EP0609802A1 - Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides - Google Patents

Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides Download PDF

Info

Publication number
EP0609802A1
EP0609802A1 EP94101381A EP94101381A EP0609802A1 EP 0609802 A1 EP0609802 A1 EP 0609802A1 EP 94101381 A EP94101381 A EP 94101381A EP 94101381 A EP94101381 A EP 94101381A EP 0609802 A1 EP0609802 A1 EP 0609802A1
Authority
EP
European Patent Office
Prior art keywords
gaseous
heat
gasification
helical
reactor
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Withdrawn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
EP94101381A
Other languages
German (de)
English (en)
Inventor
Helmut Juch
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.)
Individual
Original Assignee
Individual
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Individual filed Critical Individual
Publication of EP0609802A1 publication Critical patent/EP0609802A1/fr
Withdrawn legal-status Critical Current

Links

Images

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
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/80—Other features with arrangements for preheating the blast or the water vapour
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0903—Feed preparation
    • C10J2300/0906—Physical processes, e.g. shredding, comminuting, chopping, sorting
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F21/00—Constructions of heat-exchange apparatus characterised by the selection of particular materials
    • F28F21/08—Constructions of heat-exchange apparatus characterised by the selection of particular materials of metal
    • F28F21/081—Heat exchange elements made from metals or metal alloys
    • F28F21/082—Heat exchange elements made from metals or metal alloys from steel or ferrous alloys
    • F28F21/083—Heat exchange elements made from metals or metal alloys from steel or ferrous alloys from stainless steel

Definitions

  • the invention relates to the degassing and gasification of solid carbon-containing fuels and waste materials and an apparatus suitable for this, which meets the various ecological and operating conditions, for the continuous provision of a gaseous secondary fuel.
  • the invention relates to a process for the continuous, at least partial conversion of a solid, lumpy fuel or combustible waste material into a gaseous fuel by presorting, processing, at least partially degassing and / or at least partially gasifying in a vertical-axis shaft-like reactor, the starting material being in the form a feed column that slides down, successively a preheating and drying zone, a degassing zone, an oxidation zone and a reduction zone passes through, the preheated gaseous gasification agent is injected centrally into the lower part of the interior of the feed column and the gaseous and vaporous reaction products produced by degassing and gasification, which finally form the desired gaseous fuel, are passed downwards in a direct current to the feed column, diverted upwards and redirected and on the outside of the reactor wall, in a vertical direction, countercurrently to the feed column.
  • the invention further relates to a device for carrying out the method of at least partial degassing and / or at least partial gasification of a pre-sorted, prepared solid particulate fuel or combustible waste material, the device comprising a vertical-axis shaft-like reactor with a gas-tight charging device and gas-tight ash discharge or slag discharge device , further consists of an introduction of the gaseous gasification agent and a discharge of the gaseous fuel to be produced, as well as of heat exchangers, in such a way that an at least partially provided with a highly refractory lining reactor shaft and a downwardly narrowing narrowing refractory ceramic stove, the underside of which with a Grate with a variable passage cross-section, vertically displaceable, rotatable ceramic counterpart is lockable, furthermore a triple cylindrical jacket s and how a freely movable reactor shaft suspension is provided.
  • grate serves as the closing organ - based on the firing system - which causes the ashes to fall through or the slag to run off or, if necessary, to remove the high-carbon components (coke, charcoal) that are not to be gasified.
  • Numerous grate constructions, including rotary grates, have become known, which were mostly made of metallic materials and could not be fully satisfied due to limited heat resistance and insufficient high-temperature corrosion resistance.
  • the problem has been solved in a good approximation by a rotatable, conical ceramic body.
  • the throughput of the primary fuel can be regulated within wide limits by means of the annular gap formed by this body together with the stove and intended for the discharge.
  • Executed gas generators for wood as an insert usually work in direct current with descending gasification and use the jacket for the limited preheating of the air usually used as a gasifying agent. Additional air preheating devices in the area of the range have also been proposed, or attempts have been made to keep the latter below tolerable temperatures by means of special cooling air.
  • Central air supply pipes for introducing the gasification agent into the inside of the charging column from above, from the side or from below have already been implemented. However, their probation usually failed due to an inadmissible hindrance to the downward movement of the feed and led to blockages, channel formation or the notorious "hanging" of the latter.
  • An effective one Air preheating in the central air supply pipe has been attempted only in exceptional cases and generally only related to a partial air flow.
  • the discharge organs were often poorly designed and hardly allowed the behavior of the loading column to be influenced in the sense of achieving optimal mechanical and thermodynamic conditions.
  • the above-mentioned methods and devices were therefore unable to replace the traditional chamber furnaces of the gas works and coking plants and the traditional coal kiln.
  • the invention has for its object to provide a method and an apparatus for the continuous, at least partial degassing and / or gasification of a lumpy primary carbon-containing solid energy source in the form of a fuel and / or combustible waste material in a shaft-like reactor, which is as simple as possible in process control and plant can be used universally and directly, without additional cleaning, dedusting and detoxification devices and catalytic converter batteries supply a gaseous fuel which is as pure as possible and which can be used directly for motor, chemical, metallurgical or heating purposes.
  • the method should have the highest possible efficiency and make maximum use of the exergy content of the primary energy source while avoiding the usual losses.
  • the device is said to be particularly suitable for processing organic waste such as rubbish, garbage, sewage sludge, wood and paper waste, etc. and to enable rapid adaptation to the various input materials without loss of time or business interruption.
  • the gaseous gasification agent is first guided and heated at high speed in a helical, downward movement in countercurrent to a corresponding upward helical movement of the gaseous fuel produced within the jacket section of the shaft-like reactor, also in a helical motion through the interior of a stove body with a high heat capacity and further heated, deflected vertically upwards at the lower end of the reactor and after passing through an artificially extended distance while simultaneously heating further inside a central body protruding from below into the lower part of the charging column the latter is injected, and that the gaseous fuel produced leaving the charging column is expelled downward through an annular passage is reduced and conducted at high speed in countercurrent to the gasification agent and cooled, and that the high heat capacity of the hearth body is used to bridge interruptions in operation and to carry out intermittent processes which require a certain temperature program and are superimposed on the continuous process.
  • the object is further achieved in that in the above-mentioned device for supplying the gaseous gasification agent between its introduction and its discharge into the charging column, a series of heat exchangers, which are arranged in succession and are arranged locally in a falling direction and which consist essentially of cylindrical or conical basic shapes, consist of increasing temperature is provided, and that a ceramic central body for guiding and injecting the gaseous gasification agent from below into the lower part of the charging column is provided, which projects comparatively deep into the latter.
  • 1 is a basic schematic representation of the material flows of the process (flow diagram). It is a specifically organized treatment and processing of essentially carbon-containing primary energy sources with the greatest possible consideration of ecological and economic conditions (environmental conditions).
  • the process consists of separating out, reading out and separating out the resulting starting materials, branching off non-combustible materials, preparing and mixing the real primary energy sources pre-concentrated in this way in one Intermediate product, optionally comminuting or vice versa compacting for the production of a lumpy feed suitable for further processing for a thermal reactor and degassing or gasifying the latter into a gaseous secondary fuel.
  • 2 shows a schematic longitudinal section (vertical section) through the basic structure of the device with the flows of the gaseous media (in perspective).
  • the arrow indicated above and pointing vertically downward represents the task of the feed in the form of lumpy fuel.
  • 2 is the introduction of the gaseous gasifying agent (in the present case preferably atmospheric air) into the shaft-like reactor 3 (essentially a cylindrical wall), also abbreviated as reactor shaft.
  • the flow of the gasification agent is shown throughout as a solid solid line, that of the gaseous secondary fuel generated as a broken dash-dotted line.
  • 4 is the outer jacket of the shaft-like reactor, 5 the discharge of the gaseous fuel to be generated.
  • 6 represents the helical guidance (trajectory) of the gaseous gasification agent in the jacket section of the reactor.
  • FIG. 7 is the corresponding, locally interposed helical guidance of the gaseous fuel in the jacket section, which takes place in counterflow to FIG. 6. It is a matter of heat transfer along a helical heat exchanger, the flow of the gasification agent being heated (preheating) and that of the gaseous fuel being cooled becomes.
  • the stove or specifically the refractory ceramic stove body is called.
  • 9 is the helical guidance of the gasification agent in the hearth body 8 for the purpose of further heating.
  • 10 represents a full cone as a counterpart to the stove, stove top and grate, which protrudes from below into the charging column. In the present case, the full cone 10 is rotatable about its axis and vertically displaceable in its longitudinal direction.
  • 11 is the vertically upward feed of the gasification agent into the full cone 10
  • 12 the helical guide and the arrow 13 the vertical discharge of the gasification agent from the full cone (injection into the interior of the feed).
  • 14 represents the gaseous fuel that is generated in the feed and flows vertically downwards. The latter is deflected and directed vertically upwards between the cooker 8 and the outer jacket 4.
  • the annular passage 15 forming the grate, the cross section of which is adjustable.
  • 16 is the discharge of solid and / or liquid reaction products which, depending on the management, consists of ash, slag and solid distillation residue (coke, semi-coke, charcoal, partially degassed carbon-containing product).
  • FIG. 3 shows a simplified longitudinal section (vertical section) through the device.
  • the reference numerals 1, 2, 3, 4, 5, 8, 10, 11, 13 and 16 correspond exactly to those in FIG. 2.
  • a feed device with gas-tight feed locks 51 in the form of slides lying in horizontal planes, opening or closing linearly or rotatably.
  • the feed slides down by gravity vertically within the circular cross-section of the cylindrical wall of the shaft-like reactor 3.
  • a heat exchanger consisting of a helical channel 21 for the gasifying agent and a channel 22 for the gaseous fuel.
  • the channels 21 and 22 in helical form are nested one inside the other in the manner of a two-start thread and the gaseous media flow through them in the opposite direction.
  • the flow of the gasification agent is directed downwards, that of the gaseous fuel upwards.
  • the full lines 6 refer to the gasification agent, the broken lines to the gaseous fuel.
  • the lower part of the reactor shaft 3 has a refractory lining 17, while the outer jacket 4 is provided with a heat-insulating layer 28 over its entire length.
  • the refractory hearth body 8 has a double-conical concave inner profile 18 with narrowing and is equipped along the latter with at least one conical-helical channel 25 for the gasifying agent in the form of a downward spiral.
  • This coil serves at the same time for further preheating of the gaseous gasification agent and for cooling the hottest zone of the stove body 8.
  • the latter is provided with a heat-insulating layer 29 on all sides on its outer boundary surface in order to reduce heat losses.
  • the gasification agent (upward feed 11) arrives via a flexible connector (not specified in any more detail) into the feed pipe 19 carrying the full cone 10 as a counterpart.
  • the latter is firmly connected and serves as a carrier and guide for the full cone 10 Coaxial shaft 20 provided in vertical bearings.
  • the full cone 10 which is provided on its lower end face with a heat-insulating layer 30, is provided in its interior with at least one conical-helical channel 23 (helical shape) for the gasification agent, which is located at the cone tip in the outlet opening 24 (vertical discharge 13 and injection into the feed ) ends.
  • the gaseous fuel 14 (dash-dotted arrow) generated in the feed, flowing vertically downward, passes through the ring-shaped, rust-forming passage 15 between the cooker 8 and its counterpart (in the present case full cone 10), undergoes a deflection 26 below the cooker / grate section and arrives in the hollow cylindrical space 27 between the cooker 8 and the outer jacket 4, where it is guided vertically upwards.
  • the gaseous fuel is introduced into the helical channel 22 in the jacket section of the reactor.
  • the solid and liquid reaction products (ash, slag, distillation residues) fall vertically downward (indicated by the vertical dashed arrow discharge 16) into the container 31 provided for this.
  • Fig. 4 relates to a schematic vertical section through the jacket section of the reactor shaft with a first embodiment of the heat exchanger.
  • the channels for the gaseous media, designed as helices, are nested one inside the other on the principle of a two-start thread. This takes place in the helical channel 21 for the gasification agent Flow perpendicular to the plane of the drawing towards the viewer, which is indicated by the profile of arrowhead 6 (ring with point).
  • the flow takes place perpendicular to the plane of the drawing away from the viewer, which is shown by the profile of the arrow end 7 (ring with cross, drawn in broken lines).
  • the gaseous media are thus guided in opposite directions (countercurrent principle), so that optimal heat transfer is ensured and the gaseous fuel produced leaves the reactor at the lowest possible temperature.
  • Average velocities of the gaseous media of approx. 3 m / s are aimed for. 28 is the heat-insulating layer of the outer jacket 4.
  • FIG. 5 shows a schematic vertical section through the jacket section of the reactor shaft with a second embodiment of the heat exchanger.
  • the channels for the gaseous media which are designed as helices, are put over one another on the principle of two radially arranged threads (external thread + internal thread).
  • the helical channel 21 for the gasification agent is axially offset by half the slope relative to the channel 22 for the gaseous fuel, in order to make the construction more favorable in terms of strength on the one hand and freedom from tension on the other hand.
  • FIG. 4 With regard to flows of the gaseous media (arrow tips 6 and arrow ends 7 in profile), the statements made under FIG. 4 apply. This is also the countercurrent principle.
  • the function of thermal insulation Insulating layer 28 goes without saying.
  • Fig. 6 relates to a perspective view of a first embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent.
  • 10 shows the full cone, which acts as a counterpart, stove top and grate and protrudes from below into the interior of the lowest part of the charging column.
  • the full cone 10 has cavities for guiding and further heating the gasification agent (usually air).
  • the gasification agent usually air
  • the cross section can also have a different shape, e.g. that have a hexagon or square etc.
  • the representation 34 is the inlet opening on the lower end face of the full cone 10
  • 24 is the outlet opening for the gasifying agent located opposite the cone tip.
  • the representation is deliberately chosen so that the full cone 10 appears transparent, while the channel 23 acts like a spiral made of solid material. This corresponds to the hollow shape required on the one hand in the production of the ceramic body and the necessary solid core on the other hand.
  • Fig. 7 shows a perspective view of a second embodiment of the full cone as a counterpart, stove top and grate with guidance of the gasification agent.
  • 10 represents the full cone, the functions of which are identical to those described in FIG. 6.
  • the only contiguous cavity for guiding the gasification agent here has the shape of a wavy channel 35 lying on a virtual conical surface and having a circular cross section.
  • 34 and 24 correspond to the reference numerals of FIG Fig. 6.
  • the representation of the full cone 10 as a hollow shape and the channel 35 as a solid core also corresponds to that of Fig. 6. The same applies to what has been said about channel cross sections.
  • Fig. 8 is a schematic longitudinal section of a pipe connection for circulating gas, also shown with a heat exchanger. At the edge of the left half of the figure, the contour of the shaft-like reactor is indicated in thin lines.
  • the reference numerals 3, 10, 18 and 27 correspond exactly to those in FIG. 3.
  • the dash-dotted arrow 36 means the circulation gas is withdrawn from the lower part of the charging column (in the present case in the lower part of the oven space).
  • the recycle gas is used to heat the feed more effectively.
  • 37 represents the recycle gas return to the top of the feed column.
  • 38 is the corresponding pipeline for the recycle gas.
  • 39 is the required hot gas blower, which is designed for a temperature of at least 800 o C. It advantageously has a rotor made of highly refractory ceramic material with high heat resistance and high temperature corrosion resistance.
  • the pipeline 38 and the hot gas blower 39 are provided with a heat-insulating covering.
  • a counterflow heat exchanger 41 for circulating gas is additionally shown as an option. It consists of two chambers separated by a heat-conducting partition 44 and is used, if necessary, for further heating of the recycle gas 42 (dash-dotted arrow).
  • the heating gas 43 moves in countercurrent to the latter (dashed arrow).
  • the heating gas can be a specially provided fuel gas or a high-temperature exhaust gas.
  • the heat flow Q ⁇ is indicated by the arrow 45. This additional device can be used to increase the performance and efficiency of the entire system.
  • FIG. 9 shows a longitudinal section (vertical section) through an embodiment of the hearth / grate section with a fixed conical central body.
  • 3 is the actual shaft-like reactor (cylindrical wall, inside)
  • 4 is the outer jacket of the reactor.
  • the cooker 8 consists of two rotationally symmetrical, coaxially arranged ceramic parts.
  • the outer part has a cylindrical outer surface and a double-conical inner profile 18.
  • the inner part is cylindrical in the lower part and conical in the upper part and has a central channel for guiding the gasification agent. At the cone tip of this central body there is the vertically upward-pointing outlet opening 46 for the gasifying agent.
  • the hollow-cone-shaped ring body 47 delimited by an outer cone and an inner cylinder as a counterpart, stove top and grate.
  • the ring body 47 is rotatably and vertically displaceably mounted (not shown) and, together with the lower part of the outer part of the cooker 8, forms an annular passage 15 which forms the grate and through which the solid and liquid reaction products are discharged.
  • Both the outer part and the inner part (central body) of the cooker 8 preferably have a helical channel (helix) for the gasification agent similar to FIG. 3 (25 and 23) (not shown in this figure).
  • the shaft-like reactor 3 and its outer jacket 4 correspond exactly to the structure according to FIG. 9 and FIG. 3.
  • the hearth 8 here consists of two rotationally symmetrical, coaxially arranged ceramic parts, of which the outer part is a hollow cylinder.
  • the inner part is conical in the lower part, in the upper paraboloid and has a central channel with branches for guiding the gasification agent. Thanks to this stove construction, the cross section of the charging column is not radially inward but radially outward as it moves downward.
  • the plant was designed for the continuous gasification of waste wood.
  • the ceramic hearth body 8 consisted of a high-alumina fired ramming mass, in which there was a conical helical channel 25 (spiral) of 1.2 dm 2 circular cross-section and a total of 5 turns.
  • the cylindrical outer wall of the hearth body 8 was protected by a heat-insulating insulating layer 29 made of ceramic wool with a radial thickness of 50 mm.
  • the full cone 10 as a counterpart, stove top and grate had an opening angle of 60 o and a largest diameter of 620 mm.
  • the gas generator was also equipped with a gas-tight loading device consisting of a shaft-like structure with two loading locks 51 designed as slides. Carbon steel of approximately 10 mm thickness was used for all these parts. The same applies to the part of the container 31 adjoining the reactor for solid and liquid reaction products such as ash, slag and possibly distillation residues (charcoal, coke, semi-coke).
  • the actual shaft-like reactor 3 was only firmly connected to the outer jacket 4 in the uppermost part, so that it could extend freely in all directions.
  • the outer jacket 4, for its part, was supported by trusses and articulated levers on a three-legged frame made of strong steel profiles with feet.
  • Example 1 A plant for the continuous gasification of lumpy, organic waste such as plastic, composite material, old cardboard etc. was provided.
  • Cr / Ni steel of 14 mm thickness was used analogously to Example 1. Ceramic wool was also used for the insulating insulating layers 28, 29 and 30.
  • the helical Channels 21 and 22 were arranged according to FIG. 4, had a radial width of 500 mm and a height of 230 mm and consisted of 5 mm thick Cr / Ni steel sheet.
  • the stove body made of Al203 8 had a helical channel 25 of a total of 4 turns and a circular cross section of 3.8 dm2. The average speed of the gasification agent was approximately 15 m / s.
  • the full cone 10 mm had an aperture angle of 70 ° and a maximum diameter of the 880th It was made of Al203 and had a conical-wavy channel 35 of 1.55 dm2 circular cross-section. There were a total of 3 full trapezoidal waves. The speed of the gasification agent, based on normal conditions, was about 37 m / s in channel 35.
  • the full cone 10 was arranged to be movable in the same way and provided with corresponding drives, as was described under Example 1.
  • Example 1 is referred to as regards the feeding device and the discharge of the reaction products.
  • a sheet thickness of 14 mm for the carbon steel used was chosen.
  • the gas generator was supported or suspended in the frame as in Example 1.
  • Feed material primary fuel: lumpy organic waste
  • Primary fuel throughput 600 kg / h
  • Piece size of the insert 20 - 60 mm
  • Gas yield 3.5 m3 / kg use
  • Lower heating value of the gas (moist) 3600 kJ / Nm3
  • the plant was designed for the continuous gasification of compacted sewage sludge and similar waste materials originally produced in fine form.
  • the starting material was first air-dried and then further dewatered under high pressure and pressed into oval briquettes.
  • the basic structure of the gas generator corresponded to that of Example 1.
  • the outer jacket 4 and the casing of the cooker 8 exposed to high temperatures an austenitic, stabilized one was used Cr / Ni / Mo steel of 20 mm thickness is used.
  • the heat-insulating insulation layers 28, 29 and 30 were made of high alumina ceramic fiber for operating temperatures up to 1800 o C.
  • the helical channels 21 and 22 were shown in FIG. 5 arranged and passed as the intermediate wall 33 of Cr / Ni / Mo steel of 6 mm thickness. They had a radial width of 375 mm and an axial height of 750 mm.
  • the stove made of Al203 8 was assembled from several ring-segment-shaped sintered parts, which were interconnected by means of ceramic adhesive with a high elasticity with the interposition of thin Al203 layers of felt.
  • the hearth 8 was broken through by a helical channel 25 of a total of 3 turns with a circular cross section of 5.6 dm 2.
  • the average velocity of the gasification agent, based on the normal state, was approx. 25 m / s.
  • the full cone 10 mm had an opening angle of 65 ° and a maximum diameter of the 1300th It consisted of Al203 and had a conical-helical channel 23 with 2 1/2 turns of 2.8 dm2 circular cross-section analogous to Example 1.
  • the speed of the gasification agent, based on normal conditions, was about 50 m / s in channel 23.
  • the movement possibilities of the full cone 10 have already been described in Example 1.
  • Example 1 With regard to the additional construction elements, reference is made to Example 1.
  • the sheet thicknesses were generally chosen to be approximately 18 mm for the construction material carbon steel.
  • the rotor of the hot gas blower 39 was composed of a heat-resistant nickel-based superalloy for operating temperatures up to 950 o C. For even higher temperatures can be used, where appropriate, rotors made of ceramic material such as silicon nitride, silicon carbide or ceramic composite. Since the recycle gas removal 36 takes place in the ember bed of the charging column, the gas removed is largely free of tars, tar distillates, phenols, alcohols and acetic acid, so that serious high-temperature corrosion problems need not be expected. However, if the gas contains not negligible amounts of sulfur, it must be largely nickel-free, high-chrome materials are used.
  • the components of the reactor 3, the outer jacket 4, the casing of the Cookers 8 and the helical channels 21 and 22 were made from a ferritic, high-chromium iron base alloy with high oxidation, scale and corrosion resistance, doped with aluminum and silicon additives.
  • the load-bearing parts were made from 30 mm sheets, the heat exchangers from 10 mm thick ones.
  • the heat insulating layers 28, 29, 30 and 40 consisted of Al203 felt materials with a certain inherent strength.
  • the helical channels 21 and 22 were nested according to FIG. 4, arranged analogously to Example 2.
  • the cooker 8 according to FIG. 9 consisted of two parts, a peripheral part with a double-conical concave inner profile with narrowing and a cylindrical central part in the lower part and a fixed conical part in the upper part. Both parts were provided with helical channels (not shown in FIG. 9) for the gasification agent (analogous to reference numerals 25 and 23 in FIG. 3).
  • the channel in the peripheral part of the hearth 8 had a circular cross section of 20 dm 2 and had 5 1/2 turns.
  • the average velocity of the gasification agent in this channel was approx. 30 m / s.
  • the hearth in the central body had a circular cross section of 12 dm2 and had 4 1/2 turns.
  • part of the gas flow generated namely approx. 4 m3 / s, was removed from the hearth section in a manner similar to Example 3 (circulating gas extraction 36) and by means of a hot gas blower 39 injected via the countercurrent heat exchanger 41 as recycle gas 42 into the upper part of the feed column (recycle gas return 37).
  • the circulating gas 42 was additionally heated by the heating gas 43 via the heat-conducting partition 44 (heat flow Q ⁇ with reference numeral 45).
  • the pipeline 38 had a cross section of 40 dm 2, so that the average gas velocity, based on normal conditions, was 10 m / s.
  • Ferritic Cr / Al steel with a wall thickness of 12 mm was used for the pipeline 38 and the heat exchanger 41.
  • the insulating panel 40 had a thickness of 100 mm and was made of Al203 wool.
  • the rotor of the hot gas blower 39 consisted of a heat-resistant ferritic Cr / Al / Si / Fe alloy.
  • the additional construction elements were made from low-carbon steel sheet with a thickness of approx. 25 mm. Reference is made to the description under Example 1.
  • the plant was designed for the continuous degassing of lumpy hard coal.
  • the hard coal had a content of approx. 15 to 20% volatile components.
  • a strong gas with a comparatively high calorific value was produced.
  • the degassing was carried out at a maximum temperature in the oven portion of 550 o C.
  • an excess of oxygen was initially used, ie practically gasified, in order to bring the feed to the reaction temperature.
  • the oxygen supply was throttled so far that only the heat balance (heating of the feed, endothermic chemical reactions) was just balanced in the event of an oxygen deficit. This corresponded to about 10% of the amount of normal gasification air.
  • An austenitic Cr / Ni steel of 20 mm thickness was used for the sheet metal bodies of the reactor 3, the outer casing 4 and the casing of the hearth.
  • the heat-insulating layers 28, 29, 30 and 40 consisted of ceramic fiber mats.
  • the helical channels 21 and 22 were arranged as shown in FIG. 5 and, including the intermediate wall 33, were made of 6 mm thick Cr / Ni steel sheet. They had a radial width of 350 mm and an axial height of 475 mm.
  • the peripheral part of the cooker 8 consisted of several sintered full Al203 rings and had no channels.
  • the central body of the stove made of Al203 ramming mass was provided with a helical channel for the gasifying agent (not used in the present case only used in a very reduced amount), not shown in Fig. 10, of 4 dm2 circular cross section.
  • the average speed is approx. 20 m / s.
  • the inserted between the two oven parts of hollow cone-shaped ring body 50 (inner cone) had an opening angle of 45 o and consisted of sintered silicon carbide.
  • the gas generator was equipped with a device for circulating gas including heat exchanger according to FIG. 8 (reference numbers 36, 37, 38, 39, 40, 41, 42, 43, 44, 45).
  • a multiple of the gas flow generated namely approximately 2 m3 / s, was circulated and practically heated by the heating gas 43 to the reaction temperature of 550 ° C. via the heat exchanger 41.
  • the pipeline 38 had a cross section of 20 dm 2, the average gas velocity was 10 m / s.
  • a common Cr / Ni steel was used as the material.
  • Example 1 For the remaining construction elements, reference is made to Example 1. They consisted exclusively of ordinary soft carbon steel with a thickness of approx. 18 mm.
  • Feed material primary fuel: lumpy coal
  • Primary fuel throughput 3300 kg / h
  • Piece size of the insert 20-75 mm
  • Gas yield 0.9 m3 / kg use
  • Lower heating value of the gas (moist) 12000 kJ / Nm3
  • the invention is not restricted to the exemplary embodiments.
  • hard coal, lignite or wood is essentially used as the starting material and the process is carried out under a lack of oxygen in such a way that the degassing prevails and the gasification recedes and at optionally adjustable maximum temperatures of 500 to 1100 o C in addition to the high-quality gaseous fuel 5 from high calorific value as a further product, a high-carbon distillation residue 16 in the form of coke, semi-coke or charcoal is produced.
  • any carbon-containing fuel or waste material is used as the starting material, and the process is carried out with sufficient oxygen so that the gasification predominates and when the latter is carried out, a maximum temperature in the charging column of at least 1200 ° C. is set, all of which condensable higher carbon compounds such as tars, phenols, acetic acid, alcohols thermally decomposed, pyrolytically split and converted into flammable stable gases such as C0, H2 and CH4.
  • a carbon-containing fuel and predominantly a waste material which can contain Cl, F, Zn, Cd and / or Hg, as well as garbage, rubbish, sewage sludge in lumpy and / or briquetted or pelletized form or in as a starting material any other compact form, with or without a binder, and the gasification is carried out at a maximum temperature in the feed column of at least 1500 ° C. or at least above the vaporization temperature of said toxic heavy metals under reducing conditions, the heavy metal vapors being condensed and branched off or through in a receiver Surcharge chemically bound in the feed and discharged into the slag or ash.
  • part of the gaseous fuel generated is branched off 36 from the lower part of the charging column, optionally additionally heated with the addition of heat 45, and injected as circulating gas 42 into the upper part of the charging column for the purpose of heat transfer, 37; Heat balance continuously or intermittently H20 steam injected into the hottest zone of the ember bed of the charging column, the calorific value of the gaseous fuel to be generated is increased in extreme cases up to values of a strong gas.
  • the device for carrying out the method of at least partial degassing and / or at least partial gasification of a pre-sorted, processed solid particulate fuel or combustible waste material consists of a vertical-axis shaft-like reactor 3 with a gas-tight feed device 51 and gas-tight ash discharge or slag discharge device, and also an introduction 2 of the gaseous gasification agent and a discharge line 5 of the gaseous fuel to be produced as well as from heat exchangers, whereby a reactor shaft 3 provided at least partially with a high refractory lining 17 and a refractory ceramic cooker 8 with a narrowing downward constriction, the underside of which has a grate that can be changed as a grate Passage cross section 15 acting, vertically displaceable, rotatable ceramic counterpart is lockable, a triple cylindrical jacket 4 and a freely movable reactor shaft suspension is available, and for the supply of the gaseous gasification agent between its introduction 2 and its discharge 13 into the charging column a number of
  • the cooker 8 has a radially inward narrowing with a double-conical inner profile, the charging column in the cooker area filling the cross-section of a full circle with decreasing diameter at every level, and the ceramic central body simultaneously forms the rotatable and vertically displaceable counterpart a full cone 10 with at least one feed channel for the gaseous gasification agent.
  • the hearth 8 has a radially outward narrowing with a conical or paraboloid-shaped inner body, the charging column in the hearth area filling the cross-section of a circular ring with increasing inner diameter at every level, and the central body serving to guide the gaseous gasifying agent is also located Space is fixed and is part of the cooker 8, and the ceramic counterpart serving the end of the cooker has the shape of a hollow cone-shaped ring body with an outer cone 47 or an inner cone 50, is rotatable and vertically displaceable and has no channels.
  • the highly refractory ceramic stove body 8 is preferably equipped with cavities for guiding the gaseous gasification agent, which cavities represent at least one helical channel 25 on a virtual double cone surface or cylinder surface, the cross section of which is dimensioned such that the speed of the medium flowing through is at least 5 m / s.
  • the central body which serves, among other things, to guide the gaseous gasification agent, is advantageously provided with cavities in the form of at least one conical helical line 23 or at least one corrugated line 35 wound on a virtual conical surface for this purpose and is made of a ceramic material for good heat conduction high thermal conductivity and is clad on its lower end face to reduce heat loss with a heat-insulating layer 30.
  • the stove body 8 is structurally designed such that it has a high heat capacity and consists of a material of high specific heat such as high-carbon ramming mass, into which a reinforcement consisting of rings and radial spokes made of a material of high thermal conductivity (such as silicon carbide) For better radial heat conduction from the ember bed of the feed is embedded in the hearth body 8 and vice versa.
  • the device is generally designed in an advantageous manner in such a way that the jacket section 4 of the reactor shaft 3 is equipped with a heat-insulating layer 28 forming the outer skin and that between the outer jacket 4 and the actual reactor wall 3 there is a countercurrent heat exchanger consisting of helical elements for heat transfer from the generated gaseous fuel is on the gaseous gasifying agent, such that either arranged in a layer, nested, alternately from one and the other gaseous medium in the opposite direction through which flowed at a speed of at least 3 m / s helical channels 21; 22 are present or that corresponding helical channels 21; 22 are present, those for the gaseous gasification agent outside, those for the gaseous fuel generated are inside and separated by a heat-conducting intermediate jacket 33.

Landscapes

  • 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)
  • Gasification And Melting Of Waste (AREA)
EP94101381A 1993-02-02 1994-01-31 Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides Withdrawn EP0609802A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CH29693 1993-02-02
CH296/93 1993-02-02

Publications (1)

Publication Number Publication Date
EP0609802A1 true EP0609802A1 (fr) 1994-08-10

Family

ID=4183763

Family Applications (1)

Application Number Title Priority Date Filing Date
EP94101381A Withdrawn EP0609802A1 (fr) 1993-02-02 1994-01-31 Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides

Country Status (3)

Country Link
EP (1) EP0609802A1 (fr)
AU (1) AU5856494A (fr)
WO (1) WO1994018287A1 (fr)

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999055803A1 (fr) * 1998-04-28 1999-11-04 Bruno Berger Procede fonde sur la production d'energie a partir de dechets, utilise pour produire du courant, de l'eau et/ou de l'hydrogene et/ou du methanol a partir de biomasse et/ou de dechets organiques
US7000780B1 (en) 1999-08-03 2006-02-21 Harald Martin Method and device for drying, separating, classifying and decomposing recoverable waste products
US7147681B1 (en) 1999-08-03 2006-12-12 Harald Martin Method and device for removing recoverable waste products and non-recoverable waste products
DE202008017561U1 (de) 2008-11-20 2009-10-29 Eurotherm Technologies Ag Vorrichtung in Form eines Bewegt-Bett-Vergasers
DE202009010833U1 (de) 2009-08-11 2009-11-05 Eurotherm Technologies Ag Anordnung zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen
DE202009010832U1 (de) 2009-07-08 2010-01-28 Eurotherm Technologies Ag Anordnung zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen
DE202009010830U1 (de) 2009-02-05 2010-02-11 Eurotherm Technologies Ag Vorrichtung in Form eines Thermolysereaktors
CN101245261B (zh) * 2008-03-03 2010-09-01 戴太才 一种机械连续进料气化炉及所用的原料
ITTO20090328A1 (it) * 2009-04-27 2010-10-28 Pierluigi Martini Reattore autotermico cilindrico per la produzione di gas combustibile con sistema di entrata aria a flusso tangenziale
WO2015039640A1 (fr) 2013-09-20 2015-03-26 Recom Patent & License Gmbh Gazéifieur à 3 zones et procédé de fonctionnement d'un tel gazéifieur pour la transformation thermique de déchets et de résidus
DE202016106184U1 (de) 2016-11-04 2016-11-17 Hartwig Streitenberger Duplex-TEK-Mehrstufen-Vergaser
CN106701120A (zh) * 2016-12-29 2017-05-24 安徽虹源生物质有限公司 一种旋转式破拱、高料层上吸式生物质热解气化炭气联产装置及方法
DE102016121046A1 (de) 2016-11-04 2018-05-09 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Duplex-TEK-Mehrstufen-Vergaser
IT202100002540A1 (it) * 2021-02-05 2022-08-05 Agenzia Naz Per Le Nuove Tecnologie Lenergia E Lo Sviluppo Economico Sostenibile Enea Reattore di gassificazione a letto fisso equicorrente

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103952183A (zh) * 2014-03-25 2014-07-30 佛山市凯沃森环保科技有限公司 生物质燃气化设备
CN108753361B (zh) * 2018-08-29 2024-01-23 云南煤化集团工程技术有限公司 固定床熔渣气化炉布料器
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 (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE457257A (fr) *
DE624242C (de) * 1934-05-23 1936-01-16 Kromag A G Fuer Werkzeug Und M Gaserzeuger mit abwaerts gerichtetem Zug, insbesondere zur Erzeugung von Holzgas fuer Kraftfahrzeuge
FR2407256A1 (fr) * 1977-10-31 1979-05-25 Pps Polyvalent Patent Service Procede et dispositif de production de gaz de bois
FR2422712A1 (fr) * 1978-04-13 1979-11-09 Duvant Moteurs Perfectionnements aux gazogenes a tirage inverse
EP0055440A1 (fr) * 1980-12-27 1982-07-07 Forschungszentrum Jülich Gmbh Procédé et installation pour la production continue de gaz combustible à partir de déchets organiques
FR2505350A1 (fr) * 1981-05-08 1982-11-12 Pillard Chauffage Gazeificateurs de combustibles solides a lit fixe et a tirage inverse
FR2519017A1 (fr) * 1981-12-24 1983-07-01 Kernforschungsanlage Juelich Four a cuve de production en continu de gaz combustible a partir d'une matiere organique
DE3323675A1 (de) * 1983-07-01 1985-02-28 Richard Dipl.-Ing. 3170 Gifhorn Janesch Einrichtung zur karbonisierung, vergasung, biooel-gewinnung und synthesegas-gewinnung
EP0159420A1 (fr) * 1984-03-20 1985-10-30 JAMES HOWDEN & COMPANY LIMITED Réacteur pour gazéifier des combustibles solides
EP0240483A1 (fr) * 1986-04-01 1987-10-07 DISTRIGAZ Société anonyme dite: Procédé et appareil de gazéification de charbon en cocourant

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
BE457257A (fr) *
DE624242C (de) * 1934-05-23 1936-01-16 Kromag A G Fuer Werkzeug Und M Gaserzeuger mit abwaerts gerichtetem Zug, insbesondere zur Erzeugung von Holzgas fuer Kraftfahrzeuge
FR2407256A1 (fr) * 1977-10-31 1979-05-25 Pps Polyvalent Patent Service Procede et dispositif de production de gaz de bois
FR2422712A1 (fr) * 1978-04-13 1979-11-09 Duvant Moteurs Perfectionnements aux gazogenes a tirage inverse
EP0055440A1 (fr) * 1980-12-27 1982-07-07 Forschungszentrum Jülich Gmbh Procédé et installation pour la production continue de gaz combustible à partir de déchets organiques
FR2505350A1 (fr) * 1981-05-08 1982-11-12 Pillard Chauffage Gazeificateurs de combustibles solides a lit fixe et a tirage inverse
FR2519017A1 (fr) * 1981-12-24 1983-07-01 Kernforschungsanlage Juelich Four a cuve de production en continu de gaz combustible a partir d'une matiere organique
DE3323675A1 (de) * 1983-07-01 1985-02-28 Richard Dipl.-Ing. 3170 Gifhorn Janesch Einrichtung zur karbonisierung, vergasung, biooel-gewinnung und synthesegas-gewinnung
EP0159420A1 (fr) * 1984-03-20 1985-10-30 JAMES HOWDEN & COMPANY LIMITED Réacteur pour gazéifier des combustibles solides
EP0240483A1 (fr) * 1986-04-01 1987-10-07 DISTRIGAZ Société anonyme dite: Procédé et appareil de gazéification de charbon en cocourant

Cited By (27)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1999055803A1 (fr) * 1998-04-28 1999-11-04 Bruno Berger Procede fonde sur la production d'energie a partir de dechets, utilise pour produire du courant, de l'eau et/ou de l'hydrogene et/ou du methanol a partir de biomasse et/ou de dechets organiques
US7000780B1 (en) 1999-08-03 2006-02-21 Harald Martin Method and device for drying, separating, classifying and decomposing recoverable waste products
US7147681B1 (en) 1999-08-03 2006-12-12 Harald Martin Method and device for removing recoverable waste products and non-recoverable waste products
CN101245261B (zh) * 2008-03-03 2010-09-01 戴太才 一种机械连续进料气化炉及所用的原料
DE102008058602A1 (de) 2008-11-20 2010-06-02 Eurotherm Technologies Ag Vorrichtung in Form eines Bewegt-Bett-Vergasers und Verfahren zum Betreiben eines solchen in einer Anordnung zur thermischen Zersetzung von Abprodukten und Abfallstoffen
DE202008017561U1 (de) 2008-11-20 2009-10-29 Eurotherm Technologies Ag Vorrichtung in Form eines Bewegt-Bett-Vergasers
DE102008058602B4 (de) * 2008-11-20 2010-09-23 Eurotherm Technologies Ag Vorrichtung in Form eines Bewegt-Bett-Vergasers und Verfahren zum Betreiben eines solchen in einer Anordnung zur thermischen Zersetzung von Abprodukten und Abfallstoffen
WO2010057458A2 (fr) 2008-11-20 2010-05-27 Eurotherm Technologies Ag Dispositif en forme de gazéificateur à lit mobile et procédé pour faire fonctionner celui-ci dans un système de décomposition thermique de résidus et de déchets
DE202009010830U1 (de) 2009-02-05 2010-02-11 Eurotherm Technologies Ag Vorrichtung in Form eines Thermolysereaktors
WO2010088878A2 (fr) 2009-02-05 2010-08-12 Eurotherm Technologies Ag Dispositif en forme de réacteur de thermolyse et procédé pour faire fonctionner un tel dispositif pour la décomposition thermique de déchets
DE102009007768A1 (de) 2009-02-05 2010-08-26 Eurotherm Technologies Ag Vorrichtung in Form eines Thermolysereaktors und Verfahren zum Betreiben eines solchen in einer Anordnung zur thermischen Zersetzung von Abprodukten und Abfällen
ITTO20090328A1 (it) * 2009-04-27 2010-10-28 Pierluigi Martini Reattore autotermico cilindrico per la produzione di gas combustibile con sistema di entrata aria a flusso tangenziale
DE202009010832U1 (de) 2009-07-08 2010-01-28 Eurotherm Technologies Ag Anordnung zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen
DE102009031596A1 (de) 2009-07-08 2011-01-13 Eurotherm Technologies Ag Anordnung und Verfahren zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen und Verfahren zum Betreiben dieser Anordnung (Thermolyse-Spaltverfahren)
DE202009010833U1 (de) 2009-08-11 2009-11-05 Eurotherm Technologies Ag Anordnung zur Aufbereitung und thermischen Behandlung von Abprodukten und Abfällen
DE102013015920B4 (de) * 2013-09-20 2015-12-17 Recom Patent & License Gmbh Vorrichtung in Form eines 3-Zonen-Vergasers und Verfahren zum Betreiben eines solchen Vergasers zur thermischen Umwandlung von Abprodukten und Abfällen
DE102013015920A1 (de) 2013-09-20 2015-03-26 Intec Micro Powder Ag Vorrichtung in Form eines 3-Zonen-Vergasers und Verfahren zum Betreiben eines solchen Vergasers zur thermischen Umwandlung von Abprodukten und Abfällen
WO2015039640A1 (fr) 2013-09-20 2015-03-26 Recom Patent & License Gmbh Gazéifieur à 3 zones et procédé de fonctionnement d'un tel gazéifieur pour la transformation thermique de déchets et de résidus
CN105765038A (zh) * 2013-09-20 2016-07-13 雷科姆专利许可有限公司 三区式气化炉形式的装置以及操作此类气化炉用于废产物和废料热转化的方法
US9944866B2 (en) 2013-09-20 2018-04-17 Recom Patent & License Gmbh Three-zone gasifier and method for operating such a gasifier in order to thermally convert byproducts and waste materials
CN105765038B (zh) * 2013-09-20 2018-06-12 雷科姆专利许可有限公司 三区式气化炉形式的装置以及操作此类气化炉用于废产物和废料热转化的方法
DE202016106184U1 (de) 2016-11-04 2016-11-17 Hartwig Streitenberger Duplex-TEK-Mehrstufen-Vergaser
DE102016121046A1 (de) 2016-11-04 2018-05-09 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Duplex-TEK-Mehrstufen-Vergaser
WO2018082738A1 (fr) 2016-11-04 2018-05-11 Hs Techtransfer Ug (Haft.-Beschr.) & Co. Kg Gazéificateur multi-étagé à lit de carbone à expansion tourbillonnaire duplex
DE102016121046B4 (de) 2016-11-04 2018-08-02 HS TechTransfer UG (haftungsbeschränkt) & Co. KG Duplex-TEK-Mehrstufen-Vergaser
CN106701120A (zh) * 2016-12-29 2017-05-24 安徽虹源生物质有限公司 一种旋转式破拱、高料层上吸式生物质热解气化炭气联产装置及方法
IT202100002540A1 (it) * 2021-02-05 2022-08-05 Agenzia Naz Per Le Nuove Tecnologie Lenergia E Lo Sviluppo Economico Sostenibile Enea Reattore di gassificazione a letto fisso equicorrente

Also Published As

Publication number Publication date
AU5856494A (en) 1994-08-29
WO1994018287A1 (fr) 1994-08-18

Similar Documents

Publication Publication Date Title
EP0609802A1 (fr) Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides
EP2082013B1 (fr) Procédé pour préparer un produit gazeux riche en hydrogène
EP1226222B1 (fr) Procede de gazeification de matieres organiques et melanges de matieres
EP1261827B1 (fr) Reacteur et procede de gazeification et/ou de fusion de matieres
DE102013018074B3 (de) Hochofen und verfahren zum betrieb eines hochofens
CH615215A5 (fr)
WO2010003968A2 (fr) Procédé et dispositif pour produire du gaz de synthèse à faible teneur en goudrons à partir de biomasse
WO1981000112A1 (fr) Procede et installation pour la gazeification de combustibles en morceaux
DE102004024672B4 (de) Vorrichtung und Verfahren zur Erzeugung eines teerfreien Schwachgases durch Vergasung von Biomasse
EP3212566B1 (fr) Procédé et installation de production de gaz de synthèse
DE102009039920A1 (de) Verfahren und Vorrichtung zur Nutzung von Sauerstoff bei der Dampfreformierung von Biomasse
EP1950272A1 (fr) Procédé et dispositif destinés à la transformation thermique de pellets ou de copeaux de bois
EP3601925B1 (fr) Dispositif de réaction comprenant un échangeur de chaleur et son utilisation
EP1187891B1 (fr) Procede et dispositif d'elimination de dechets
EP2454013B1 (fr) Réacteur et procédé de gazéification de biomasse
DE60026264T2 (de) Verfahren und Anlage für die Herstellung von brennbaren Gasen aus an organischen Materialien reichen Einsätzen
EP1377649B1 (fr) Installation et procede pour produire de l'energie par pyrolyse
DE102004008621A1 (de) Herdofenreaktoren und Verfahren zur Umwandlung fester und pastöser, organischer Stoffe in Prozessgas
DE102010002737B4 (de) Vorrichtung zur Durchführung eines Verfahrens zur Erzeugung von Dampf
DE2855510B1 (de) Verfahren und Anlage zur thermischen Verwertung von Abfaellen
EP0360052A1 (fr) Réacteur de pyrolyse pour l'élimination thermique de déchets
DD285819A5 (de) Verfahren und eine maschine fuer die umsetzung von brennbaren schmutzstoffen oder abfaellen in saubere energie und brauchbare produkte
DE102007017859A1 (de) Vergaser
DE4317412C2 (de) Anlage zur thermischen Behandlung von kohlenstoffhaltigem Material
EP0001856B1 (fr) Procédé et installation pour la production en continu de gaz de gazogène et de gaz à l'eau

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AT BE CH DE DK ES FR GB GR IE IT LI LU MC NL PT SE

RBV Designated contracting states (corrected)

Designated state(s): AT BE CH DE DK ES FR GB IT LI LU NL PT SE

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 19950211