set to a temperature in the temperature range between 900 to 1000 ° C.
  • a temperature sensor 26 inserted into the bulk material layer measures a reference temperature in the shaft furnace above the embers bed 18, which changes analogously with the reaction temperature in the embers bed.
  • the temperature sensor 26 is in operative connection with a flow controller 27 which is used in the exemplary embodiment in the feed 21 for the gasification agent.
  • the flow of the gasification agent in the feed 21 can also be regulated in another way, for example by changing the suction pressure in the fuel gas line 24 or in combination with flow controller 27 and setting the vacuum at the ash discharge 25.
  • the The supply of gasification agent is throttled, the flow of air or oxygen is increased when the temperature drops.
  • the temperature of the ember bed can also be regulated by the composition of the gasifying agent. With the metered addition of air, oxygen, water vapor or carbon dioxide is a safe and, as a result of the direct supply of the gasifying agent in the bulk layer Above the embers bed, a rapidly reacting control of the gasification process was also achieved.
  • the discharge device 17 has cone surfaces 28 which, in the exemplary embodiment, have an inclination angle of 20 degrees, indicated in the drawing by reference numeral 29, relative to the base surface of the cone. It has been found in the case of gasification of fine material that, with such an inclination of the conical surfaces, the good-looking sport and the discharge of the good from the ember bed take place evenly without undesired compression of the material and at all points of the discharge gap.
  • the discharge device is arranged step by step by means of a drive 31.
  • the gasified material falls through the discharge gap 19 onto an ash bed 32 which forms on the bottom of the shaft furnace below the discharge device 17.
  • the fuel gas flowing out of the ember bed is passed over the ash bed 32 for the subsequent reaction of the remaining carbon and flows to the ash discharge 25.
  • Shovels 33 attached to the discharge device 17, which reach to the bottom of the shaft furnace, also transport the ash to the ash discharge when the discharge device 17 is rotated 25th
  • the shaft furnace which is designed in the same way as the shaft furnace described except for the material feed with a screw conveyor, the shaft was left open to simplify the material supply.
  • the height of the bulk material layer in the shaft furnace was dimensioned such that the flow resistance of the bulk material layer above the mouth of the gasification agent feed was greater than the flow resistance in the feeder.
  • the feed was open to the atmosphere. As a gasifying agent of the shaft furnace was sucked air into the S chüttgut für.
  • Another shaft furnace with a diameter of 400 mm and a height of 1.5 m was used to gasify sawdust, which was also introduced into the shaft furnace mixed with wooden parts.
  • the wooden parts had different sizes up to the size of logs of 150 mm in length.
  • the reaction zone of this shaft furnace was 450 mm long, the maximum temperature in the G lutbett was 900 to 1000 ° C.
  • the discharge device also made a full revolution step by step 1 to 2 times per hour. The cycle time was about 4 minutes. With a throughput of 30 to 40 kg of material to be gasified per hour, about 100 m 3 of fuel gas were generated per hour.
  • the shaft furnace has also been operated with the following waste materials successfully: sawdust, H obels fondne, cocoa shells, shredded bark, chopped straw, geshredderter domestic waste, pelletized domestic waste, algae.
  • the gasification process can be optimally adjusted by controlling the supply of gasification agent and regulating the crop discharge.
  • the cone shape and gap width of the discharge device and the reaction zone are adapted for different materials.
  • materials of the most varied structure and different gasification behavior can preferably be input by simply replacing the discharge device in order to generate fuel gas.
  • the waste first enters the rotary drum 34 via the filling lock 1, which is arranged at one end of a rotating drum 34 which is inclined with respect to the horizontal.
  • the filling lock 1 can be locked gas-tight .
  • the waste is heated to about 550 ° C and dried and degassed.
  • the rotary drum 34 is heated for this purpose, either directly by the arrangement of one or more burners 8, of which only one is shown in the drawing, or also in that the exhaust pipe 11 connected to the shaft furnace 4 below the gasification chamber 6 for the
  • the flammable gases produced during the gasification are guided in such a way that their course with the section part 3 surrounds the rotary drum 34 so that the outer wall of the rotary drum 34 also forms an inner wall of the section 3 of the exhaust pipe 11. If it is appropriate, both types of heating can be used at the same time.
  • the rotary drum 34 is connected to the upper part of the shaft furnace 4 via an intermediate chamber 35 in such a way that the material introduced into the rotary drum 34 is passed on into the shaft of the shaft furnace 4 after drying and degassing.
  • the material which has been dried and degassed in the rotary drum 34 is therefore first passed further into the intermediate chamber 35 which can be closed in a gas-tight manner by means of locks 36 and 37 and which overlaps the upper part of the shaft of a shaft furnace 4.
  • the upper part of the shaft furnace 4 is covered by a vibrating screen 38.
  • the remaining non-combustible waste components such as metal bodies, accessed via the R üttelsieb 38 in a printer connected to the intermediate chamber 35 and by means of the lock 37 gas-tightly closable shaft 39 and can be removed from there.
  • the additions required for binding pollutants which can be formed by the waste during the heat treatment become the one in this embodiment direction added according to the invention through the lock 36 provided on the intermediate chamber.
  • the upper part of the shaft furnace 4 forms the gasification chamber 6, which can be heated by means of a burner 9, at the upper end of which a feed line 5 opens for the gasification agents to be added.
  • the gasification space 6, as can be seen from FIG. 3, is separated from the space adjoining at the bottom by a constriction formed as an annular gap.
  • a tubular part 40 protrudes into the shaft of the shaft furnace 4 with a part 41, which is conically widening at the end projecting into the shaft.
  • the annular gap is formed by the base of the conical part 41 and the adjacent wall of the furnace shaft.
  • the tubular part 40 can be arranged rotatably about its longitudinal axis, in which case, as not shown in the drawing, it can be expedient to arrange stirring arms projecting laterally into the shaft, by means of which a loosening of the material to be gasified is achieved during the rotary movement .
EP81110618A 1980-12-27 1981-12-19 Procédé et installation pour la production continue de gaz combustible à partir de déchets organiques Withdrawn EP0055440A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DE19803049251 DE3049251A1 (de) 1980-12-27 1980-12-27 Verfahren und einrichtung zum vergasen von abfaellen aus organischen stoffen
DE3049251 1980-12-27
DE3112975 1981-04-01
DE19813112975 DE3112975A1 (de) 1981-04-01 1981-04-01 Verfahren zur kontinuierlichen erzeugung von brenngas und schachtofen zur durchfuehrung des verfahrens

Publications (1)

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EP0055440A1 true EP0055440A1 (fr) 1982-07-07

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EP (1) EP0055440A1 (fr)
KR (1) KR830008107A (fr)
DD (1) DD202176A5 (fr)
DK (1) DK577381A (fr)
FI (1) FI814066L (fr)
NO (1) NO814387L (fr)

Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3332913A1 (de) * 1983-06-03 1984-12-13 Chemische Fabrik Uetikon, Uetikon Verfahren zur erzeugung schadstoffarmer brenn- bzw. abgase und einrichtung sowie presslinge zur durchfuehrung des verfahrens
EP0130580A2 (fr) * 1983-07-02 1985-01-09 Forschungszentrum Jülich Gmbh Procédé pour gazéifier des déchets liquides contenant des composants organiques et four à cuve pour la mise en oeuvre du procédé
EP0152912A2 (fr) * 1984-02-22 1985-08-28 Kraftwerk Union-Umwelttechnik GmbH Procédé pour la production de gaz combustibles à partir de déchets
JPS62501637A (ja) * 1985-02-05 1987-07-02 エ−ブリ−　インタ−ナシヨナル　コ−ポレイシヨン 合成フェイスストック及びライナ
EP0532901A1 (fr) * 1991-09-18 1993-03-24 SAS GINO TOMADINI & C. Méthode et installation pour gazéifier des combustibles solides contenant des matériaux fusibles non-combustibles
EP0609802A1 (fr) * 1993-02-02 1994-08-10 JUCH, Helmut Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides
FR2792926A1 (fr) * 1999-04-30 2000-11-03 Air Liquide Procede pour la production d'un gaz de synthese a debit regule dans une unite de traitement de dechets
CN1818477B (zh) * 2006-03-03 2010-05-12 孙吉章 双向鼓风有机燃料炉膛二次燃烧节能炉
CN111043604A (zh) * 2019-12-26 2020-04-21 云南净美环保科技有限公司 一种小微型生活垃圾气化炉
CN117588758A (zh) * 2024-01-18 2024-02-23 江苏华炎炳麟科技有限公司 一种可燃固废气化焚烧装置

Families Citing this family (2)

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DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
WO2008103831A1 (fr) * 2007-02-21 2008-08-28 Energy & Environmental Research Center Foundation Système de gazéification à cocourant thermiquement stable et procédés associés

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DE592608C (de) * 1932-02-14 1934-02-10 Humboldt Deutzmotoren A G Gaserzeuger fuer Reishuelsen und aehnliche pflanzliche Abfallstoffe
DE688014C (fr) * 1937-11-28 1940-02-10 Kloeckner Humboldt Deutz Akt G
US2204902A (en) * 1937-07-09 1940-06-18 John U Mcdonald Process for producing gas
US3746521A (en) * 1971-03-15 1973-07-17 E Giddings Gasification method and apparatus
DE2432504A1 (de) * 1974-07-04 1976-01-15 Karl Dipl Ing Kiener Verfahren und vorrichtung zum herstellen von brenngas aus abfallstoffen
DE2654041B1 (de) * 1976-11-29 1978-03-16 Kernformschungsanlage Juelich Einrichtung und Verfahren zur Verbrennung von Abfallstoffen
DE2734973A1 (de) * 1977-08-03 1979-02-08 Kernforschungsanlage Juelich Verfahren und verbrennungsofen zum verbrennen von abfaellen
US4142867A (en) * 1974-07-04 1979-03-06 Karl Kiener Apparatus for the production of combustible gas
EP0012307A2 (fr) * 1978-12-07 1980-06-25 Saarberg-Fernwärme GmbH Grille rotative pour un réacteur à gazéification et/ou à combustion
WO1981000112A1 (fr) * 1979-07-05 1981-01-22 Kiener Karl Procede et installation pour la gazeification de combustibles en morceaux
EP0029795A1 (fr) * 1979-11-16 1981-06-03 ENTREPRISE GENERALE DE CHAUFFAGE INDUSTRIEL PILLARD. Société anonyme dite: Gazéificateur de combustibles solides à lit fixe et à tirage inversé

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BE457333A (fr) *
DE592608C (de) * 1932-02-14 1934-02-10 Humboldt Deutzmotoren A G Gaserzeuger fuer Reishuelsen und aehnliche pflanzliche Abfallstoffe
US2204902A (en) * 1937-07-09 1940-06-18 John U Mcdonald Process for producing gas
DE688014C (fr) * 1937-11-28 1940-02-10 Kloeckner Humboldt Deutz Akt G
US3746521A (en) * 1971-03-15 1973-07-17 E Giddings Gasification method and apparatus
US4142867A (en) * 1974-07-04 1979-03-06 Karl Kiener Apparatus for the production of combustible gas
DE2432504A1 (de) * 1974-07-04 1976-01-15 Karl Dipl Ing Kiener Verfahren und vorrichtung zum herstellen von brenngas aus abfallstoffen
DE2654041B1 (de) * 1976-11-29 1978-03-16 Kernformschungsanlage Juelich Einrichtung und Verfahren zur Verbrennung von Abfallstoffen
DE2734973A1 (de) * 1977-08-03 1979-02-08 Kernforschungsanlage Juelich Verfahren und verbrennungsofen zum verbrennen von abfaellen
GB2002887A (en) * 1977-08-03 1979-02-28 Kernforschungsanlage Juelich Process and incinerator for burning refuse
EP0012307A2 (fr) * 1978-12-07 1980-06-25 Saarberg-Fernwärme GmbH Grille rotative pour un réacteur à gazéification et/ou à combustion
WO1981000112A1 (fr) * 1979-07-05 1981-01-22 Kiener Karl Procede et installation pour la gazeification de combustibles en morceaux
EP0029795A1 (fr) * 1979-11-16 1981-06-03 ENTREPRISE GENERALE DE CHAUFFAGE INDUSTRIEL PILLARD. Société anonyme dite: Gazéificateur de combustibles solides à lit fixe et à tirage inversé

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE3332913A1 (de) * 1983-06-03 1984-12-13 Chemische Fabrik Uetikon, Uetikon Verfahren zur erzeugung schadstoffarmer brenn- bzw. abgase und einrichtung sowie presslinge zur durchfuehrung des verfahrens
EP0130580A2 (fr) * 1983-07-02 1985-01-09 Forschungszentrum Jülich Gmbh Procédé pour gazéifier des déchets liquides contenant des composants organiques et four à cuve pour la mise en oeuvre du procédé
EP0130580A3 (en) * 1983-07-02 1985-12-18 Kernforschungsanlage Julich Gesellschaft Mit Beschrankter Haftung Process for gasifying waste liquids containing organic components, and shaft furnace for carrying out the process
EP0152912A2 (fr) * 1984-02-22 1985-08-28 Kraftwerk Union-Umwelttechnik GmbH Procédé pour la production de gaz combustibles à partir de déchets
EP0152912A3 (en) * 1984-02-22 1986-06-25 Kiener Pyrolyse Gesellschaft Fur Thermische Abfallverwertung Mbh Process for producing combustible gases from waste products
JPS62501637A (ja) * 1985-02-05 1987-07-02 エ−ブリ−　インタ−ナシヨナル　コ−ポレイシヨン 合成フェイスストック及びライナ
EP0532901A1 (fr) * 1991-09-18 1993-03-24 SAS GINO TOMADINI & C. Méthode et installation pour gazéifier des combustibles solides contenant des matériaux fusibles non-combustibles
EP0609802A1 (fr) * 1993-02-02 1994-08-10 JUCH, Helmut Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides
WO1994018287A1 (fr) * 1993-02-02 1994-08-18 Helmut Juch Degazeification et/ou gazeification en continu d'un combustible ou d'un dechet solide
FR2792926A1 (fr) * 1999-04-30 2000-11-03 Air Liquide Procede pour la production d'un gaz de synthese a debit regule dans une unite de traitement de dechets
CN1818477B (zh) * 2006-03-03 2010-05-12 孙吉章 双向鼓风有机燃料炉膛二次燃烧节能炉
CN111043604A (zh) * 2019-12-26 2020-04-21 云南净美环保科技有限公司 一种小微型生活垃圾气化炉
CN117588758A (zh) * 2024-01-18 2024-02-23 江苏华炎炳麟科技有限公司 一种可燃固废气化焚烧装置
CN117588758B (zh) * 2024-01-18 2024-04-05 江苏华炎炳麟科技有限公司 一种可燃固废气化焚烧装置

Also Published As

Publication number Publication date
NO814387L (no) 1982-06-28
DK577381A (da) 1982-06-28
DD202176A5 (de) 1983-08-31
KR830008107A (ko) 1983-11-09
FI814066L (fi) 1982-06-28

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