EP2377911A2 - Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide - Google Patents

Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide Download PDF

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Publication number
EP2377911A2
EP2377911A2 EP10185292A EP10185292A EP2377911A2 EP 2377911 A2 EP2377911 A2 EP 2377911A2 EP 10185292 A EP10185292 A EP 10185292A EP 10185292 A EP10185292 A EP 10185292A EP 2377911 A2 EP2377911 A2 EP 2377911A2
Authority
EP
European Patent Office
Prior art keywords
gas
zone
shaft
oxidation
oxidation chamber
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.)
Granted
Application number
EP10185292A
Other languages
German (de)
English (en)
Other versions
EP2377911A3 (fr
EP2377911B1 (fr
Inventor
Björn Kuntze
Bruno Merz
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Big Dutchman International GmbH
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Big Dutchman International GmbH
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Filing date
Publication date
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Publication of EP2377911A2 publication Critical patent/EP2377911A2/fr
Publication of EP2377911A3 publication Critical patent/EP2377911A3/fr
Application granted granted Critical
Publication of EP2377911B1 publication Critical patent/EP2377911B1/fr
Not-in-force legal-status Critical Current
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/22—Arrangements or dispositions of valves or flues
    • 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
    • C10J3/58—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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/15—Details of feeding means
    • C10J2200/156—Sluices, e.g. mechanical sluices for preventing escape of gas through the feed inlet
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1223—Heating the gasifier by burners

Definitions

  • the invention relates to a method and apparatus for producing fuel gas from a solid fuel in a shaft gasifier, which is designed as a fixed-bed gasifier.
  • a fuel gas is generated in a pyrolysis stage, which contains a high tar load.
  • the tar load together with the fuel gas by a high-temperature oxidation at a temperature of well above 1000 deg. C either thermally cracked and / or oxidized.
  • the oxidation state is operated with air or oxygen. In this case, temperatures above the ash melting point of the fuel used are achieved.
  • the process is generally substoichiometric.
  • the exhaust gas from the oxidation stage is then subjected to a reduction reaction with in-house produced coke (eg charcoal), whereby the combustion products (CO2 and H2O) with the coke to the combustible gas components CO and H2 react.
  • coke eg charcoal
  • CO2 and H2O combustion products
  • the generated combustible gas is intended for use in internal combustion engines and gas turbines.
  • the gas stream from the pyrolysis stage is passed through the oxidation stage and air or oxygen is used as the oxidizing agent, very high temperatures are required to destroy the tar constituents (> 1300 ° C.). Since the process proceeds clearly substoichiometric, the destruction is based more on a thermal splitting than on an oxidation.
  • the oxidation stage due to high dust loading of the pyrolysis gases procedural difficulties with the handling of the forming liquid slag, which also partially discharged with the gas stream and enters the reduction zone and hardens there.
  • the following reduction stage must be constructively designed for the high temperature level of the incoming gas stream.
  • the raw gas produced in carburetors has a more or less large amount of dust.
  • the load is essentially dependent on the design of the carburettor, the starting materials and the mode of operation.
  • Fixed bed gasifiers often have raw gas dust loadings of 2 - 8 g / Nm ⁇ 3>. The raw gas dust loadings of fluidized bed gasifiers are even higher.
  • the target values for clean gas dust loading are dependent on the requirements of the gas utilization facilities. In practice, for example, for applications with heat engines clean gas dust loads of up to 50 mg / NM ⁇ 3> is required. The target values for this application are 5 mg / Nm ⁇ 3>.
  • the well-known methods such. Cyclone, electrostatic filters, fabric filters, hot gas filtration, scrubbers, etc. to disposal.
  • the target values of 5 mg / Nm ⁇ 3> required above can be achieved, for example, with fabric filters or hot gas filters.
  • fabric filters When using fabric filters, the dust-laden raw gas is initially at the typical temperature range of the filter materials 80 - 250 deg. C to pre-cool. In terms of process technology, the dust load proves to be a hindrance.
  • the use of hot gas filtration is particularly advantageous, since here, without intermediate cooling in the typical temperature range of the raw gas of 400 to 800 ° C.
  • common filter elements such as e.g. Filter candles made of glass fiber, sintered metal or ceramic, can be used. These elements are arranged in corresponding independent filter apparatuses.
  • the problem of discharging the filter ash deposited in the filter is to be solved.
  • the high operating temperatures and other requirements serving for explosion protection lead to cost-intensive designs.
  • the object of the present invention is to provide a method and an apparatus for the simple and economic production of low-tar and dust-free fuel gas by multi-stage gasification of solid fuels.
  • the procedure is process-technically stable and has improved operating parameters.
  • the fuel gas produced is intended for use in heat engines.
  • Object of the present invention is also to provide measures for the dedusting of raw gas from a gasification plant, which takes place by the integration of the hot gas filtration in the carburetor in a manner that neither a separate filter housing nor an independent discharge of the filter ash is required.
  • the invention as characterized in the claims provides a method of producing fuel gas from a solid fuel, comprising the steps of: supplying the fuel into a pit gasifier formed as a descending fixed bed reactor; Degassing of the fuel in a degassing zone of the shaft gasifier by autothermal partial gasification with air supply from the outside; Supplying the pyrolysis gas thus obtained from the degassing zone into an oxidation stage located within the shaft and separated from the degassing zone, in which partial oxidation and thermal cracking of the raw gas take place with the addition of an oxidizing agent; and reduction of the exhaust gas from the oxidation stage in a reduction zone downstream of the oxidation zone through the coke formed in the degassing zone with heat extraction to a fuel gas, wherein the Redutechnischskoks from the degassing zone is bypassing the oxidation stage of the reduction zone fed directly.
  • a further feature of the method according to the invention is that the gas produced is filtered before it leaves the shaft.
  • the filtering is carried out by arranged in front of the outlet opening filter cartridges, which are exposed to time-dependent or differential pressure controlled a pressure surge cleaning.
  • the process according to the invention has the advantage that the oxidation stage is charged with a low-pyrolysis gas and can be operated at a comparatively low oxidation temperature and thus also permits a low gas inlet temperature into the reduction stage, requires little reducing coke and allows easy transport of the uncut reducing coke from the degassing zone the reduction zone allows.
  • the integrated into the gas generation filtering of the raw gas increases the freedom from dust of the clean gas.
  • the invention also consists in a device for producing fuel gas from a solid fuel in a shaft gasifier, which is designed as a descending fixed bed reactor.
  • the device comprises a central oxidation chamber arranged in the fixed bed reactor, which is separated from the degassing zone and to which the pyrolysis gas produced in the degassing zone is supplied.
  • the oxidation chamber is connected to an oxidant supply line via which the oxidation chamber is supplied with an oxidizing agent, under the action of which partial oxidation and thermal cracking of the pyrolysis gas take place.
  • a reduction zone which receives the exhaust gas from the oxidation chamber and which is supplied to the resulting in the pyrolysis gas production Redutationskoks from the degassing zone directly and bypassing the oxidation chamber.
  • a reduction of the exhaust gas from the oxidation chamber by the supplied reducing coke with heat removal takes place to a fuel gas.
  • a filter arrangement which is arranged inside the shaft in front of a gas outlet opening.
  • the filter assembly comprises filter cartridges, which are arranged substantially horizontally or vertically in front of the gas outlet opening and which are exposed via jet pulse nozzles, the time-dependent or differential pressure controlled by a pressure surge cleaning.
  • FIG. 1 shows a schematic representation of a shaft carburetor, which is designed as a descending fixed-bed gasifier 1, which has an upright cylindrical shaft 2.
  • the fixed bed gasifier 1 is fed via a lock system 3 fuel from above.
  • This may be coal, wood or other woody biomasses.
  • the supplied fuel is crushed into pieces or chips.
  • the level of the shaft with fuel 4 is monitored by a level indicator 5.
  • a nozzle system which may comprise at least one or more nozzle planes, which comprises a plurality of distributed over the circumference of the shaft 2 nozzles 6, which are fed via a ring channel 7 with fresh air.
  • the annular channel 7 is supplied with an air stream 8 via an inlet connection 9, so that a partial flow of the air required for an autothermal partial gasification of the fuel is introduced into the shaft 2 through each of the nozzles.
  • energy is obtained by partial combustion under air supply.
  • the fixed-bed gasifier 1 has an oxidation stage separate from the degassing zone 10, in which a partial oxidation and a thermal cracking of the raw gas takes place with the addition of an oxidizing agent.
  • the oxidation stage is formed by an oxidation chamber 12, which is preferably arranged centrally in the carburettor shaft 2.
  • the oxidation chamber 12 has a cylindrical housing 13, which is arranged concentrically to the longitudinal axis 14 of the shaft and which is bounded above by a conical part 15 and which is open at the bottom.
  • the supply air duct 16 passes through the cover 17 of the shaft 2 and extends concentrically to the longitudinal axis 14 of the shaft 2.
  • it can also be arranged laterally outside the longitudinal axis or in the radial direction and parallel to this run.
  • radial openings 18 are arranged, which are distributed over the circumference of the housing 13.
  • the reducing coke 24 is generated in the space between the oxidation chamber 12 and the wall of the carburettor shaft 2 during the degassing of the fuel 4. Due to the central arrangement of the oxidation chamber 12 in the shaft 2 and the cylindrical housing 13 of the oxidation chamber 12 an annular space between the housing 13 and the shaft wall is formed, which is referred to herein as the annular gap 26 and the reducing coke 24 over the circumference of the annular gap 26th distributed to the reduction zone 23 is supplied. In this case, the reducing coke 24 can slip into the reduction zone 23 to replace the used reducing coke without the need for a mechanical conveying device. By reducing coke 24, the exhaust gas 22 is reduced in the reduction zone 23 under heat removal to fuel gas.
  • the reduction zone 23 is delimited by a grate which is designed as a movable grate and in particular as a rotary grate 28 and by means of which the ash produced during the reduction process is separated from the reduction zone 23 and disposed of via an exit opening 29.
  • a grate which is designed as a movable grate and in particular as a rotary grate 28 and by means of which the ash produced during the reduction process is separated from the reduction zone 23 and disposed of via an exit opening 29.
  • To drive the rotary grate 28 is an electric gear motor 30.
  • the shaft 2 is closed at the bottom by a bottom plate 31 and rests on columns, of which FIG. 1 only the columns 32 and 33 are shown.
  • the motor 30 is mounted below the bottom plate 31 on the columns or on the bottom plate and connected by a shaft 34 with the rotary grate 28.
  • the height extent of the reduction zone 23 can be changed, which is an optimization of the method in terms of ash quality, pressure loss in the reduction zone 23 and adaptation to fuel properties is advantageous.
  • the shaft 34 is arranged axially displaceable in the output shaft of the electric geared motor 30 designed as a hollow shaft and can be fixed in the respectively selected position against a further displacement by adjusting rings, not shown.
  • the height of the reduction zone 23 is dependent on a number of factors such as fuel ash content, particulate matter, gas generator load and coke reactivity.
  • the oxidation chamber 12 is arranged in the cylindrical shaft 2 concentric with its longitudinal axis 14.
  • the supply air duct 16 opens centrally from above into the oxidation chamber 12 and is extended in the direction of the center thereof, whereby a uniform combustion of the pyrolysis gas 20 supplied from the degassing zone 10 is promoted.
  • Alternatively, to achieve a uniform combustion process within the oxidation chamber of the supply air duct 16 may be provided at its outlet opening with a mixing chamber in which the pyrolysis gas 20 and the supply air 21 are intimately mixed.
  • the annular gap 26 filled with reducing coke 24 forms a flow resistance for the pyrolysis gas 20 generated in the degassing zone 10. Due to the flow resistance for the pyrolysis gas 20 prevailing in this coke charge, this preferably flows through the openings 18 arranged in the upper region into the oxidation chamber 12, which pure gas space has only a negligible flow resistance.
  • a flow through the annular gap 26 with pyrolysis gas 20 is also prevented by the inflowing through the lower nozzle levels supply air 8 generates a very low tarry fuel gas and thus a flow-related barrier represents for the pyrolysis gas formed in the region of the uppermost nozzle level.
  • the very low tar content of the fuel gas formed in the region of the lower nozzle levels is due to the fact that here already degassed fuel is present in the form of the reducing coke 24 and thus no tar is released.
  • the fuel gas 35 collected in the space 45 below the grate 28 is sucked downwards or laterally out of the reduction zone 23, depending on the dedusting concept used.
  • the removal of the fuel gas 35 takes place laterally through an arranged in the wall of the shaft 2 in the lower part of the outlet opening 36.
  • the fuel gas is after his Removal from the reduction zone 23 cooled and cleaned according to the requirements of use in heat engines.
  • the oxidation chamber 12 can also be operated with a significantly lowered oxidation temperature. This is always useful when using ash-rich fuels with low ash melting points required for the thermal destruction of long-chain hydrocarbons oxidation temperatures of 1000 deg. C or above are not permitted due to the danger of slagging.
  • the intended for the oxidation stage combustion air or the pyrolysis gas stream 20 steam is added.
  • flue gas from the heat engine or other combustion plants can be mixed.
  • the combustion temperatures are lowered. This process corresponds to the exhaust gas recirculation of internal combustion engines to reduce NOx emissions.
  • the water vapor content in the gas increases, which also has a destructive effect on the tar.
  • the admixture increases the mass flow in the oxidation chamber and thereby lowers the oxidation temperature with otherwise constant material flows.
  • the desired destruction of the long-chain hydrocarbons can be achieved if the amount of water vapor and / or flue gas admixed is determined such that even at stoichiometric ratios the oxidation temperature which is permissible to prevent the slagging is no longer exceeded.
  • the hydrocarbons are then oxidized at considerably lower temperatures to carbon dioxide and water vapor.
  • slightly superstoichiometric ratios can also be set, resulting in combustion with excess oxygen. This is fast and increases the reaction rate, which can lead to smaller sizes of apparatus.
  • the additionally introduced water vapor and / or the additionally introduced flue gas causes destruction of the tar constituents even at substoichiometric ratios, so that the oxidation temperature can be reduced at high partial pressures of water vapor.
  • the fixed-bed gasifier 1 is equipped with more than one nozzle plane with nozzles 6 for introducing the gasification air.
  • two nozzle levels are provided, each of which receives an air stream 8 is supplied.
  • the nozzle levels 6 can be charged with different mixtures of air, water vapor and flue gases from the heat engine. The enrichment of the air stream 8 with steam and / or flue gas causes a reduction of the combustion temperatures in the degassing zone 10 and allows the control of these combustion temperatures.
  • FIG. 2 a shaft carburetor based on FIG. 1 described type, which is equipped with an additional gasification zone.
  • the manhole carburetor of FIG. 1 corresponding components have in FIG. 2 the same reference numerals.
  • the shaft carburetor of FIG. 2 a degassing zone 10, which is supplied via an inlet port 9 air, a central oxidation chamber 12 with a supply air duct 16 and a reduction zone 23.
  • a further gasification zone 40 is provided, which is also referred to herein as Restkoksvergasungszone and which is operated with additional air as a countercurrent gasifier.
  • the additional air is supplied as under-air 41 via an inlet port 42, which is arranged below a movable grate 43.
  • the grate 43 is like the grate 28 of FIG. 1 designed as a rotating grate and is driven by an electric geared motor 44.
  • flue gas and / or water vapor can also be supplied for lowering and controlling the reaction temperatures.
  • the generated raw gas is collected in an annular gas collecting space 45, which is arranged at the level of the reduction zone 23 and is formed by a cylindrical wall 46 and a cover 47.
  • the gas collection chamber 45 is open at the bottom and is only through the bulk cone 48 of Reduction coke limited.
  • the raw gas 50 collected in the gas collecting space 45 is sucked off via a nozzle 51 arranged on the circumference of the shaft 2.
  • An advantage of in FIG. 2 illustrated device is that the separated with the grate 43 and disposed of via an outlet 49 ash contains only very small amounts of carbon.
  • FIGS. 3 and 4 A further embodiment of the device according to the invention is shown in FIG FIGS. 3 and 4 ,
  • the in FIG. 3 Shaft carburetor shown corresponds to that of FIG. 1 and additionally has an integration of the dedusting of the raw gas into the raw gas collecting space.
  • Dedusting takes place through a filter arrangement 55, which is arranged below the grate 28 in a correspondingly enlarged raw gas collecting space 54 in front of the gas outlet opening 36.
  • the filter arrangement 55 comprises filter cartridges 56 which are known per se and which are aligned transversely to the longitudinal axis 14 of the shaft, preferably horizontally, and are fastened to a filter plate 57 which separates a clean gas collecting space 58 from the raw gas collecting space 54.
  • the filter cartridges 56 are held by a support plate 59.
  • the filter cartridges 56 are arranged one above the other in front of the gas outlet opening 36, as shown in the sectional view of FIG. 4 seen.
  • the raw gas is passed through the filter cartridges 56, wherein the dust contained in the raw gas is deposited on the filter cartridges 56.
  • the separated dust collects together with the grate ash in the region 60 at the bottom of the shaft 2 and is discharged through the outlet opening 29.
  • the cleaning of the building up on the filter cartridges 56 filter cake is done according to the prior art time or differential pressure controlled by means of pressure surge cleaning (jet pulses).
  • the filter cartridges are fed via jet-pulse nozzles 61 compressed gas pulses for cleaning the filter cartridges.
  • jet-pulse nozzles 61 compressed gas pulses for cleaning the filter cartridges.
  • the jet pulse nozzles 61 are fed in the prior art with compressed inert gas (nitrogen or carbon dioxide) or with compressed natural gas (clean gas).
  • FIG. 5 is a modification of the gasification apparatus according to FIG. 2 represented, which is equipped with an integrated dedusting of the raw gas produced.
  • shaft carburetor 64 of FIG. 5 Dedusting is done by a filter assembly 65 which is arranged on the circumference of the carburettor.
  • the filter assembly 65 includes hot gas filter cartridges 67, which are aligned substantially parallel to the longitudinal axis 14 of the shaft.
  • the shaft carburetor 64 has an enlarged Rohgassammelraum 54, including the carburettor shaft is formed in two parts.
  • a downwardly open upper carburetor chute 68 projects into an enlarged outer chute 69 which forms the lower part of the carburettor shaft.
  • annular gap 70 Between the upper carburetor shaft 68 and the outer shaft 69 is an annular gap 70, the upper end of which is connected by a flange 71 to the upper carburetor shaft 68.
  • a gas outlet opening 72 is arranged at the upper end of the annular gap 70 in the outer shaft 69.
  • a filter plate 78 Below the gas outlet opening 72 is located in the annular gap 70, a filter plate 78, in which the filter cartridges 67 are mounted and which separates a clean gas collection chamber 73 from the raw gas collection chamber 54.
  • the filter cartridges 67 protrude in the annular gap 70 substantially parallel to the common longitudinal axis 14 of the wells 68 and 69 down.
  • the dust deposited on the filter candles falls within the scope of the cleaning described below as a filter cake on the bulk cone 74 of the Reduktionskokses 75.
  • the filter dust enters the further gasification zone for the residual coke.
  • the strongly carbonaceous filter dust is then largely gassed into ashes as part of the progressing gasification of the residual coke and discharged together with the grate ash via the outlet port 77.
  • the cleaning of the filter cartridges 67 by compressed gas pulses, which are supplied via jet-pulse nozzles 76 takes place.
  • the jet-pulse nozzles 76 are arranged in the flange 71 in association with the filter cartridges 67.
  • the pressure gas supplied through the nozzles 76 corresponds to that previously in connection with FIG FIG. 3 described.
  • dedusting into a shaft gasifier is not limited to shaft carburetor with an oxidation stage separate from the degasification zone in the form of a central oxidation chamber, but may also be applied to shaft carburetors of other types such as e.g. at carburetors, which work after the so-called double fire procedure.
  • a double firing type carburetor 80 is shown in FIG FIG. 6 shown schematically.
  • This carburetor corresponds in its outer structure of the shaft carburetor of FIG. 2 but without a separate from the degassing zone oxidation state in the form of a central oxidation chamber.
  • the supply air to the carburetor 80 is usually referred to with upper air and lower air and is in FIG. 6 represented by the air feeds 81 and 82.
  • the integrated dedusting is achieved in the carburetor 80 by a filter assembly 83 which is arranged on the circumference of a correspondingly enlarged Rohgassammelraum 84.
  • the filter assembly 83 contains hot gas filter cartridges 86, which are arranged substantially parallel to the longitudinal axis of the carburetor 80.
  • the enlargement of the Rohgassammelraums 84 and the arrangement of the filter cartridges 86 corresponds to that in conjunction with FIG. 5 described embodiment.
  • the filter cartridges 86 are arranged in an annular gap between a downwardly open shaft 90 and an outer shaft 91 comprising this shaft and lie in the flow direction in front of a gas outlet opening 92 which is located at the upper end of the annular gap.
  • the filter cartridges 86 are mounted in a filter plate 87 which separates a clean gas collecting space 85 from the raw gas collecting space 84.
  • the cleaning of the filter cartridges 86 is again carried out by compressed gas pulses via jet-pulse nozzles 93, which are arranged in a connection flange 94 of the outer shaft to the downwardly open shaft above the filter cartridges 86 are supplied.
  • the compressed gas supplied through the nozzles 93 is the same as that previously described in connection with FIG FIG. 3 described. As with the device after FIG.
  • the dust deposited on the filter cartridges precipitates as filter cake onto a pour cone 94 of the reduction coke 95. In this way, the filter dust passes into the further gasification zone for the residual coke.
  • the highly carbonaceous filter dust is then largely gassed into ashes in the context of progressing gasification of the coke and discharged together with the grate ash on the outlet port 96.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
EP10185292.9A 2006-06-08 2007-06-01 Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide Not-in-force EP2377911B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE200620009174 DE202006009174U1 (de) 2006-06-08 2006-06-08 Vorrichtung zur Erzeugung von Brenngas aus einem festen Brennstoff
EP07010863A EP1865046B1 (fr) 2006-06-08 2007-06-01 Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide

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EP07010863A Division EP1865046B1 (fr) 2006-06-08 2007-06-01 Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide
EP07010863A Division-Into EP1865046B1 (fr) 2006-06-08 2007-06-01 Procédé et dispositif destinés à la production de gaz combustible à partir d'un combustible solide
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Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008036502A1 (de) * 2008-08-05 2010-02-11 Krones Ag Verfahren und Vorrichtung zur Herstellung von Synthesegas aus Biomasse
DE202010013745U1 (de) 2010-02-05 2010-12-30 Pyrox Gmbh Schachtvergaser zur Erzeugung von Brenngas aus einem festen Brennstoff
DE102010033646B4 (de) 2010-02-05 2012-05-24 Pyrox Gmbh Verfahren und Schachtvergaser zur Erzeugung von Brenngas aus einem festen Brennstoff
RU2542319C2 (ru) 2010-02-16 2015-02-20 Биг Дачман Интернэшнл Гмбх Устройство для газификации и способ газификации
BR122019000133B1 (pt) 2010-11-08 2020-09-15 Ze Energy Inc Reformador para reformação de gás de destilação seco e sistema de reformação
DE202011004328U1 (de) 2011-03-22 2012-06-25 Big Dutchman International Gmbh Schachtvergaser zum Betrieb bei einer unterstöchiometrischen Oxidation
DE102011075438A1 (de) 2011-05-06 2012-11-08 Bilfinger Berger Industrial Services Gmbh Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlestoffhaltigen Edukten durch Vergasung
DE202012008777U1 (de) * 2012-09-13 2015-10-06 Big Dutchman International Gmbh Vorrichtung zur Erzeugung von Brenngas aus einem festen Brennstoff
CN103175222B (zh) * 2013-03-19 2014-12-17 哈尔滨工程大学 一种用于化学回热循环的空气助燃双燃料喷嘴
CZ26592U1 (cs) * 2013-12-18 2014-03-10 Tarpo Spol.S R.O. Zařízení pro vícestupňové zplyňování uhlíkatých paliv
AT515649A1 (de) * 2014-04-04 2015-10-15 Leopold Dipl Ing Seirlehner Verfahren und eine Vorrichtung zum Herstellen von Brenngas aus kohlenstoffhaltigen festen Ersatzstoffen
DE102021134191A1 (de) 2021-12-22 2023-06-22 BHYO GmbH Verfahren und Anlageverbund zur Erzeugung von Synthesegas

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4404673C2 (de) 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
DE19846805A1 (de) 1998-10-10 2000-04-13 Clemens Kiefer Verfahren und Vorrichtung zur Vergasung und Verbrennung

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US987195A (en) * 1911-03-21 Bruno Versen Gas-producer.
FR979452A (fr) * 1942-04-22 1951-04-26 Perfectionnements aux gazogènes à bois et analogues
DE1037051B (de) * 1944-07-31 1958-08-21 Metallgesellschaft Ag Verfahren zum Schwelen und Vergasen fester Brennstoffe in Schachtgaserzeugern
US2821464A (en) * 1955-01-17 1958-01-28 Bleyer Karl Method and apparatus for making producer gas
NL167191C (nl) * 1975-04-01 1981-11-16 Nii Slantsev & Slantseper Oven voor het door thermisch behandelen winnen van koolwaterstoffen uit een massa vaste brandstof, zoals olieschalies.
DD150906A1 (de) * 1980-05-22 1981-09-23 Roscher Karl Dieter Verfahren und vorrichtung zur festbettdruckvergasung
DE8328140U1 (de) * 1983-09-28 1991-04-25 Michel-Kim, Herwig, 1000 Berlin Reaktorvorrichtung zur Erzeugung von Generatorgas aus brennbaren Abfallprodukten
DE3406307A1 (de) * 1984-02-22 1985-08-22 KPA Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Verfahren zur erzeugung von brennbaren gasen aus abfallstoffe
SE446101B (sv) * 1984-12-28 1986-08-11 Skf Steel Eng Ab Sett och anordning for att generera gas
DE3528975A1 (de) * 1985-08-13 1987-02-26 Knut Kiener Biomassen-totalvergasungsanlage
DE3543424A1 (de) * 1985-12-09 1987-06-11 Deilmann Ag C Verfahren und vorrichtung zur erzeugung von gas
DE19618213A1 (de) * 1996-05-07 1997-11-13 Petersen Hugo Verfahrenstech Verfahren zur Erzeugung von Brenngas und Anlage zur Durchführung des Verfahrens
IT1289003B1 (it) * 1996-10-16 1998-09-25 Tomadini Gino & C Procedimento perfezionato di gassificazione di combustibili e relativo dispositivo gassificatore
TR200000412T1 (tr) * 1998-06-16 2000-10-23 Graveson Energy Management Ltd. Gazlaştırma reaktör aygıtı.
EP1248828B1 (fr) * 2000-01-10 2004-06-23 Adrian Fürst Dispositif et procede pour produire des gaz combustibles
DE10258640A1 (de) * 2002-12-13 2004-06-24 Björn Dipl.-Ing. Kuntze Verfahren und Vorrichtung zur Erzeugung von Brenngas aus festen Brennstoffen
DE202004011213U1 (de) * 2004-07-16 2004-11-04 Kuntschar, Walter Gleichstromvergaser
AT505188B1 (de) * 2004-08-27 2009-06-15 Schiefer Erwin Reaktor zur vergasung von biomasse

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE4404673C2 (de) 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
DE19846805A1 (de) 1998-10-10 2000-04-13 Clemens Kiefer Verfahren und Vorrichtung zur Vergasung und Verbrennung

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Publication number Publication date
EP2377911A3 (fr) 2013-12-25
EP2377911B1 (fr) 2015-08-12
DE202006009174U1 (de) 2007-10-11
EP1865046B1 (fr) 2012-10-03
DK1865046T3 (da) 2012-10-15
SI1865046T1 (sl) 2013-01-31
EP1865046A1 (fr) 2007-12-12
ES2548984T3 (es) 2015-10-22
ES2393408T3 (es) 2012-12-21

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