EP2487226A2 - Procédé et dispositif de génération d'un gaz - Google Patents

Procédé et dispositif de génération d'un gaz Download PDF

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Publication number
EP2487226A2
EP2487226A2 EP12167075A EP12167075A EP2487226A2 EP 2487226 A2 EP2487226 A2 EP 2487226A2 EP 12167075 A EP12167075 A EP 12167075A EP 12167075 A EP12167075 A EP 12167075A EP 2487226 A2 EP2487226 A2 EP 2487226A2
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EP
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Prior art keywords
zone
gasification
fuel
fluidized bed
gasification zone
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EP12167075A
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German (de)
English (en)
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EP2487226A3 (fr
Inventor
Klaus Bosch
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Biomassekraftwerk Betriebs GmbH and KG
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Biomassekraftwerk Betriebs GmbH and KG
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Publication of EP2487226A2 publication Critical patent/EP2487226A2/fr
Publication of EP2487226A3 publication Critical patent/EP2487226A3/fr
Withdrawn legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/006—General arrangement of incineration plant, e.g. flow sheets
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F23G5/0276—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage using direct heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
    • F23G5/16—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber
    • F23G5/165—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion in a separate combustion chamber arranged at a different level
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/12—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of plastics, e.g. rubber
    • 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
    • C10J2200/158—Screws
    • 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
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0996—Calcium-containing inorganic materials, e.g. lime
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C10J3/503—Fuel charging devices for gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/30—Pyrolysing
    • F23G2201/304—Burning pyrosolids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2201/00—Pretreatment
    • F23G2201/70—Blending
    • F23G2201/701—Blending with additives

Definitions

  • the present invention relates to a method for producing a gas by gasification of fuels, in particular biogenic fuels and / or plastics, as well as a device for carrying out this method.
  • a method in which, in order to produce a nitrogen-poor or nearly nitrogen-free gas by gasification heterogeneous biogenic fuels and plastics first brought the fuel to be gasified under exclusion of air with the hot bed material of a fluidized bed combustion in contact and thereby in the presence of water vapor and / or CO 2 is at least partially degassed.
  • the resulting residual fuel is fed to a fluidized bed with circulating bed material and thereby burned, whereby the bed material is heated and is returned after its separation from the exhaust gas back into the antechamber.
  • the gasification plant for carrying out the method is characterized in that it is formed in a housing of an internally circulating fluidized bed, wherein the antechamber is used for the return of the hot bed material and is formed as a gasification space, while the actual fluidized bed is formed as a combustion zone are provided for the integration of the bed material in the fluidized bed as well as in the return of the hot bed material in the vestibule lock-like devices.
  • the bed material sand is mixed with catalytic nickel and / or niobium compounds, so that thereby the gasification temperature is lowered and the gas composition is controlled in particular in the direction of reducing the CH 4 content.
  • the in AT 405 937 B described method has the disadvantage that the automatically adjusting temperatures in the gasification and combustion part can not be practically influenced. In practice, this means that the process is almost unusable, since the temperature in the gasification for the gas quality and in particular for the tar content of the product gas is crucial. The possibility of regulating the temperature to a desired value is therefore absolutely necessary.
  • the bed material In the gasification of heterogeneous biogenic fuels or plastics based on fluidized bed technology, the bed material is circulated between a combustion zone and a gasification zone in an internal circuit, whereby a portion of the fuel in the combustion zone is burned and thus the bed material is heated.
  • the heated bed material passes through a separator (eg cyclone) and optionally a siphon into the gasification zone.
  • a separator eg cyclone
  • optionally a siphon into the gasification zone.
  • the endothermic gasification process is driven and the bed material is cooled according to the amount of fuel supplied.
  • the cooled bed material passes through a connecting channel with an unreacted part of the fuel back into the combustion part and is heated there again accordingly. With this cycle it is possible to maintain the endothermic gasification process.
  • a separator may be in the form of a cyclone, which basically separates the bed material from the flue gas. Since the degree of separation of, for example, a cyclone is limited, a portion of the bed material is lost via the flue gas path. This loss must be compensated with the addition of additional bed material, which reduces the efficiency of a gasification plant.
  • fluidized bed media beds materials
  • sands can be used as bedding material or preferably calcite, dolomite or olivine or mixtures thereof.
  • various artificially produced materials such as nickel and / or zirconium compounds can be used.
  • the fuel is introduced into or over the fluidized bed and reacted under stoichiometric conditions only partially thermally.
  • the product gas produced consists of various components, with the higher hydrocarbon compounds (referred to as tars for short) causing the greatest procedural difficulties in the energetic conversion of the fuel gas.
  • the present invention relates to a process for producing a gas by gasification of fuels, in particular biogenic fuels and / or plastics, in a reactor comprising a gasification and a combustion zone, wherein the reactor comprises a fluidized bed material which is continuously heated from the combustion zone into the gasification zone and from the gasification zone in the cooled state together with non-gasified residual fuel is fed back into the combustion zone, wherein the fuel is introduced into the formed as a circulating fluidized bed gasification zone, the fuel in the circulating fluidized bed of the gasification zone at Heilab gleich to form a product gas at least is partially gasified and spent and the remaining or unreacted residual fuel is spent together with the cooled bed material in the combustion zone, where the bed material to form a fast fluidized bed it is fluidized, reheated by combustion of the residual fuel and recycled via a separator in the circulating fluidized bed of the gasification zone, wherein the flue gas formed in the combustion zone and recovered from the separator is fed to a Feststoffabscheider to
  • the solid components of the flue gas which in particular comprise bed material, arising in the combustion zone, overflow a separator, such as a cyclone, at least partially removed from the flue gas.
  • a separator such as a cyclone
  • at least one further solids separator is used according to the invention, which separates the solid constituents of the flue gases leaving the reactor substantially entirely from the gas phase. Any fines still present in the flue gas can be removed via a flue gas filter.
  • the first time it is possible for the first time to efficiently separate bed material located in the flue gas from the flue gas.
  • the bed material accumulating in the at least one further separation device is subsequently returned directly to the combustion zone.
  • the deposited bed material may be collected in a container and optionally mixed with "fresh" bed material to be subsequently recycled to the incineration zone.
  • Suitable catalytically active bed material are, for example, Ca 2 SiO 4 (Larnit), MgO (periclase), SiO 2 (quartz), CaCO 3 (calcite), Mg 2 SiO 4 (forsterite), Fe 3 O 4 (magnetite), Al 2 O 3 (corundum), Ca 3 Mg (SiO 4 ) 2 (Merwinite), CaMgSiO 4 (monticellite), Ca 3 (PO 4 ) 2 ( ⁇ -tri-calc.ph.) Or mixtures thereof.
  • Catalytic activation of the bed material under the above conditions occurs in a temperature range of about 700-950 ° C.
  • the catalytic activation of the bed material makes it possible to reduce the tar concentration in the product gas of up to> 8 g / Nm 3 to ⁇ 0.5 g / Nm 3 . Due to the lower tar concentration due to the catalytically active bed material, it is possible to maintain the downstream process engineering facilities, such as wood gas cooling, wood gas filtration and wood gas scrubbing, in a stable and trouble-free operation and the appropriate quality for a variety of work machines, such as gas engine, gas turbine and fuel cell, to provide.
  • process engineering facilities such as wood gas cooling, wood gas filtration and wood gas scrubbing
  • the flue gas produced during combustion includes beside Bed material also harmful to the environment, which may be due in particular to incomplete combustion of the fuel. These substances are preferably post-combusted in a secondary combustion chamber before the flue gas reaches the solids separator.
  • Fines and other polluting gases and substances in the flue gas may be removed through a filter (i.e., flue gas filter).
  • a filter i.e., flue gas filter
  • the fuel is provided with at least one catalyst prior to introduction into the gasification zone.
  • the at least one catalyst can also be introduced directly into the gasification zone and / or combustion zone.
  • catalysts catalytic materials
  • the product gas composition can be optimized so that the tar content is lowered and the calorific value is increased.
  • a further aspect of the present invention relates to a device for producing a gas by gasification of fuels, in particular biogenic fuels and / or plastics, in a reactor comprising a gasification zone and a combustion zone, the reactor having a bed material fluidized by inflow of fluidizing gas via feed lines, which is conducted in the heated state via a line continuously from the combustion zone into the gasification zone and in the cooled state via a line from the gasification zone together with non-gasified residual fuel back into the combustion zone, wherein the fuel introduced via a line in the formed as a circulating fluidized bed gasification zone is the fuel in the circulating fluidized bed of the gasification zone at Heilab gleich to form a product gas at least partially degassed or gasified and the remaining or unreacted residual fuel z along with the cooled bed material is introduced via the line into the combustion zone where the bed material fluidizes to form a fast fluidized bed, reheated by combustion of the residual fuel and recycled via a line upstream of a separator into the circulating fluid
  • a post-combustion chamber is arranged after the separator and before the solids separator.
  • a flue gas filter is arranged after the solids separator.
  • the separator and / or the solids separator is preferably a centrifugal separator.
  • additional inlet nozzles for fluidizing gas are preferably provided for the provision of a moving bed.
  • the circulating fluidized bed is provided in the gasification zone of the reactor by means of suitable internals, such as baffles.
  • suitable internals such as baffles.
  • inlet nozzles for fluidizing gas are provided in the bottom region of the gasification zone of the reactor in the vicinity of the fuel feed and / or in the environment or in the line from the gasification zone into the combustion zone for the purpose of providing the moving bed.
  • the adequate circulation of the bed material is an essential part of the functionality of the process.
  • the transfer of the bed material from the gasification zone in the combustion zone is often done in practice via an inclined fluidized slide (here, the inclination angle of the slide is crucial), this is often a weak point in terms of material flow but also leakage of air into the gasification zone, which largely avoided must become.
  • suitable design of the inlet nozzles by the pulse of the incoming gas actively supports the flow of solids from the gasifier zone into the combustion zone and counteracts the leakage, both requirements can be met much better.
  • a device is also provided in which the gasification zone of the reactor has on the outlet side devices for separating dust formed in the gasification zone, the separated dust being transported via a guiding device inside the gasification zone into the circulating fluidized bed or into the moving bed.
  • the devices for separating dust formed in the gasification zone are selected from the group consisting of filtering separators, centrifugal separators and combinations thereof, and if metal or ceramic candle filters are used as filtering separators, which may be used for the Teerspaltung catalytically active materials are populated.
  • the internal separators may, as stated, be made differently and may, for example, operate on a centrifugal basis (e.g., cyclones) or as filtering separators (e.g., metallic or ceramic candle filters).
  • it is advisable to use catalytically active materials for the tar splitting which enables a significant tar reduction at suitable temperatures.
  • a combined particle and tar separation would be possible and it can downstream devices avoided and also the product gas can be easily cooled without fear of tar condensation.
  • Sand or catalytically active natural materials preferably calcite, dolomite or olivine or mixtures thereof may be used as the bed material.
  • nickel and / or zirconium compounds come into question.
  • Yet another aspect of the present invention relates to a process for producing a gas by gasification of fuels, particularly biogenic fuels and / or plastics, in a reactor comprising a gasification and a combustion zone, wherein the reactor comprises a fluidized bed material which is continuously heated Condition is passed from the combustion zone into the gasification zone and from the gasification zone in the cooled state together with non-gasified residual fuel back into the combustion zone, wherein the fuel is introduced into the formed as a circulating fluidized bed gasification zone, the fuel in the circulating fluidized bed of the gasification zone at Heilab gleich to form a product gas is at least partially degassed and gasified and the remaining or unreacted residual fuel is spent together with the cooled bed material in the combustion zone, where the bed material fluidized to form a fast fluidized bed, by combustion of the Residual fuel is reheated and recycled to the circulating fluidized bed of the gasification zone, characterized in that the catalyst is added before introduction into the gasification zone, a catalyst and / or a catalyst
  • the catalyst can be added directly to the fuel or, according to a particularly advantageous embodiment, introduced into the gasification zone and / or combustion zone, wherein the amounts of catalytic material can be adjusted depending on the fuel quantities supplied and the corresponding product gas composition and quality.
  • the product gas quality in particular its tar content and its calorific value, can be actively changed in order to achieve optimum system performance of the downstream system components. This makes it possible to optimize the performance of downstream machines.
  • the direct introduction of catalysts into the fluidized bed steam gasifier allows for the first time the regulation of the desired product gas quality or product gas composition for easier and more optimized further processing in a working machine or for conversion to pure methane in a so-called methanation plant.
  • the at least one catalyst comprises a material selected from the group consisting of quicklime CaO, calcium hydroxide Ca (OH) 2 , limestone powder CaCO 3 , nickel oxide NiO, fayalite Fe 2 SiO 4 , forsterite Mg 2 SiO 4 , iron (III) oxide Fe 2 O 3 and combinations thereof.
  • the catalyst is preferably introduced into the plant in solid form.
  • the catalyst in the form of a suspension.
  • the catalyst is preferably introduced via a metering device.
  • the dosing device can be controlled manually or automatically. In an automatic control, it is advantageous to analyze the composition of the product gas, and then to determine the amount of added catalyst.
  • a further aspect of the present invention relates to a device for producing a gas by gasification of fuels, in particular biogenic fuels and / or plastics, in a reactor comprising a gasification zone and a combustion zone, the reactor having a bed material fluidized by inflow of fluidizing gas via feed lines, which is conducted in the heated state via a line continuously from the combustion zone into the gasification zone and in the cooled state via a line from the gasification zone together with non-gasified residual fuel back into the combustion zone, wherein the fuel introduced via a line in the formed as a circulating fluidized bed gasification zone is the fuel in the circulating fluidized bed of the gasification zone at Heilab gleich to form a product gas at least partially degassed or gasified and the remaining or unreacted residual fuel z along with the cooled bed material is introduced via the line into the combustion zone, where the bed material is fluidized to form a fast fluidized bed, reheated by combustion of the residual fuel and returned via a line in the circulating fluidized bed in the gasification
  • the at least one feed line is arranged on a metering device.
  • Fig. 1 shows a flow diagram of the device according to the invention.
  • the gasification reactor 1 consists of a circulating fluidized bed in the gasification region, a moving bed, in which here the fuel is introduced, a connecting line 6 (here designed as a connection slide) between the gasification zone 2 and formed as a fast fluidized bed combustion zone 3 and another connecting line 5 with cyclone 8 and siphon 18th for the return of heated bed material in the gasification zone 2.
  • the fuel supply 15 takes place in the gasification zone 2, which can be adjusted by suitable fluidization of the fuel entry into the connecting chute 6.
  • the fluidization of the gasification fluidized bed is divided and can therefore be set differently.
  • a circulation of the bed material sets in a clockwise direction.
  • particles which tend to float are carried downwards and can thus be transported via the connecting chute 6 and further into the combustion zone 3.
  • internals eg baffles
  • inflow devices 4 there is fluidization in the connecting chute 6, via inflow devices 19 the fast fluidized bed is provided in the combustion zone 3 and for the return line 5 with siphon 18 the gas supply can be adjusted independently of each other so that the desired circulation of bed material between gasification zone 2 and combustion zone 3.
  • a particle separator may be provided, for example a candle filter with pulse cleaning.
  • a dust-free and tarry raw gas can be achieved even at higher fines in the fuel.
  • the separated particles can be introduced via a collecting line directly into the connecting chute 6 and thus transferred into the combustion zone 3. This prevents unwanted accumulation of fine ash particles in the gasification zone 2.
  • the fine particles are burned out and leave the reactor via the cyclone 8 of the combustion zone as fly ash.
  • the resulting in the combustion zone 3 flue gas is passed through a cyclone 8 and a Nachbrennsch 13 to a solids separator 10.
  • the solids separator from which bed material present in the flue gas is separated, is connected via a line 11 to the combustion zone 3 and / or a bed material container 7 and an ash container 20.
  • the flue gas leaving the solids separator 10 is cleaned by a flue gas filter 14.
  • the device according to the invention also has feed lines 16, with the aid of which catalysts or catalytic materials can be introduced into the gasification zone 2 and / or combustion zone 3.
  • feed lines 16 may be connected to a metering 17, the amount the catalyst to be entered controls.
  • the supply lines 16 may be connected via a screw conveyor 21 with a reservoir 22 for supporting the catalyst.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
EP12167075A 2009-03-19 2010-03-19 Procédé et dispositif de génération d'un gaz Withdrawn EP2487226A3 (fr)

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AT4442009A AT508002B1 (de) 2009-03-19 2009-03-19 Verfahren und vorrichtung zur erzeugung eines gases
EP10450045A EP2251399A3 (fr) 2009-03-19 2010-03-19 Procédé et dispositif destinés à la production d'une gaz

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CN108179032A (zh) * 2018-01-09 2018-06-19 新奥科技发展有限公司 一种流化床气化炉、煤气化系统及方法
CN112961705A (zh) * 2021-02-04 2021-06-15 中国华能集团清洁能源技术研究院有限公司 一种煤气化直接制甲烷/甲醇的气化炉
CN116042274B (zh) * 2023-03-07 2025-06-24 酒泉钢铁(集团)有限责任公司 一种高热值发生炉煤气生产工艺

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AT405937B (de) 1995-11-03 1999-12-27 Austrian Energy & Environment Verfahren zur erzeugung eines stickstoffarmen gases und vergasungsanlage

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AT509681B1 (de) 2016-06-15
EP2487226A3 (fr) 2012-08-22
AT508002B1 (de) 2010-10-15
EP2251399A3 (fr) 2011-05-18
AT508002A4 (de) 2010-10-15
EP2251399A2 (fr) 2010-11-17
AT509681A1 (de) 2011-10-15

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