EP2356200B1 - Method for thermochemically gasifying solid fuels - Google Patents

Method for thermochemically gasifying solid fuels Download PDF

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Publication number
EP2356200B1
EP2356200B1 EP09783675.3A EP09783675A EP2356200B1 EP 2356200 B1 EP2356200 B1 EP 2356200B1 EP 09783675 A EP09783675 A EP 09783675A EP 2356200 B1 EP2356200 B1 EP 2356200B1
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EP
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Prior art keywords
fuel
zone
gasification
gasifying
medium
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EP09783675.3A
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German (de)
French (fr)
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EP2356200A2 (en
Inventor
Klaus Weichselbaum
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Burkhardt GmbH
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Burkhardt GmbH
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Priority to HRP20180376TT priority Critical patent/HRP20180376T1/en
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    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02Fixed-bed gasification of lump fuel
    • C10J3/20Apparatus; Plants
    • C10J3/30Fuel charging devices
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02Fixed-bed gasification of lump fuel
    • C10J3/20Apparatus; Plants
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/48Apparatus; Plants
    • C10J3/482Gasifiers with stationary fluidised bed
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46Gasification of granular or pulverulent flues in suspension
    • C10J3/48Apparatus; Plants
    • C10J3/50Fuel charging devices
    • C10J3/503Fuel charging devices for gasifiers with stationary fluidised bed
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72Other features
    • C10J3/723Controlling or regulating the gasification process
    • CCHEMISTRY; METALLURGY
    • C10PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10JPRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00Details of gasification apparatus
    • C10J2200/15Details of feeding means
    • C10J2200/158Screws

Definitions

  • the present invention relates to a one-step process for the thermochemical gasification of solid fuels according to the principle of an ascending DC gasification.
  • the fuel is supplied to a gasification chamber against the force of gravity and flows through in the same direction by a gasification medium and an emerging product gas.
  • a corresponding gasifier for the thermochemical gasification of solid fuels has a gasification chamber and a fuel supply, which supplies the fuel against gravity to the gasification chamber and a supply for a gasification medium in the gasification chamber.
  • the carburetor has a top side arranged on the gasification chamber outlet for a product gas.
  • thermochemical gasification has been known for a long time in the prior art, and in connection with regenerative energy generation and waste and waste disposal, a great potential has been seen in gasification for a long time. Nevertheless, no such method has been able to establish itself on the market in large numbers until now.
  • a mixed form of a fixed bed gasifier is in the WO 97/01617 A1 shown.
  • the gasification takes place there in a mixed flow composed of countercurrent, direct current and crossflow.
  • the ash discharge takes place at the bottom of a grate.
  • a temperature profile is recorded via the height of the carburettor and, based on this, the position of the oxidation zone is set by moving the grate. Due to the moving grate and the process control in the mixed stream of the carburetor is structurally relatively expensive.
  • Descending DC gasifiers are operated in large numbers in the form of Imbert carburetor and similar devices during World War II and are used in this or slightly modified form for most of the smaller carburetor plants, as they deliver a low-tar gas. They are characterized in that the fuel sinks by gravity down and the carburetor from the gasification agent and product gas is also flowed through in this direction. They require coarse-grained fuel with a relatively narrow particle size distribution, since otherwise the underlying reduction zone is "blocked" by fines and thus is no longer permeable enough for the product gas. In addition, bridges and gas channels can form in oxidation and reduction zones, so that a fuel gas loaded with a high tar content is produced.
  • agitators or vibrators such as DE 197 55 700 C2 , where by means of a stirrer, the channel formation is to be prevented.
  • the EP 0 955 350 B1 suggests, however, by means of a swirl formation with the aid of the supplied air to prevent the passage of uncooked tar from the pyrolysis gas. Below the oxidation zone in this case a diaphragm is used, on which solid particles are to accumulate.
  • the DE 44 17 082 C1 describes an ascending DC gasifier with an air-cooled agitator to avoid channel and bridge formation.
  • the agitator simultaneously carries the ash out of the reaction vessel through a lateral opening by means of a rotary vane.
  • an afterburner chamber with secondary air supply above the pyrolysis zone is provided in order to crack the tar-charged pyrolysis gases and to deposit dust-like pyrolysis coke.
  • the DE 35 09 263 A1 also shows a fixed bed gasifier operating on the ascending DC method.
  • the fuel and the gasification agent are supplied to the carburetor from below.
  • a mixing device is provided in the gasification chamber in this carburetor. Both the oxidation zone and the reduction zone are formed in this gasifier layered in a fixed bed. Each zone is assigned its own mixer.
  • the EP 0 531 778 A1 shows another design of a DC gasifier, in which the fresh fuel is added from above and transported through an inner tube of a screw conveyor inside the carburetor down towards the carburetor bottom.
  • the inner tube also forms the pyrolysis zone.
  • the fuel exits and enters the lower outer region of the screw conveyor, where it passes through an oxidation process due to the gasification agent supplied there.
  • the screw conveyor the material is transported to the upper end of the screw, where it mixes with freshly supplied from above fuel. The reduction takes place during transport of the fuel from bottom to top. The withdrawal of the product gas takes place in a central region of the screw.
  • the object of the present invention is to provide a gasification process and a device which, with simple plant technology, enable the production of a low-tarry product gas.
  • a fuel is supplied to a gasification chamber contrary to gravity and flows through a gasification medium and a resulting product gas in the same direction.
  • Suitable fuels are all carbonaceous solids such as biomass, sewage sludge, plastics and the like.
  • a gasification space is provided, a fuel supply, which supplies the fuel against gravity to the gasification space and a supply for a gasification medium.
  • an outlet for a product gas is furthermore arranged.
  • the fuel is supplied to the gasification chamber continuously or at least quasi-continuously via a fuel feed in the gasifier bottom, that the gasification medium via a feed, which is arranged below in the gasification layer layer forming reaction zones, through the supplied fuel through a layer-forming Oxidation zone is supplied and in this case the amount of the supplied gasification medium is adjusted by a control unit such that in a reduction zone above the oxidation zone without additional fluidizing a stationary fluidized bed is formed.
  • the discharge of ash takes place only through the outlet for the product gas.
  • the fuel supply is in this case arranged in the carburetor bottom and preferably formed adjustable for continuous or quasi-continuous fuel supply.
  • the feed for the gasification medium is layered below itself in the gasification space Reaction zones arranged in order to achieve a uniform flow through the pyrolysis, oxidation and reduction zone, which forms substantially homogeneously.
  • a supply for another fluidizing means is not provided, and an ash discharging device is formed only through the outlet for the product gas and the exiting product gas.
  • the fuel in the gasification chamber is conveyed substantially homogeneously from bottom to top through the gasification space and flows through the gasification medium from below.
  • the fuel itself forms a distributor plate for producing a stationary fluidized bed.
  • the supplied amount of the gasification medium is in this case controllable by a control unit such that in the lower regions of the carburetor in the fuel supply and the pyrolysis zone is a fixed bed, in the overhead reduction zone, however, can form a fluidized bed.
  • This is made possible by the increase in volume of the gasification medium flowing through as a result of the strong rise in temperature in the oxidation zone and by the pyrolysis and combustion gases which form.
  • it is possible to carry out simultaneously without pyrolysis in a fixed bed and a coke gasification by reduction in a fluidized bed without using a mechanical Anström convinceds and without further fluidizing in the same reactor vessel, without mechanical separation.
  • the fuel as a distributor plate or the corresponding supply of the gasification medium, a stable over a wide range of air volume fluidized bed can be generated.
  • a substantially improved implementation of the pyrolysis coke formed in the oxidation zone in gas and fly ash is possible.
  • oxidation and reduction zone in this case a comparatively tarerarmes gas can be generated, which can be achieved by the continuous fuel supply and the almost complete implementation of the pyrolysis coke a very uniform quality of the gas.
  • the inventive method thus operates on the basic principle of an ascending DC gasification, which is combined with an integrated fluidized bed.
  • the resulting Ash is completely discharged by the exiting product gas. Due to the upper burnup and the almost complete material conversion, no further discharge devices for the ash are required.
  • the reduction zone above the oxidation zone is completely formed as a stationary fluidized bed.
  • the implementation of the fuel or the pyrolysis coke can be done in a favorable manner and in a short time.
  • the fuel in the gasification space is loosened contactless and mixed.
  • the loosening and mixing of the fuel is not actively mixing, but only passively, by continuously sufficient free-flowing, fresh fuel is supplied. Due to the uniform flow through the reaction zones and the introduction of the gasification medium from below through the fuel through the mixing and loosening is further supported.
  • the fuel is thereby kept constantly in motion, whereby a channel and bridging in the fuel can be avoided.
  • the method according to the invention it is therefore possible, without mechanical parts in the gasification space, which are always exposed to high loads, to achieve a tarerarmes gas uniform quality at a high efficiency.
  • Devices for conveying and / or mixing the fuel are in this case arranged exclusively outside the gasification space, so that there are no components in the temperature-loaded zones of the gasification space.
  • the carburetor can thus be operated with little interference and is exposed to little wear.
  • the structural complexity of such a carburetor is low.
  • additional mixing devices can also be used.
  • the method is preferably carried out in such a way that the fuel in the oxidation zone is burned from top to bottom at a substantially constant speed. This can be achieved by a corresponding continuous supply of the gasification medium, so that forms a layered oxidation zone at a constant ratio of the supply of the gasification medium and the fuel.
  • a pellet-shaped fuel is used as fuel, preferably wood pellets are used.
  • wood pellets are used.
  • the homogeneity and flowability of pelletized fuels enables a relatively simple carburetor design using simple conveyor technology and thus leads to cost-effective overall systems.
  • the extra cost over non-pelleted fuels is more than offset.
  • chips of small grain size are equally conceivable and suitable.
  • the gasification medium is supplied together with the fuel and flows successively through a pyrolysis zone, the oxidation zone and the reduction zone.
  • the feed for the gasification medium is preferably formed together with the fuel supply.
  • An embodiment with a separate feed for the gasification medium is also possible.
  • the supply of the gasification medium from the bottom takes place here as well, since this the mixing of the fuel is supported. Furthermore, the formation of channels and the trickling back of fines is prevented.
  • the gasifier is operable with different power.
  • the fuel is conveyed through the gasification space with the speed decreasing towards the top.
  • the gasification chamber has an upwardly widening cross-section. This ensures that the fuel is passed through the carburetor with the speed decreasing at the top. As a result, adaptation to the processes taking place at different speeds in the individual reaction zones is possible in a favorable manner.
  • the position of the oxidation zone in the gasification chamber always adjusts itself at the point where the combustion rate and the feed rate coincide.
  • the gasification chamber is surrounded by an insulation, preferably of ceramic fibers.
  • the thermal load of the carburetor outer wall can be reduced thereby.
  • the gasification medium and / or the fuel are preheated.
  • Part of the required process heat can thus be introduced into the process from the outside.
  • the required process heat can also be completely autothermal by substoichiometric combustion of a portion of the fuel.
  • At least one temperature sensor is arranged in the gasification space, which monitors the fill level of the gasification space. It is also advantageous if in the gasification room a plurality of sensors is arranged, which detect the position of the forming reaction zones, in particular the oxidation zone. Since in the method according to the invention, the individual reaction zones form very homogeneous and layered, they have significant temperature differences. The location of the reaction zones as well as the level in the gasification space can thereby be detected simply, inexpensively and without the arrangement of moving parts by temperature sensors.
  • a wall of the gasification chamber is made of a conventional steel. Due to the uniform flow through the reaction zones as well as the high material conversion in the fluidized bed, a low-tarry product gas can be produced in the device at comparatively low temperatures of approximately 850 ° C. There is a reducing atmosphere in the area of high temperatures. The structural complexity of the carburetor can thus be kept low by using a conventional steel. Special refractory lining, high temperature resistant steels or ceramics are not required.
  • the ash discharged with the product gas is separated from the product gas by means of a separation device. This can be accomplished by simple means, such as a cyclone separator.
  • the carburetor 1 has a fuel supply 2 in the carburetor bottom with a delivery unit 5 for the fuel.
  • a gasification chamber 3 is arranged, which has a variable cross-section in the example shown.
  • the gasification chamber 3 is frusto-conical and separated from the outer Vergaserwandung by an insulation 4.
  • a gas collecting chamber 12 is formed, in which the resulting gases 14 are collected and withdrawn through the outlet 7 arranged on the top side of the gasification chamber 3.
  • the carburettor 1 has a feed 6 for a gasification medium 16, which is in operative connection with a control unit 15.
  • the control unit 15 controls the amount of the gasification medium 16 fed in in such a way that a fluidized bed 17 is formed automatically without mechanical distributor bottoms in the gasification space and without additional fluidizing means.
  • FIG. 1 in this case shows a carburetor 1, in which the feed 6 for the gasification medium 16 is formed together with the feed 2 for the fuel 8.
  • the fuel 8 flows through from below from the gasification medium 16, so that the mixing of the fuel 8 is supported and a uniform distribution of the gasification medium 16 over the entire cross section is ensured.
  • the supply of the gasification medium 16 may also, as in FIG. 2 shown below the pyrolysis zone 9 laterally by an annular nozzle. Again, however, the supply of the gasification medium 16 through the fuel 8 passes through, thereby mixing the fuel. 8 and uniform distribution of the gasification medium 16 to achieve. Additional mechanical mixing devices are therefore not required. In addition, this can prevent fines from the overhead reaction zones 9, 10, 11 from entering the fuel 8.
  • the fuel 8 is continuously or quasi-continuous against gravity, i. the same amount of fuel per unit time, pressed by the fuel supply 2 into the gasification chamber 3 and promoted by the carburetor 1.
  • the fuel 8 in this case flows through the gasification medium 16 and product gas 14 in the same direction. It is therefore in this respect an ascending DC gasification.
  • a gasification medium 16 is advantageously used preheated air.
  • the process can also be completely autothermic.
  • the combustion of the fuel 8 takes place from top to bottom, with a layer-shaped oxidation zone 10 is formed at a suitable constant ratio of air supply to fuel.
  • temperatures of about 800 ° C is formed below the same also a layered pyrolysis zone 9, in which decomposes the fuel 8 at temperatures around 500 ° C in pyrolysis and gaseous compounds.
  • the gas-air mixture formed in the pyrolysis zone 9 by the air 16 flowing through the fuel 8 from below through the fuel 8 maintains the energy production in the oxidation zone 10, where a part of these gases and the pyrolysis coke burns.
  • the remaining pyrolysis coke formed in the pyrolysis zone 9 gradually migrates upwards through the oxidation zone 10 and forms a reduction zone 11 above it.
  • the presentation of the FIG. 2 shows a process in which the reduction zone 11 is formed substantially completely in the form of a fluidized bed 17. In this way, a particularly good and rapid implementation of the pyrolysis coke can be achieved.
  • a method according to FIG. 1 possible, wherein the reduction zone 11 above the oxidation zone 10 is first formed in layers. In the upper region of the gasification space, however, the reduction zone 11 is present as a fluidized bed 17. In each case, the gasification is carried out according to the principle of an ascending DC gasification, which, however, according to the invention is combined with an integrated fluidized bed 17 in the reduction zone 11.
  • the pyrolysis coke is flowed through, inter alia, by CO 2 and H 2 O from the pyrolysis zone 9 and the oxidation zone 10, these being reduced endothermically to the combustible gases CO and H 2 , whereby the pyrolysis coke is gasified.
  • the resulting gas pressure causes the pyrolysis coke to be raised and thereby loosened. It forms according to the invention by the appropriate adjustment of the supplied amount of the gasification medium 16 and the flow of the fuel 8 from below an equilibrium between the gas pressure and the weight of the pyrolysis coke up to the fluidized bed.
  • the fuel 8 forms by its continuous För-tion with appropriate control of the supply of the gasification medium 16 a distributor plate for fluidized bed production.
  • the fluidized bed 17 can be produced without further fluidizing agent. This makes it possible to almost completely convert the pyrolysis coke formed in the oxidation zone 10 to gas and fly ash and thus to achieve a high degree of efficiency of the overall process. It has been shown that the fluidized bed 17 is stable in the carburetor 1 over a relatively wide range of air volumes and thus the regulation of the amount of air through the control unit 15 is easily possible to the necessary for the thermochemical gasification air rates.
  • the resulting ash is preferably discharged as fly ash without additional discharge devices with the process gas 14 and then separated from the product gas 14 by simple means, for example by a cyclone separator. Due to the upper burnup in the method according to the invention and the guidance of the gasification medium 16 and the product gas 14 through the carburetor 1 and the good implementation of the fuel 8, the product gas 14 with the outlet 7 as discharge devices for the ash is completely sufficient. If, however, excess pyrolysis coke is produced or intentionally generated, this can likewise be taken off together with the resulting dusty ash with the product gas 14.
  • the uniform flow through the very homogeneously forming pyrolysis, oxidation and reduction zones 9, 10, 11 leads to the production of a tarry gas of very uniform quality at comparatively low temperatures of about 850 ° C. in the oxidation zone 10 possible to carry out a carburetor 1 without the use of special high-temperature resistant steels or ceramics.
  • Even conventional structural steel can be used, since there is no appreciable oxidation due to the reducing atmosphere of the substoichiometric combustion.
  • the avoidance of the usual in the prior art ceramic components also leads due to low heat capacity advantageously too short heating and cooling times when starting and stopping the carburetor. 1
  • a preferred embodiment of a carburetor 1 has, as shown in the example, an upwardly widening cross-section of the gasification chamber 3. This allows operation with different power, because it causes the fuel 8 to move upwards through the carburetor 1 with decreasing speed.
  • the burning down to be carried out in the oxidation zone 10 at a substantially constant speed now leads to a self-regulating setting of a stable operating point at which the oxidation zone 10 remains at the point where the burning rate and feed rate of the fuel 8 coincide.
  • the continuous or quasi-continuous supply of new fuel 8, in particular in conjunction with the changing cross-section of the gasification chamber 3, ensures constant movement and thorough mixing of the material and thus prevents channeling and bridge formation in the oxidation and reduction zones 10, 11 without further mechanical devices.
  • a plurality of superimposed temperature sensors 13 is further arranged, which cooperate with the control unit 15 and the level of the gasification chamber 3 and the position of the reaction zones (9, 10, 11) detect by measurement.
  • the boundaries between the fuel 8 and the pyrolysis and oxidation zone (9, 10) and between the reduction zone (11) and the overlying gas collection chamber (12) are characterized by significant temperature differences due to the very homogeneous formation in the inventive method and the carburetor ,
  • the control technology important location of the reaction zones 9, 10, 11, in particular the oxidation zone 10, and the filling level can thus be detected in a simple manner cost and without moving parts.
  • a carburetor 1 manages without moving parts in the hot area and has no mechanically loaded hot parts, which often constitute a source of interference in the prior art.
  • the carburetor 1 according to the invention finds by self-regulating properties with low mechanical and / or electronic control effort a stable operating point and thus provides a durable tarerarmes product gas with only slightly fluctuating quality. Channel and bridge formation as well as tar slippage can be avoided.
  • the carburetor 1 is therefore particularly suitable for small and medium sized systems up to about 1 MW electrically, since no complex gas aftertreatment is required. It is also possible to directly produce a motorable product gas. Furthermore, the production of charcoal is possible by means of the device with appropriate process control.
  • the fuel used 8 need not be coarse and may contain high amounts of fines, since the process control a tendency to clog is avoided. Thus, fuels 8 which are available in sufficient quantity on the market can be used.
  • the carburetor 1 Due to the simple structural design and a simple control technology by means of the control unit 15, the carburetor 1 can also be manufactured and operated inexpensively.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Treatment Of Sludge (AREA)

Description

Die vorliegende Erfindung betrifft ein einstufiges Verfahren zum thermochemischen Vergasen fester Brennstoffe nach dem Prinzip einer aufsteigenden Gleichstromvergasung. Der Brennstoff wird bei diesem Verfahren entgegen der Schwerkraft einem Vergasungsraum zugeführt und von einem Vergasungsmedium und einem entstehenden Produktgas in gleicher Richtung durchströmt. Ein entsprechender Vergaser zum thermochemischen Vergasen fester Brennstoffe weist einen Vergasungsraum und eine Brennstoffzuführung auf, welche den Brennstoff entgegen der Schwerkraft dem Vergasungsraum zuführt sowie eine Zuführung für ein Vergasungsmedium in den Vergasungsraum. Weiterhin weist der Vergaser einen oberseitig an dem Vergasungsraum angeordneten Auslass für ein Produktgas auf.The present invention relates to a one-step process for the thermochemical gasification of solid fuels according to the principle of an ascending DC gasification. In this method, the fuel is supplied to a gasification chamber against the force of gravity and flows through in the same direction by a gasification medium and an emerging product gas. A corresponding gasifier for the thermochemical gasification of solid fuels has a gasification chamber and a fuel supply, which supplies the fuel against gravity to the gasification chamber and a supply for a gasification medium in the gasification chamber. Furthermore, the carburetor has a top side arranged on the gasification chamber outlet for a product gas.

Verfahren der thermochemischen Vergasung sind im Stand der Technik seit langem bekannt, wobei in Zusammenhang mit der regenerativen Energieerzeugung sowie der Abfall- und Reststoffentsorgung seit längerem ein großes Potential in der Vergasung gesehen wird. Dennoch konnte sich bis jetzt kein derartiges Verfahren in größeren Stückzahlen am Markt etablieren.Methods of thermochemical gasification have been known for a long time in the prior art, and in connection with regenerative energy generation and waste and waste disposal, a great potential has been seen in gasification for a long time. Nevertheless, no such method has been able to establish itself on the market in large numbers until now.

Wirbelschichtvergaser nach dem Stand der Technik bedingen eine relativ komplexe Anlagentechnik und der Teergehalt der produzierten Gase macht für die meisten Anwendungen eine weitere, aufwändige Gasreinigung nötig. Sie werden daher üblicherweise nur für Anlagengrößen größer 1 MW elektrisch eingesetzt.State-of-the-art fluidized bed gasifiers require relatively complex plant technology, and the tar content of the gases produced necessitates a further, complicated gas purification for most applications. They are therefore usually used electrically only for plant sizes greater than 1 MW.

Aus der DE 1 017 314 B ist ein Wirbelschichtvergaser bekannt, der den Abzug von Schlacke und Asche als Schmelze und damit ohne mechanische Einbauten erlaubt. Dazu weist er im unteren Bereich eine sehr heiße, schwach bewegte und im oberen Bereich eine kühlere, stark bewegte Wirbelschicht auf. Dieses Verfahren ist jedoch bei Anlagen kleiner Leistung unwirtschaftlich, da es zweierlei Vergasungsmittel benötigt: reinen Sauerstoff für die untere Zone und Wasserdampf für die obere Zone. Durch die Zuführung des Sauerstoffs in der unteren, schwach bewegten Zone bildet sich dort eine Oxidationszone aus. Der Brennstoff wird im Wesentlichen oberhalb der Oxidationszone, teilweise auch im Bereich der Wirbelschicht, zugeführt und wird dabei durch die stark bewegte Wirbelschicht verteilt und bewegt. Die Pyrolyse und die Reduktion finden somit gleichzeitig im gesamten oberen Bett statt. Der Teergehalt der erzeugten Gase ist daher auch hier relativ hoch. Auf Grund der hohen Temperaturen von bis zu 1500°C ist zudem eine aufwändige Feuerfestauskleidung erforderlich.From the DE 1 017 314 B is known a fluidized bed gasifier, which allows the withdrawal of slag and ash as a melt and thus without mechanical installations. For this he has a very hot at the bottom, weakly moving and in the upper part a cooler, strongly moving fluidized bed. However, this process is uneconomical for low power plants because it requires two types of gasification: pure oxygen for the lower zone and water vapor for the upper zone. By supplying the oxygen in the lower, weakly moving zone, an oxidation zone is formed there. The fuel is supplied essentially above the oxidation zone, partly also in the area of the fluidized bed, and is thereby distributed and moved by the strongly moving fluidized bed. The pyrolysis and the reduction thus take place simultaneously in the entire upper bed. The tar content of the gases produced is therefore relatively high here as well. Due to the high temperatures of up to 1500 ° C, an elaborate refractory lining is required.

Festbettvergaser werden gewöhnlich in Gegenstrom- und Gleichstromvergaser unterteilt, Kreuzstromvergaser und Doppelfeuervergaser stellen die häufigsten Misch- und Sonderformen dar, kämpfen aber im Wesentlichen mit den gleichen Problemen wie die beiden Grundformen. Die Gegenstromvergaser haben zwar einen sehr guten Wirkungsgrad, sind aber wegen der extremen Teerbeladung des Produktgases für kleine und mittlere Anlagen völlig ungeeignet.Fixed bed gasifiers are usually subdivided into countercurrent and direct current gasifiers, cross flow gasifiers and double fire gasifiers are the most common mixing and special forms, but essentially have the same problems as the two basic forms. Although the countercurrent carburetors have a very good efficiency, but are due to the extreme Teerbeladung the product gas for small and medium-sized systems completely unsuitable.

Eine Mischform eines Festbettvergasers ist in der WO 97/01617 A1 gezeigt. Die Vergasung erfolgt dort in einem aus Gegenstrom, Gleichstrom und Querstrom zusammengesetzten Gemischtstrom. Der Ascheaustrag erfolgt am unteren Ende eines Rostes. Zur Regelung des Prozesses wird über die Höhe des Vergasers ein Temperaturprofil aufgenommen und darauf basierend durch Bewegung des Rostes die Lage der Oxidationszone eingestellt. Aufgrund des bewegten Rostes sowie der Prozessführung im Gemischtstrom ist der Vergaser konstruktiv vergleichsweise aufwendig.A mixed form of a fixed bed gasifier is in the WO 97/01617 A1 shown. The gasification takes place there in a mixed flow composed of countercurrent, direct current and crossflow. The ash discharge takes place at the bottom of a grate. To control the process, a temperature profile is recorded via the height of the carburettor and, based on this, the position of the oxidation zone is set by moving the grate. Due to the moving grate and the process control in the mixed stream of the carburetor is structurally relatively expensive.

Absteigende Gleichstromvergaser sind in Form des Imbertvergasers und ähnlicher Geräte während des 2. Weltkrieges in großen Stückzahlen betrieben worden und werden in dieser oder leicht abgewandelter Form für die meisten kleineren Vergaseranlagen eingesetzt, da sie ein teerarmes Gas liefern. Sie sind dadurch gekennzeichnet, dass der Brennstoff durch die Schwerkraft nach unten sinkt und der Vergaser vom Vergasungsmittel und Produktgas ebenfalls in dieser Richtung durchströmt wird. Sie erfordern grobstückigen Brennstoff mit relativ enger Korngrößenverteilung, da sonst die untenliegende Reduktionszone durch Feinanteile "verstopft" und damit für das Produktgas nicht mehr durchlässig genug ist. Zudem kann es zu einer Bildung von Brücken und Gaskanälen in Oxidations- und Reduktionszonen kommen, so dass ein mit einem hohen Teergehalt belastetes Brenngas erzeugt wird.Descending DC gasifiers are operated in large numbers in the form of Imbert carburetor and similar devices during World War II and are used in this or slightly modified form for most of the smaller carburetor plants, as they deliver a low-tar gas. They are characterized in that the fuel sinks by gravity down and the carburetor from the gasification agent and product gas is also flowed through in this direction. They require coarse-grained fuel with a relatively narrow particle size distribution, since otherwise the underlying reduction zone is "blocked" by fines and thus is no longer permeable enough for the product gas. In addition, bridges and gas channels can form in oxidation and reduction zones, so that a fuel gas loaded with a high tar content is produced.

Zur Behebung dieser Probleme verwenden zahlreiche Erfindungen Rührwerke oder Vibratoren, wie z.B. DE 197 55 700 C2 , wo mittels eines Rührwerkes die Kanalbildung verhindert werden soll. Die EP 0 955 350 B1 schlägt hingegen vor, mittels einer Drallbildung mit Hilfe der zugeführten Luft das Durchleiten ungecrackten Teers aus dem Pyrolysegas zu verhindern. Unterhalb der Oxidationszone wird hierbei ein Diaphragma eingesetzt, an welchem sich feste Partikel ansammeln sollen.To overcome these problems, numerous inventions use agitators or vibrators, such as DE 197 55 700 C2 , where by means of a stirrer, the channel formation is to be prevented. The EP 0 955 350 B1 suggests, however, by means of a swirl formation with the aid of the supplied air to prevent the passage of uncooked tar from the pyrolysis gas. Below the oxidation zone in this case a diaphragm is used, on which solid particles are to accumulate.

Weiterhin sind aufsteigende Gleichstromvergaser bekannt, bei welchen der Brennstoff von unten zugeführt wird. Auch hier kann es zu einer Kanal- und Brückenbildung und zu Problemen durch die Teerbeladung des Produktgases kommen.Furthermore, ascending direct current gasifiers are known in which the fuel is supplied from below. Again, it may lead to channel and bridge formation and problems due to the Teerbeladung of the product gas.

Die DE 44 17 082 C1 beschreibt einen aufsteigenden Gleichstromvergaser mit einem luftgekühlten Rührwerk zur Vermeidung von Kanal- und Brückenbildung. Das Rührwerk trägt mittels eines Drehflügels gleichzeitig die Asche durch eine seitliche Öffnung aus dem Reaktionsbehälter aus. Weiterhin ist eine Nachverbrennungskammer mit Sekundärluftzuführung oberhalb der Pyrolysezone vorgesehen, um die teerbeladenen Pyrolysegase zu cracken und staubförmigen Pyrolysekoks abzuscheiden.The DE 44 17 082 C1 describes an ascending DC gasifier with an air-cooled agitator to avoid channel and bridge formation. The agitator simultaneously carries the ash out of the reaction vessel through a lateral opening by means of a rotary vane. Furthermore, an afterburner chamber with secondary air supply above the pyrolysis zone is provided in order to crack the tar-charged pyrolysis gases and to deposit dust-like pyrolysis coke.

Die DE 35 09 263 A1 zeigt ebenfalls einen Festbettvergaser, der nach dem aufsteigenden Gleichstromverfahren arbeitet. Der Brennstoff sowie das Vergasungsmittel werden dem Vergaser dabei von unten zugeführt. Um eine gleichmäßige Verbrennung und Vergasung des Brennstoffs zu erreichen und Verbackungen und Kanalbildung zu vermeiden, ist bei diesem Vergaser eine Mischeinrichtung im Vergasungsraum vorgesehen. Sowohl die Oxidationszone als auch die Reduktionszone sind bei diesem Vergaser schichtförmig im Festbett ausgebildet. Jeder Zone ist jeweils ein eigener Mischer zugeordnet.The DE 35 09 263 A1 also shows a fixed bed gasifier operating on the ascending DC method. The fuel and the gasification agent are supplied to the carburetor from below. In order to achieve a uniform combustion and gasification of the fuel and to avoid caking and channeling, a mixing device is provided in the gasification chamber in this carburetor. Both the oxidation zone and the reduction zone are formed in this gasifier layered in a fixed bed. Each zone is assigned its own mixer.

Die EP 0 531 778 A1 zeigt eine andere Bauform eines Gleichstromvergasers, bei welchem der frische Brennstoff von oben zugegeben wird und durch ein Innenrohr einer Förderschnecke im Inneren des Vergasers nach unten in Richtung Vergaserboden transportiert wird. Das Innenrohr bildet dabei zugleich auch die Pyrolysezone aus. Am unteren Ende des Innenrohres tritt der Brennstoff aus und gelangt in den unteren Außenbereich der Förderschnecke, dort durchläuft es aufgrund des dort zugeführten Vergasungsmittels einen Oxidationsprozess. Durch die Förderschnecke wird das Material an das obere Ende der Schnecke befördert, wo es sich mit frisch von oben zugeführtem Brennstoff vermischt. Die Reduktion findet dabei während des Transports des Brennstoffs von unten nach oben statt. Der Abzug des Produktgases erfolgt in einem mittleren Bereich der Schnecke.The EP 0 531 778 A1 shows another design of a DC gasifier, in which the fresh fuel is added from above and transported through an inner tube of a screw conveyor inside the carburetor down towards the carburetor bottom. At the same time, the inner tube also forms the pyrolysis zone. At the lower end of the inner tube, the fuel exits and enters the lower outer region of the screw conveyor, where it passes through an oxidation process due to the gasification agent supplied there. By the screw conveyor, the material is transported to the upper end of the screw, where it mixes with freshly supplied from above fuel. The reduction takes place during transport of the fuel from bottom to top. The withdrawal of the product gas takes place in a central region of the screw.

Bauteile im Bereich der Oxidationszone sind hohen thermischen Belastungen sowie einem starken Verschleiß ausgesetzt. Zudem sind Einbauten bei Temperaturen deutlich über 1.000°C teuer und besitzen eine geringe Lebenserwartung.Components in the area of the oxidation zone are exposed to high thermal loads and heavy wear. In addition, internals are expensive at temperatures well above 1,000 ° C and have a low life expectancy.

Die Aufgabe der vorliegenden Erfindung ist es, ein Vergasungsverfahren und eine Vorrichtung zur Verfügung zu stellen, welche bei einfacher Anlagentechnik die Erzeugung eines teerarmen Produktgases ermöglichen.The object of the present invention is to provide a gasification process and a device which, with simple plant technology, enable the production of a low-tarry product gas.

Die Aufgabe wird durch die Merkmale des unabhängigen Patentanspruchs 1 gelöst. Vorteilhafte Ausgestaltungen der Erfindung sind in den jeweiligen Unteransprüchen beschrieben.The object is solved by the features of independent claim 1. Advantageous embodiments of the invention are described in the respective subclaims.

Bei einem einstufigen Verfahren zum thermochemischen Vergasen fester Brennstoffe nach dem Prinzip einer aufsteigenden Gleichstromvergasung wird ein Brennstoff entgegen der Schwerkraft einem Vergasungsraum zugeführt und von einem Vergasungsmedium und einem entstehenden Produktgas in gleicher Richtung durchströmt. Als Brennstoffe kommen hierbei sämtliche kohlenstoffhaltige Feststoffe wie Biomasse, Klärschlamm, Kunststoffe und dgl. in Frage. Bei einem einstufigen Vergaser ist ein Vergasungsraum vorgesehen, eine Brennstoffzuführung, welche den Brennstoff entgegen der Schwerkraft dem Vergasungsraum zuführt sowie eine Zuführung für ein Vergasungsmedium. Oberseitig an dem Vergasungsraum ist weiterhin ein Auslass für ein Produktgas angeordnet. Erfindungsgemäß ist nun vorgesehen, dass der Brennstoff dem Vergasungsraum kontinuierlich oder zumindest quasikontinuierlich über eine Brennstoffzuführung im Vergaserboden zugeführt wird, dass das Vergasungsmedium über eine Zuführung, welche unterhalb von sich im Vergasungsraum schichtförmig ausbildenden Reaktionszonen angeordnet ist, durch den zugeführten Brennstoff hindurch einer sich schichtförmig ausbildenden Oxidationszone zugeführt wird und hierbei die Menge des zugeführten Vergasungsmediums durch eine Regeleinheit derart eingestellt wird, dass in einer Reduktionszone oberhalb der Oxidationszone ohne zusätzliche Fluidisierungsmittel eine stationäre Wirbelschicht ausgebildet wird. Der Austrag von Asche erfolgt dabei lediglich durch den Auslass für das Produktgas.In a one-step process for the thermochemical gasification of solid fuels according to the principle of ascending DC gasification, a fuel is supplied to a gasification chamber contrary to gravity and flows through a gasification medium and a resulting product gas in the same direction. Suitable fuels here are all carbonaceous solids such as biomass, sewage sludge, plastics and the like. In question. In a single-stage gasifier, a gasification space is provided, a fuel supply, which supplies the fuel against gravity to the gasification space and a supply for a gasification medium. On the upper side of the gasification chamber, an outlet for a product gas is furthermore arranged. According to the invention, it is now provided that the fuel is supplied to the gasification chamber continuously or at least quasi-continuously via a fuel feed in the gasifier bottom, that the gasification medium via a feed, which is arranged below in the gasification layer layer forming reaction zones, through the supplied fuel through a layer-forming Oxidation zone is supplied and in this case the amount of the supplied gasification medium is adjusted by a control unit such that in a reduction zone above the oxidation zone without additional fluidizing a stationary fluidized bed is formed. The discharge of ash takes place only through the outlet for the product gas.

Die Brennstoffzuführung ist hierbei im Vergaserboden angeordnet und vorzugsweise regelbar zur kontinuierlichen oder quasikontinuierlichen Brennstoffzufuhr ausgebildet. Bei dem Vergaser ist die Zuführung für das Vergasungsmedium unterhalb von sich im Vergasungsraum schichtförmig ausbildenden Reaktionszonen angeordnet, um eine gleichmäßige Durchströmung der sich im Wesentlichen homogen ausbildenden Pyrolyse-, Oxidations- und Reduktionszone zu erzielen. Eine Zuführung für ein weiteres Fluidisierungsmittel ist nicht vorgesehen und eine Ascheaustragvorrichtung ist lediglich durch den Auslass für das Produktgas und das austretende Produktgas gebildet. Durch die kontinuierliche Zuführung des Brennstoffes wird der Brennstoff in dem Vergasungsraum weitgehend homogen von unten nach oben durch den Vergasungsraum gefördert und durch das Vergasungsmedium von unten angeströmt. Der Brennstoff selbst bildet hierdurch einen Anströmboden zur Erzeugung einer stationären Wirbelschicht. Die zugeführte Menge des Vergasungsmediums ist hierbei durch eine Regeleinheit derart regelbar, dass in den unteren Bereichen des Vergasers in der Brennstoffzuführung und der Pyrolysezone ein Festbett vorliegt, in der oben liegenden Reduktionszone sich jedoch eine Wirbelschicht ausbilden kann. Dies wird ermöglicht durch die Volumenvergrößerung des durchströmenden Vergasungsmediums in Folge des starken Temperaturanstiegs in der Oxidationszone und durch die sich bildenden Pyrolyse- und Verbrennungsgase. So ist es möglich, ohne Verwendung eines mechanischen Anströmbodens und ohne weitere Fluidisierungsmittel im gleichen Reaktorgefäß, ohne mechanische Trennung, gleichzeitig eine Pyrolyse im Festbett und eine Koksvergasung durch Reduktion im Fließbett durchzuführen. Durch die Verwendung des Brennstoffes als Anströmboden bzw. die entsprechende Zuführung des Vergasungsmediums kann eine über einen breiten Luftmengenbereich stabile Wirbelschicht erzeugt werden. Hierdurch ist eine wesentlich verbesserte Umsetzung des in der Oxidationszone gebildeten Pyrolysekokses in Gas und Flugasche möglich. Durch die gleichmäßige Durchströmung der Pyrolyse-, Oxidations- und Reduktionszone kann hierbei ein vergleichsweise teerarmes Gas erzeugt werden, wobei durch die kontinuierliche Brennstoffzufuhr und die nahezu vollständige Umsetzung des Pyrolysekokses eine sehr gleichmäßige Qualität des Gases erzielt werden kann. Das erfindungsgemäße Verfahren arbeitet somit nach dem Grundprinzip einer aufsteigenden Gleichstromvergasung, welches kombiniert ist mit einer integrierten Wirbelschicht. Die entstehende Asche wird hierbei vollständig durch das austretende Produktgas ausgetragen. Durch den oberen Abbrand und die nahezu vollständige Stoffumsetzung sind keine weiteren Austragvorrichtungen für die Asche erforderlich.The fuel supply is in this case arranged in the carburetor bottom and preferably formed adjustable for continuous or quasi-continuous fuel supply. In the case of the gasifier, the feed for the gasification medium is layered below itself in the gasification space Reaction zones arranged in order to achieve a uniform flow through the pyrolysis, oxidation and reduction zone, which forms substantially homogeneously. A supply for another fluidizing means is not provided, and an ash discharging device is formed only through the outlet for the product gas and the exiting product gas. As a result of the continuous supply of the fuel, the fuel in the gasification chamber is conveyed substantially homogeneously from bottom to top through the gasification space and flows through the gasification medium from below. As a result, the fuel itself forms a distributor plate for producing a stationary fluidized bed. The supplied amount of the gasification medium is in this case controllable by a control unit such that in the lower regions of the carburetor in the fuel supply and the pyrolysis zone is a fixed bed, in the overhead reduction zone, however, can form a fluidized bed. This is made possible by the increase in volume of the gasification medium flowing through as a result of the strong rise in temperature in the oxidation zone and by the pyrolysis and combustion gases which form. Thus, it is possible to carry out simultaneously without pyrolysis in a fixed bed and a coke gasification by reduction in a fluidized bed without using a mechanical Anströmbodens and without further fluidizing in the same reactor vessel, without mechanical separation. By using the fuel as a distributor plate or the corresponding supply of the gasification medium, a stable over a wide range of air volume fluidized bed can be generated. As a result, a substantially improved implementation of the pyrolysis coke formed in the oxidation zone in gas and fly ash is possible. By the uniform flow through the pyrolysis, oxidation and reduction zone in this case a comparatively tarerarmes gas can be generated, which can be achieved by the continuous fuel supply and the almost complete implementation of the pyrolysis coke a very uniform quality of the gas. The inventive method thus operates on the basic principle of an ascending DC gasification, which is combined with an integrated fluidized bed. The resulting Ash is completely discharged by the exiting product gas. Due to the upper burnup and the almost complete material conversion, no further discharge devices for the ash are required.

Nach einer vorteilhaften Ausführung der Erfindung wird die Reduktionszone oberhalb der Oxidationszone vollständig als stationäre Wirbelschicht ausgebildet. Die Umsetzung des Brennstoffes bzw. des Pyrolysekokses kann hierdurch in günstiger Weise und in kurzer Zeit erfolgen.According to an advantageous embodiment of the invention, the reduction zone above the oxidation zone is completely formed as a stationary fluidized bed. The implementation of the fuel or the pyrolysis coke can be done in a favorable manner and in a short time.

Vorteilhafterweise wird der Brennstoff in dem Vergasungsraum berührungslos aufgelockert und durchmischt. Die Auflockerung und Durchmischung des Brennstoffes erfolgt nicht aktiv vermischend, sondern ausschließlich passiv, indem kontinuierlich hinreichend rieselfähiger, frischer Brennstoff zugeführt wird. Durch die gleichmäßige Durchströmung der Reaktionszonen und die Einleitung des Vergasungsmediums von unten durch den Brennstoff hindurch wird die Vermischung und Auflockerung weiter unterstützt.Advantageously, the fuel in the gasification space is loosened contactless and mixed. The loosening and mixing of the fuel is not actively mixing, but only passively, by continuously sufficient free-flowing, fresh fuel is supplied. Due to the uniform flow through the reaction zones and the introduction of the gasification medium from below through the fuel through the mixing and loosening is further supported.

Der Brennstoff wird hierdurch ständig in Bewegung gehalten, wodurch eine Kanal- und Brückenbildung im Brennstoff vermieden werden kann. Mittels des erfindungsgemäßen Verfahrens gelingt es daher, ohne mechanische Teile im Vergasungsraum, welche stets hohen Belastungen ausgesetzt sind, ein teerarmes Gas gleichmäßiger Qualität bei einem hohen Wirkungsgrad zu erzielen.The fuel is thereby kept constantly in motion, whereby a channel and bridging in the fuel can be avoided. By means of the method according to the invention it is therefore possible, without mechanical parts in the gasification space, which are always exposed to high loads, to achieve a tarerarmes gas uniform quality at a high efficiency.

Vorrichtungen zur Förderung und/oder Durchmischung des Brennstoffes sind hierbei ausschließlich außerhalb des Vergasungsraumes angeordnet, so dass in den temperaturbelasteten Zonen des Vergasungsraumes keine Bauteile liegen. Der Vergaser kann hierdurch störungsarm betrieben werden und ist nur geringem Verschleiß ausgesetzt. Zudem ist der bauliche Aufwand eines derartigen Vergasers gering. Je nach Art des verwendeten Brennstoffes können jedoch auch zusätzliche Mischeinrichtungen verwendet werden.Devices for conveying and / or mixing the fuel are in this case arranged exclusively outside the gasification space, so that there are no components in the temperature-loaded zones of the gasification space. The carburetor can thus be operated with little interference and is exposed to little wear. In addition, the structural complexity of such a carburetor is low. Depending on the type of fuel used, however, additional mixing devices can also be used.

Vorzugsweise wird das Verfahren hierbei derart geführt, dass der Brennstoff in der Oxidationszone mit im Wesentlichen konstanter Geschwindigkeit von oben nach unten verbrannt wird. Dies kann durch eine entsprechende kontinuierliche Zuführung des Vergasungsmediums erzielt werden, so dass sich bei einem gleichbleibenden Verhältnis der Zufuhr des Vergasungsmediums und des Brennstoffes eine schichtförmige Oxidationszone ausbildet.The method is preferably carried out in such a way that the fuel in the oxidation zone is burned from top to bottom at a substantially constant speed. This can be achieved by a corresponding continuous supply of the gasification medium, so that forms a layered oxidation zone at a constant ratio of the supply of the gasification medium and the fuel.

Weiterhin ist es vorteilhaft, wenn als Brennstoff ein pelletförmiger Brennstoff verwendet wird, wobei vorzugsweise Holzpellets zum Einsatz kommen. Insbesondere mit Holzpellets steht ein genormter Brennstoff mit definierten Eigenschaften zur Verfügung, der in großer Menge am Markt verfügbar ist. Die Homogenität und Rieselfähigkeit pelletierter Brennstoffe ermöglicht eine relativ einfache Vergaserkonstruktion unter Verwendung einfacher Fördertechnik und führt so zu kostengünstigen Gesamtanlagen. Der Mehrpreis gegenüber nicht pelletierten Brennstoffen wird damit mehr als wett gemacht. Hackschnitzel kleiner Körnung sind jedoch ebenso denkbar und geeignet.Furthermore, it is advantageous if a pellet-shaped fuel is used as fuel, preferably wood pellets are used. Especially with wood pellets is a standardized fuel with defined properties available, which is available in large quantities on the market. The homogeneity and flowability of pelletized fuels enables a relatively simple carburetor design using simple conveyor technology and thus leads to cost-effective overall systems. The extra cost over non-pelleted fuels is more than offset. However, chips of small grain size are equally conceivable and suitable.

Vorzugsweise wird das Vergasungsmedium gemeinsam mit dem Brennstoff zugeführt und durchströmt nacheinander eine Pyrolysezone, die Oxidationszone und die Reduktionszone. Bei einer Vorrichtung zum Vergasen fester Brennstoffe ist die Zuführung für das Vergasungsmedium vorzugsweise gemeinsam mit der Brennstoffzuführung ausgebildet.Preferably, the gasification medium is supplied together with the fuel and flows successively through a pyrolysis zone, the oxidation zone and the reduction zone. In a device for gasifying solid fuels, the feed for the gasification medium is preferably formed together with the fuel supply.

Eine Ausführung mit einer getrennten Zuführung für das Vergasungsmedium ist ebenso möglich. Vorzugsweise erfolgt jedoch auch hier die Zufuhr des Vergasungsmediums von ganz unten, da hierdurch die Durchmischung des Brennstoffs unterstützt wird. Weiterhin wird die Entstehung von Kanälen und das Zurückrieseln von Feinanteilen verhindert. Prinzipiell ist es jedoch auch möglich, das Vergasungsmedium unterhalb der Pyrolysezone beispielsweise über eine Ringdüse seitlich zuzuführen.An embodiment with a separate feed for the gasification medium is also possible. Preferably, however, the supply of the gasification medium from the bottom takes place here as well, since this the mixing of the fuel is supported. Furthermore, the formation of channels and the trickling back of fines is prevented. In principle, however, it is also possible to feed the gasification medium below the pyrolysis zone laterally, for example via an annular nozzle.

Vorteilhaft ist es weiterhin, wenn der Vergaser mit unterschiedlicher Leistung betreibbar ist. Hierzu ist es vorteilhaft, wenn der Brennstoff mit nach oben hin abnehmender Geschwindigkeit durch den Vergasungsraum gefördert wird. Durch den Abbrand des Brennstoffes in der Oxidationszone mit weitgehend konstanter Geschwindigkeit nach unten hin verschiebt sich hierbei lediglich die Lage der Oxidationszone innerhalb des Vergasungsraumes, wobei sich jedoch stets selbstregelnd ein stabiler Betriebspunkt einstellt.It is also advantageous if the gasifier is operable with different power. For this purpose, it is advantageous if the fuel is conveyed through the gasification space with the speed decreasing towards the top. As a result of the burnup of the fuel in the oxidation zone at a substantially constant rate downwards, only the position of the oxidation zone within the gasification chamber shifts, whereby, however, a stable operating point always sets itself in a self-regulating manner.

Um den Vergaser mit unterschiedlicher Leistung betreiben zu können, ist es vorteilhaft, wenn der Vergasungsraum einen sich nach oben erweiternden Querschnitt aufweist. Hierdurch wird erreicht, dass der Brennstoff mit nach oben hin abnehmender Geschwindigkeit durch den Vergaser geführt wird. Hierdurch ist in günstiger Weise eine Anpassung an die in den einzelnen Reaktionszonen mit unterschiedlicher Geschwindigkeit ablaufenden Prozesse möglich. Die Lage der Oxidationszone in dem Vergasungsraum stellt sich hierbei stets an der Stelle ein, wo Abbrandgeschwindigkeit und Vorschubgeschwindigkeit übereinstimmen.In order to operate the carburetor with different power, it is advantageous if the gasification chamber has an upwardly widening cross-section. This ensures that the fuel is passed through the carburetor with the speed decreasing at the top. As a result, adaptation to the processes taking place at different speeds in the individual reaction zones is possible in a favorable manner. The position of the oxidation zone in the gasification chamber always adjusts itself at the point where the combustion rate and the feed rate coincide.

Nach einer anderen vorteilhaften Weiterbildung der Erfindung ist der Vergasungsraum von einer Isolierung vorzugsweise aus keramischen Fasern umgeben. Die thermische Belastung der Vergaseraußenwand kann hierdurch reduziert werden.According to another advantageous embodiment of the invention, the gasification chamber is surrounded by an insulation, preferably of ceramic fibers. The thermal load of the carburetor outer wall can be reduced thereby.

Weiterhin ist es vorteilhaft, wenn das Vergasungsmedium und/oder der Brennstoff vorgewärmt werden. Ein Teil der benötigten Prozesswärme kann hierdurch von außen in den Prozess eingebracht werden. Ebenso kann die benötigte Prozesswärme jedoch auch vollständig autotherm durch unterstöchiometrische Verbrennung eines Teiles des Brennstoffes erfolgen.Furthermore, it is advantageous if the gasification medium and / or the fuel are preheated. Part of the required process heat can thus be introduced into the process from the outside. Likewise, however, the required process heat can also be completely autothermal by substoichiometric combustion of a portion of the fuel.

Vorteilhaft ist es weiterhin, wenn in dem Vergasungsraum wenigstens ein Temperatursensor angeordnet ist, welcher den Füllstand des Vergasungsraumes überwacht. Ebenso ist es vorteilhaft, wenn in dem Vergasungsraum eine Mehrzahl von Sensoren angeordnet ist, welche die Lage der sich ausbildenden Reaktionszonen, insbesondere der Oxidationszone, erfassen. Da sich bei dem erfindungsgemäßen Verfahren die einzelnen Reaktionszonen sehr homogen und schichtförmig ausbilden, weisen diese deutliche Temperaturdifferenzen auf. Die Lage der Reaktionszonen sowie der Füllstand in dem Vergasungsraum kann hierdurch einfach, kostengünstig und ohne die Anordnung bewegter Teile durch Temperatursensoren erfasst werden.It is furthermore advantageous if at least one temperature sensor is arranged in the gasification space, which monitors the fill level of the gasification space. It is also advantageous if in the gasification room a plurality of sensors is arranged, which detect the position of the forming reaction zones, in particular the oxidation zone. Since in the method according to the invention, the individual reaction zones form very homogeneous and layered, they have significant temperature differences. The location of the reaction zones as well as the level in the gasification space can thereby be detected simply, inexpensively and without the arrangement of moving parts by temperature sensors.

Weiterhin ist es vorteilhaft, wenn eine Wand des Vergasungsraumes aus einem herkömmlichen Stahl ausgeführt ist. Durch die gleichmäßige Durchströmung der Reaktionszonen sowie den hohen Stoffumsatz in der Wirbelschicht kann in der Vorrichtung ein teerarmes Produktgas bei vergleichsweise niedrigen Temperaturen von maximal etwa 850°C erzeugt werden. Dabei liegt im Bereich der hohen Temperaturen eine reduzierende Atmosphäre vor. Der bauliche Aufwand des Vergasers kann somit durch Verwendung eines herkömmlichen Stahls gering gehalten werden. Besondere Feuerfestauskleidung, hochtemperaturbeständige Stähle oder Keramiken sind nicht erforderlich.Furthermore, it is advantageous if a wall of the gasification chamber is made of a conventional steel. Due to the uniform flow through the reaction zones as well as the high material conversion in the fluidized bed, a low-tarry product gas can be produced in the device at comparatively low temperatures of approximately 850 ° C. There is a reducing atmosphere in the area of high temperatures. The structural complexity of the carburetor can thus be kept low by using a conventional steel. Special refractory lining, high temperature resistant steels or ceramics are not required.

Vorteilhaft ist es weiterhin, wenn die mit dem Produktgas ausgetragene Asche mittels einer Abscheideeinrichtung aus dem Produktgas abgeschieden wird. Dies kann mit einfachen Mitteln, beispielsweise einem Zyklonabscheider, bewerkstelligt werden.It is furthermore advantageous if the ash discharged with the product gas is separated from the product gas by means of a separation device. This can be accomplished by simple means, such as a cyclone separator.

Weitere Vorteile der Erfindung werden anhand der nachfolgend dargestellten Ausführungsbeispiele beschrieben. Es zeigen:

Figur 1
ein Ausführungsbeispiel eines Vergasers in einem schematischen Vertikalschnitt sowie eine schematische Darstellung des erfindungsgemäßen Verfahrens und
Figur 2
eine schematische Darstellung des erfindungsgemäßen Verfahrens, wobei die Reduktionszone in Form einer Wirbelschicht ausgebildet ist.
Further advantages of the invention will be described with reference to the embodiments illustrated below. Show it:
FIG. 1
an embodiment of a carburetor in a schematic vertical section and a schematic representation of the method according to the invention and
FIG. 2
a schematic representation of the method according to the invention, wherein the reduction zone is formed in the form of a fluidized bed.

In beiden Figuren weist der Vergaser 1 eine Brennstoffzuführung 2 im Vergaserboden mit einer Fördereinheit 5 für den Brennstoff auf. Im Inneren des Vergasers 1 ist ein Vergasungsraum 3 angeordnet, welcher im gezeigten Beispiel einen veränderlichen Querschnitt aufweist. Vorliegend ist der Vergasungsraum 3 kegelstumpfförmig ausgeführt und von der äußeren Vergaserwandung durch eine Isolierung 4 getrennt.In both figures, the carburetor 1 has a fuel supply 2 in the carburetor bottom with a delivery unit 5 for the fuel. In the interior of the carburetor 1, a gasification chamber 3 is arranged, which has a variable cross-section in the example shown. In the present case, the gasification chamber 3 is frusto-conical and separated from the outer Vergaserwandung by an insulation 4.

Im oberen Bereich des Vergasungsraumes 3 ist ein Gassammelraum 12 ausgebildet, in welchem die entstehenden Gase 14 gesammelt und durch den oberseitig an dem Vergasungsraum 3 angeordneten Auslass 7 abgezogen werden. Weiterhin weist der Vergaser 1 eine Zuführung 6 für ein Vergasungsmedium 16 auf, welche mit einer Regeleinheit 15 in Wirkverbindung steht. Durch die Regeleinheit 15 ist erfindungsgemäß die Menge des zugeführten Vergasungsmediums 16 derart steuerbar, dass sich selbsttätig ohne mechanische Anströmböden in dem Vergasungsraum und ohne zusätzliche Fluidisierungsmittel eine Wirbelschicht 17 ausbildet.In the upper region of the gasification chamber 3, a gas collecting chamber 12 is formed, in which the resulting gases 14 are collected and withdrawn through the outlet 7 arranged on the top side of the gasification chamber 3. Furthermore, the carburettor 1 has a feed 6 for a gasification medium 16, which is in operative connection with a control unit 15. By means of the control unit 15, according to the invention, the amount of the gasification medium 16 fed in can be controlled in such a way that a fluidized bed 17 is formed automatically without mechanical distributor bottoms in the gasification space and without additional fluidizing means.

Figur 1 zeigt hierbei einen Vergaser 1, bei welchem die Zuführung 6 für das Vergasungsmedium 16 gemeinsam mit der Zuführung 2 für den Brennstoff 8 ausgebildet ist. Hierdurch wird der Brennstoff 8 von unten von dem Vergasungsmedium 16 durchströmt, so dass die Durchmischung des Brennstoffes 8 unterstützt und eine gleichmäßige Verteilung des Vergasungsmediums 16 über den gesamten Querschnitt sichergestellt wird. FIG. 1 in this case shows a carburetor 1, in which the feed 6 for the gasification medium 16 is formed together with the feed 2 for the fuel 8. As a result, the fuel 8 flows through from below from the gasification medium 16, so that the mixing of the fuel 8 is supported and a uniform distribution of the gasification medium 16 over the entire cross section is ensured.

Die Zufuhr des Vergasungsmediums 16 kann jedoch auch, wie in Figur 2 gezeigt, unterhalb der Pyrolysezone 9 seitlich durch eine Ringdüse erfolgen. Auch hier erfolgt jedoch die Zufuhr des Vergasungsmediums 16 durch den Brennstoff 8 hindurch, um hierdurch eine Durchmischung des Brennstoffes 8 und gleichmäßige Verteilung des Vergasungsmediums 16 zu erzielen. Zusätzliche mechanische Mischeinrichtungen sind somit nicht erforderlich. Zudem kann hierdurch verhindert werden, dass Feinanteile aus den obenliegenden Reaktionszonen 9, 10, 11 zurück in den Brennstoff 8 gelangen.However, the supply of the gasification medium 16 may also, as in FIG. 2 shown below the pyrolysis zone 9 laterally by an annular nozzle. Again, however, the supply of the gasification medium 16 through the fuel 8 passes through, thereby mixing the fuel. 8 and uniform distribution of the gasification medium 16 to achieve. Additional mechanical mixing devices are therefore not required. In addition, this can prevent fines from the overhead reaction zones 9, 10, 11 from entering the fuel 8.

Bei dem erfindungsgemäßen Verfahren wird der Brennstoff 8 entgegen der Schwerkraft kontinuierlich oder quasikontinuierlich, d.h. die gleiche Menge an Brennstoff je Zeiteinheit, durch die Brennstoffzuführung 2 in den Vergasungsraum 3 gedrückt und durch den Vergaser 1 gefördert. Der Brennstoff 8 wird hierbei vom Vergasungsmedium 16 und Produktgas 14 in der gleichen Richtung durchströmt. Es handelt sich in dieser Hinsicht also um eine aufsteigende Gleichstromvergasung. Als Vergasungsmedium 16 kommt vorteilhafterweise vorgewärmte Luft zum Einsatz. Der Prozess kann jedoch auch vollständig autotherm geführt werden.In the method according to the invention, the fuel 8 is continuously or quasi-continuous against gravity, i. the same amount of fuel per unit time, pressed by the fuel supply 2 into the gasification chamber 3 and promoted by the carburetor 1. The fuel 8 in this case flows through the gasification medium 16 and product gas 14 in the same direction. It is therefore in this respect an ascending DC gasification. As a gasification medium 16 is advantageously used preheated air. However, the process can also be completely autothermic.

Der Abbrand des Brennstoffes 8 erfolgt dabei von oben nach unten, wobei sich bei einem geeigneten gleichbleibenden Verhältnis Luftzufuhr zu Brennstoffzufuhr eine schichtförmige Oxidationszone 10 ausbildet. Durch die in der Oxidationszone 10 herrschenden Temperaturen von über 800°C bildet sich unterhalb derselben eine ebenfalls schichtförmige Pyrolysezone 9, in welcher sich der Brennstoff 8 bei Temperaturen um 500°C in Pyrolysekoks und gasförmige Verbindungen zersetzt. Das mit der von unten durch den Brennstoff 8 strömenden Luft 16 in der Pyrolysezone 9 gebildete Gas-Luftgemisch unterhält die Energieerzeugung in der Oxidationszone 10, wo ein Teil dieser Gase und des Pyrolysekokses verbrennt. Der verbleibende in der Pyrolysezone 9 gebildete Pyrolysekoks wandert allmählich durch die Oxidationszone 10 nach oben und bildet darüber eine Reduktionszone 11 aus. Die Darstellung der Figur 2 zeigt hierbei einen Prozess, bei welchem die Reduktionszone 11 im Wesentlichen vollständig in Form einer Wirbelschicht 17 ausgebildet ist. Hierdurch kann eine besonders gute und schnelle Umsetzung des Pyrolysekokses erzielt werden. Je nach Prozessführung und evtl. auch baulichen Gegebenheiten des Vergasers 1 ist jedoch auch ein Verfahren nach Figur 1 möglich, wobei die Reduktionszone 11 oberhalb der Oxidationszone 10 zunächst schichtförmig ausgebildet wird. Im oberen Bereich des Vergasungsraumes liegt die Reduktionszone 11 hingegen als Wirbelschicht 17 vor. In jedem Falle wird die Vergasung nach dem Prinzip einer aufsteigenden Gleichstromvergasung durchgeführt, welche jedoch erfindungsgemäß mit einer integrierten Wirbelschicht 17 in der Reduktionszone 11 kombiniert ist.The combustion of the fuel 8 takes place from top to bottom, with a layer-shaped oxidation zone 10 is formed at a suitable constant ratio of air supply to fuel. By prevailing in the oxidation zone 10 temperatures of about 800 ° C is formed below the same also a layered pyrolysis zone 9, in which decomposes the fuel 8 at temperatures around 500 ° C in pyrolysis and gaseous compounds. The gas-air mixture formed in the pyrolysis zone 9 by the air 16 flowing through the fuel 8 from below through the fuel 8 maintains the energy production in the oxidation zone 10, where a part of these gases and the pyrolysis coke burns. The remaining pyrolysis coke formed in the pyrolysis zone 9 gradually migrates upwards through the oxidation zone 10 and forms a reduction zone 11 above it. The presentation of the FIG. 2 shows a process in which the reduction zone 11 is formed substantially completely in the form of a fluidized bed 17. In this way, a particularly good and rapid implementation of the pyrolysis coke can be achieved. Depending on the process control and possibly also structural conditions of the carburetor 1, however, a method according to FIG. 1 possible, wherein the reduction zone 11 above the oxidation zone 10 is first formed in layers. In the upper region of the gasification space, however, the reduction zone 11 is present as a fluidized bed 17. In each case, the gasification is carried out according to the principle of an ascending DC gasification, which, however, according to the invention is combined with an integrated fluidized bed 17 in the reduction zone 11.

In der Reduktionszone 11, 17 wird der Pyrolysekoks unter anderem von CO2 und H2O aus der Pyrolysezone 9 und der Oxidationszone 10 durchströmt, wobei diese endotherm zu den brennbaren Gasen CO und H2 reduziert werden, wodurch der Pyrolysekoks vergast wird.In the reduction zone 11, 17, the pyrolysis coke is flowed through, inter alia, by CO 2 and H 2 O from the pyrolysis zone 9 and the oxidation zone 10, these being reduced endothermically to the combustible gases CO and H 2 , whereby the pyrolysis coke is gasified.

Wenn sich nun in der Reduktionszone 11 durch Feinanteile die Zwischenräume im Pyrolysekoks zusetzen, so führt der dadurch ansteigende Gasdruck dazu, dass der Pyrolysekoks angehoben und damit gelockert wird. Es bildet sich erfindungsgemäß durch die entspreche Einstellung der zugeführten Menge des Vergasungsmediums 16 und die Anströmung des Brennstoffs 8 von unten ein Gleichgewicht zwischen Gasdruck und Gewichtskraft des Pyrolysekokses bis hin zum Fließbett.If, in the reduction zone 11, the intermediate spaces in the pyrolysis coke become clogged by fines, the resulting gas pressure causes the pyrolysis coke to be raised and thereby loosened. It forms according to the invention by the appropriate adjustment of the supplied amount of the gasification medium 16 and the flow of the fuel 8 from below an equilibrium between the gas pressure and the weight of the pyrolysis coke up to the fluidized bed.

Das von unten zugeführte Vergasungsmedium 16, vorzugsweise Luft, erfährt in der Oxidationszone 10 einen sprunghaften Temperaturanstieg und damit verbunden eine Volumenvergrößerung. Zusammen mit den entstehenden Pyrolyse- und Verbrennungsgasen führt dies insbesondere beim bevorzugten Einsatz handelsüblicher Holzpellets als Brennstoff zur dauerhaften Ausbildung einer Wirbelschicht 17 in der Reduktionszone 11. Damit wird die von Festbettvergasern bekannte kritische Kanalbildung in diesem Bereich vollständig unterbunden.The supplied from below gasification medium 16, preferably air, experiences in the oxidation zone 10, a sudden increase in temperature and, associated therewith, an increase in volume. Together with the resulting pyrolysis and combustion gases, this leads in particular to the preferred use of commercially available wood pellets as fuel for permanent formation of a fluidized bed 17 in the reduction zone 11. Thus, the known from fixed bed gasifiers critical channel formation is completely suppressed in this area.

Bei dem erfindungsgemäßen Vergasungsverfahren bildet der Brennstoff 8 durch seine kontinuierliche För-derung bei entsprechender Regelung der Zufuhr des Vergasungsmediums 16 einen Anströmboden zur Wirbelschichterzeugung. Die Wirbelschicht 17 kann hierbei ohne weitere Fluidisierungsmittel erzeugt werden. Hierdurch ist es möglich, den in der Oxidationszone 10 gebildeten Pyrolysekoks nahezu vollständig zu Gas und Flugasche umzusetzen und damit einen hohen Wirkungsgrad des Gesamtverfahrens zu erreichen. Es hat sich gezeigt, dass die Wirbelschicht 17 in dem Vergaser 1 über einen relativ breiten Luftmengenbereich stabil ist und damit die Regelung der Luftmenge durch die Regeleinheit 15 auf die für die thermochemische Vergasung nötigen Luftraten problemlos möglich ist.In the gasification process of the invention, the fuel 8 forms by its continuous För-tion with appropriate control of the supply of the gasification medium 16 a distributor plate for fluidized bed production. The fluidized bed 17 can be produced without further fluidizing agent. This makes it possible to almost completely convert the pyrolysis coke formed in the oxidation zone 10 to gas and fly ash and thus to achieve a high degree of efficiency of the overall process. It has been shown that the fluidized bed 17 is stable in the carburetor 1 over a relatively wide range of air volumes and thus the regulation of the amount of air through the control unit 15 is easily possible to the necessary for the thermochemical gasification air rates.

Die entstehende Asche wird vorzugsweise als Flugasche ohne zusätzliche Austragsvorrichtungen mit dem Prozessgas 14 ausgetragen und danach mit einfachen Mitteln, beispielsweise durch einen Zyklonabscheider, aus dem Produktgas 14 abgeschieden. Durch den oberen Abbrand bei dem erfindungsgemäßen Verfahren sowie die Führung des Vergasungsmediums 16 sowie das Produktgas 14 durch den Vergaser 1 und die gute Umsetzung des Brennstoffs 8 ist das Produktgas 14 mit dem Auslass 7 als Austragvorrichtungen für die Asche vollkommen ausreichend. Sofern dennoch überschüssiger Pyrolysekoks entsteht oder gezielt erzeugt werden soll, kann dieser ebenfalls zusammen mit der entstehenden staubförmigen Asche mit dem Produktgas 14 abgezogen werden.The resulting ash is preferably discharged as fly ash without additional discharge devices with the process gas 14 and then separated from the product gas 14 by simple means, for example by a cyclone separator. Due to the upper burnup in the method according to the invention and the guidance of the gasification medium 16 and the product gas 14 through the carburetor 1 and the good implementation of the fuel 8, the product gas 14 with the outlet 7 as discharge devices for the ash is completely sufficient. If, however, excess pyrolysis coke is produced or intentionally generated, this can likewise be taken off together with the resulting dusty ash with the product gas 14.

Bei dem erfindungsgemäßen Vergasungsverfahren führt die gleichmäßige Durchströmung der sich sehr homogen ausbildenden Pyrolyse-, Oxidations- und Reduktionszonen 9, 10, 11 zur Erzeugung eines teerarmen Gases sehr gleichmäßiger Qualität bei vergleichsweise niedrigen Temperaturen von etwa 850°C in der Oxidationszone 10. Dadurch wird es möglich, einen Vergaser 1 ohne Verwendung spezieller hochtemperaturbeständiger Stähle oder Keramiken auszuführen. Selbst herkömmlicher Baustahl ist verwendbar, da durch die reduzierende Atmosphäre der unterstöchiometrischen Verbrennung keine nennenswerte Oxidation stattfindet. Die Vermeidung der im Stand der Technik üblichen keramischen Bauteile führt zudem bedingt durch geringe Wärmekapazitäten vorteilhafterweise zu kurzen Aufheiz- und Abkühlzeiten beim An- und Abfahren der Vergaser 1.In the gasification process according to the invention, the uniform flow through the very homogeneously forming pyrolysis, oxidation and reduction zones 9, 10, 11 leads to the production of a tarry gas of very uniform quality at comparatively low temperatures of about 850 ° C. in the oxidation zone 10 possible to carry out a carburetor 1 without the use of special high-temperature resistant steels or ceramics. Even conventional structural steel can be used, since there is no appreciable oxidation due to the reducing atmosphere of the substoichiometric combustion. The avoidance of the usual in the prior art ceramic components also leads due to low heat capacity advantageously too short heating and cooling times when starting and stopping the carburetor. 1

Eine bevorzugte Ausführung eines Vergasers 1 besitzt wie im Beispiel dargestellt einen sich nach oben erweiternden Querschnitt des Vergasungsraumes 3. Dies erlaubt den Betrieb mit unterschiedlicher Leistung, denn es bewirkt, dass der Brennstoff 8 mit abnehmender Geschwindigkeit durch den Vergaser 1 nach oben wandert. Der in der Oxidationszone 10 mit weitgehend konstanter Geschwindigkeit nach unten zu erfolgende Abbrand führt nun dazu, dass sich selbstregelnd ein stabiler Betriebspunkt einstellt, bei dem die Oxidationszone 10 an der Stelle verharrt, wo Abbrandgeschwindigkeit und Vorschubgeschwindigkeit des Brennstoffes 8 übereinstimmen.A preferred embodiment of a carburetor 1 has, as shown in the example, an upwardly widening cross-section of the gasification chamber 3. This allows operation with different power, because it causes the fuel 8 to move upwards through the carburetor 1 with decreasing speed. The burning down to be carried out in the oxidation zone 10 at a substantially constant speed now leads to a self-regulating setting of a stable operating point at which the oxidation zone 10 remains at the point where the burning rate and feed rate of the fuel 8 coincide.

Weiterhin sorgt die kontinuierliche oder quasikontinuierliche Zufuhr neuen Brennstoffes 8 insbesondere in Verbindung mit dem wechselnden Querschnitt des Vergasungsraumes 3 für eine ständige Bewegung und Durchmischung des Materials und verhindert damit ohne weitere mechanische Vorrichtungen die Kanal- und Brückenbildung in Oxidations- und Reduktionszone 10, 11.Furthermore, the continuous or quasi-continuous supply of new fuel 8, in particular in conjunction with the changing cross-section of the gasification chamber 3, ensures constant movement and thorough mixing of the material and thus prevents channeling and bridge formation in the oxidation and reduction zones 10, 11 without further mechanical devices.

Im Vergasungsraum ist weiterhin eine Mehrzahl übereinander angeordneter Temperatursensoren 13 angeordnet, welche mit der Regeleinheit 15 zusammenwirken und den Füllstand des Vergasungsraumes 3 sowie die Lage der Reaktionszonen (9, 10, 11) messtechnisch erfassen. Die Grenzen zwischen dem Brennstoff 8 und der Pyrolyse- und Oxidationszone (9, 10) sowie zwischen der Reduktionszone (11) und dem darüber liegenden Gassammelraum (12) sind aufgrund der sehr homogenen Ausbildung bei dem erfindungsgemäßen Verfahren und dem Vergaser 1 durch deutliche Temperaturdifferenzen gekennzeichnet. Die regelungstechnisch wichtige Lage der Reaktionszonen 9, 10, 11, insbesondere der Oxidationszone 10, sowie die Füllhöhe können somit kostengünstig und ohne bewegte Teile in einfacher Weise erfasst werden.In the gasification chamber a plurality of superimposed temperature sensors 13 is further arranged, which cooperate with the control unit 15 and the level of the gasification chamber 3 and the position of the reaction zones (9, 10, 11) detect by measurement. The boundaries between the fuel 8 and the pyrolysis and oxidation zone (9, 10) and between the reduction zone (11) and the overlying gas collection chamber (12) are characterized by significant temperature differences due to the very homogeneous formation in the inventive method and the carburetor , The control technology important location of the reaction zones 9, 10, 11, in particular the oxidation zone 10, and the filling level can thus be detected in a simple manner cost and without moving parts.

Die mit der Erfindung erzielten Vorteile bestehen insbesondere darin, dass ein Vergaser 1 ohne bewegte Teile im heißen Bereich auskommt und keine mechanisch belasteten heißen Teile aufweist, welche im Stand der Technik häufig eine Störquelle darstellen. Der erfindungsgemäße Vergaser 1 findet durch selbstregelnde Eigenschaften bei geringem mechanischen und/oder elektronischen Regelungsaufwand einen stabilen Betriebspunkt und liefert damit dauerhaft ein teerarmes Produktgas mit nur geringfügig schwankender Qualität. Kanal- und Brückenbildung sowie Teerschlupf können vermieden werden. Der Vergaser 1 ist daher insbesondere für kleine und mittlere Anlagen bis ca. 1 MW elektrisch geeignet, da keine aufwändige Gasnachbehandlung erforderlich ist. Ebenso ist es möglich, direkt ein motorfähiges Produktgas zu erzeugen. Weiterhin ist mittels der Vorrichtung bei entsprechender Prozessführung auch die Herstellung von Holzkohle möglich.The advantages achieved by the invention are in particular that a carburetor 1 manages without moving parts in the hot area and has no mechanically loaded hot parts, which often constitute a source of interference in the prior art. The carburetor 1 according to the invention finds by self-regulating properties with low mechanical and / or electronic control effort a stable operating point and thus provides a durable tarerarmes product gas with only slightly fluctuating quality. Channel and bridge formation as well as tar slippage can be avoided. The carburetor 1 is therefore particularly suitable for small and medium sized systems up to about 1 MW electrically, since no complex gas aftertreatment is required. It is also possible to directly produce a motorable product gas. Furthermore, the production of charcoal is possible by means of the device with appropriate process control.

Der eingesetzte Brennstoff 8 braucht nicht grobstückig zu sein und darf hohe Mengen Feinanteil enthalten, da durch die Prozessführung eine Verstopfungsneigung vermieden wird. Somit können Brennstoffe 8 verwendet werden, die in ausreichender Menge am Markt verfügbar sind.The fuel used 8 need not be coarse and may contain high amounts of fines, since the process control a tendency to clog is avoided. Thus, fuels 8 which are available in sufficient quantity on the market can be used.

Durch den einfachen konstruktiven Aufbau und eine einfache Regelungstechnik mittels der Regeleinheit 15 kann der Vergaser 1 zudem kostengünstig hergestellt und betrieben werden.Due to the simple structural design and a simple control technology by means of the control unit 15, the carburetor 1 can also be manufactured and operated inexpensively.

Die Erfindung ist nicht auf das dargestellte Ausführungsbeispiel beschränkt. Abwandlungen und Kombinationen im Rahmen der Patentansprüche fallen ebenfalls unter die Erfindung.The invention is not limited to the illustrated embodiment. Variations and combinations within the scope of the claims also fall under the invention.

Claims (6)

  1. A single-stage method for thermochemically gasifying solid fuels (8) according to the principle of rising downdraft gasification, a fuel (8) being fed into a gasifying chamber (3) against gravity, a gasifying medium (16) being mixed into the fuel in a downdraft, and a resulting product gas (14) being discharged in a downdraft, characterized in that, the fuel (8) is continuously fed into the gasifying chamber (3) via a fuel inlet (2) in the gasifier floor, and that the gasifying medium (16) is fed from below through the infed fuel (8) into a forming stratified oxidation zone (10), wherein the gasifying medium (16) is fed via an inlet (6) below a stratified pyrolysis zone (9) forming in the gasifying chamber (3) and present as a solid bed into the stratified oxidation zone (10) and into a reduction zone (11), wherein the fuel forms an impinging flow floor for generating a stationary fluidized bed and wherein the amount of the gasifying medium (16) fed in is adjusted by a controller unit (15), such that a solid bed is present in the lower regions of the gasifier in the fuel inlet and in the pyrolysis zone, and the stationary fluidized bed (17) is implemented in the reduction zone (11) above the oxidation zone (10) without a mechanical flow impingement floor, and without feeding in additional fluidizing medium, and the ash produced is carried away solely by the exiting product gas.
  2. The method according to the preceding claim, characterized in that the reduction zone (11) above the oxidation zone (10) is entirely implemented as a stationary fluidized bed (17).
  3. The method according to any one of the preceding claims, characterized in that the fuel (8) is broken up and mixed without contact in the gasifying chamber.
  4. The method according to any one of the preceding claims, characterized in that the gasifying medium (16) is fed in together with the fuel (8) and flows through a pyrolysis zone (9), the oxidation zone (10), and the reduction zone (11) in sequence.
  5. The method according to any one of the preceding claims, characterized in that the fuel (8) is transported through the gasifying chamber (3) at a velocity decreasing with upward progression.
  6. The method according to any one of the preceding claims, characterized in that the fill level of the gasifying chamber (3) and/or the location of the forming reaction zones (9, 10, 11), particularly the pyrolysis zone (9), the oxidation zone (10), and the reduction zone (11) is captured by one or a plurality of temperature sensors (13).
EP09783675.3A 2008-10-23 2009-10-02 Method for thermochemically gasifying solid fuels Active EP2356200B1 (en)

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DE102008043131A DE102008043131B4 (en) 2008-10-23 2008-10-23 Process and apparatus for thermochemical gasification of solid fuels
PCT/EP2009/062807 WO2010046222A2 (en) 2008-10-23 2009-10-02 Method and device for thermochemically gasifying solid fuels

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US8721748B1 (en) 2013-01-28 2014-05-13 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
AT14489U1 (en) 2013-12-18 2015-12-15 Syncraft Engineering Gmbh Method and device for discharging contaminants
ES2662406T3 (en) 2015-04-30 2018-04-06 Ws-Wärmeprozesstechnik Gmbh Procedure and device for biomass gasification
EP3309240A1 (en) 2016-10-12 2018-04-18 WS-Wärmeprozesstechnik GmbH Method and device for gasification of biomass
CN115261074B (en) * 2022-07-29 2023-04-11 赣州市怡辰宏焰能源科技有限公司 Tower type fire grate gasification furnace with water tank

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WO2010046222A3 (en) 2010-07-22
DE102008043131B4 (en) 2012-09-20
EP2356200A2 (en) 2011-08-17
WO2010046222A2 (en) 2010-04-29
HRP20180376T1 (en) 2018-04-20

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