DE3523765A1 - Process for gasifying carbonaceous fuels and equipment for carrying out the process - Google Patents

Abstract

The invention relates to a process and equipment for gasifying carbonaceous fuels by heating the fuel with exclusion of air to form low-temperature carbonisation gases in a low-temperature carbonisation zone (II), subsequent carbonisation in a coking zone (III), oxidation of the resulting coal (coke) and of the low-temperature carbonisation gases in an oxidation zone (IV) with oxygen supply and subsequent reduction by means of coal originating from the coking zone in a reduction zone (V). In order to avoid the formation of tar fractions and other harmful substances in the product gas and altogether to obtain gasification of the feed material as completely as possible and with low production of harmful substances, it is provided according to the invention that, by blowing oxygen-containing gas (air) into a substantially solid-free oxidation zone (IV), the low-temperature carbonisation gas is drawn into the solid-free oxidation zone (IV) with separation from solid constituents of the low-temperature carbonisation zone (II), and substantially completely burned. <IMAGE>

Description

The invention relates to a method and a device for the gasification of in particular fine-grained or chip-shaped carbonaceous fuels by heating the Fuel in the absence of air with formation of carbonization gases in a smoldering zone, subsequent charring in a coking zone, oxidation of the resulting coal (Coke) and the carbonization gases with oxygen supply in one Oxidation zone and subsequent reduction with the help of coal from the coking zone in a reduction zone.

Such methods and devices have long been known and were used to supply gas in particular before 1945 Vehicle engines used.

Under the impression of rising energy prices, more polluting Mountains of waste and an increasing awareness of environmentally friendly and decentralized energy supply, which in particular also of great importance in the countries of the third world are such gasification processes and devices now technically and economically again become attractive.

For small to medium capacities, the so-called Imbert method known in which a generally cylindrical double-walled pyrolysis tank with fuel is filled, which is then heated in the absence of air becomes. The process heat required for this is initially delivered by hot combustion gases that one by burning the fuel in the lower part of the Pyrolysis container generated with air supply. During the The pyrolysis process is formed inside the pyrolysis container essentially three stacked zones which with increasing distance from the combustion or Oxidation zone at the bottom of the pyrolysis tank  have correspondingly lower temperatures.

The upper zone, in which temperatures range from 300 to 400 ° C Rule is also known as the drying zone. In the underlying smoldering zone are at temperatures of about 400 to 500 ° C the volatile components from the solid fuel driven out; smoldering gas is produced. This process continues in the one below Coking zone continues at temperatures up to 700 ° C, whereby in lower region of the coking zone as a practical solid only pure carbon in the form of e.g. coke or charcoal.

Since the pyrolysis container is closed at the top, the resulting must Smoldering gas, which in the gaseous state is a significant occupies larger space than in the previous bound Shape, pass down through the oxidation zone, where it is largely burned. In this stadium the gasification process becomes much of the required Process heat not from burning carbon but delivered by the burning carbonization gas. Because of the coal or coke slides under gravity below and is partially below the through the air supply limited oxidation zone in the so-called Reduction zone.

The exhaust gases resulting from the combustion of the carbonization gas at a temperature of approx. 1200 ° C. also contain CO ₂ to a considerable extent, which is reduced to Co at the temperatures prevailing in the reduction zone of approximately 900 ° C. by the carbon present here escapes to the consumer together with the other exhaust gases through the cavity formed by the double wall of the pyrolysis container and thereby releases the process heat to the pyrolysis container.

In a further reaction, the water vapor present in the carbonization gas and the carbon in the reduction zone likewise produce CO and H ₂ , which likewise escape together with the other exhaust gases and release their chemical energy as heat when the product gas is later burned.

In general, when gasifying fuels, the aim is to obtain the largest possible proportion of the product gas in the form of energy-supplying CO and H ₂ , possibly also in smaller amounts of CH ₄ . A certain proportion of N ₂ and CO ₂ is unavoidable.

A disadvantage of many gasification processes, however, is that that the carbonization gas is not at sufficiently high temperatures is completely burned, leaving one row for the next Use of the product gas harmful and polluting Substances (e.g. higher quality hydrocarbons, Naphthenes and aromatics) are present in the product gas.

This disadvantage occurs especially in the case of a direct current fixed bed gasifier on if the Diameter of the oxidation zone exceeds certain values. This problem is exacerbated when used Fuels are fine-grained and / or chip-shaped, so that this method is practically not for such fuels can be used. The reason for this is that the descending carbonization gas in the oxidation zone so-called Cold runner forms in which the temperature is well below that required for cracking the substances mentioned Temperature. With lumpy fired goods you can go through appropriate air supply up to certain cross sections of the Oxidation zone avoid the formation of such cold runners, because the air supply over larger areas more or less can be done evenly. For fine-grained or chip-shaped Fuel would however be scaled down accordingly the cross section of the oxidation zone and thus the entire carburetor to uneconomically small units to lead.  

The fluidized bed process also to be considered does not know the formation of such cold runners, is however for specifically light substances, e.g. Wood shavings or for a mixture specifically lighter and heavier Substances such as Household waste practically not applicable and also for systems of small to medium capacity too expensive and complicated and can therefore not be economical be used.

Other processes have the disadvantage that they are in a separate oxidation and / or reduction zone Require the use of additional foreign coke or charcoal.

The object of the present invention is therefore a method and to create a device by means of which it is possible, especially fine-grained and / or chip-shaped gasify carbonaceous material so that essentially only a pollutant-free gas with high Calorific value and mineral ash are created.

This object is achieved in that in one method with the features of the preamble of claim 1 Blowing oxygen-containing gas (air) into an essentially solid-free oxidation zone below the carbonization gas Separation of solid components into the solids-free Oxidation zone sucked in and essentially complete is burned.

The separation of the carbonization gas from the solids in the pyrolysis chamber and its subsequent combustion with the addition of oxygen in an essentially solid-free oxidation zone leads to a complete combustion of the Smoldering gas, in which practically none of the above harmful substances are present. This succeeds because because of the absence of solid fuels, apart from some whirled up dust, in the oxidation zone the formation of cold runners is no longer possible.  It is completely irrelevant whether lumpy fuel or used fine-grained and / or chip-shaped material becomes what compared to the direct current fixed bed process above all brings a considerable cost advantage, because fine-grained and / or chip fuels often as waste products incur otherwise only at cost are to be eliminated. Instead, they can go through the procedure according to the invention for gas or energy generation be used sensibly, so that in addition to the elimination of waste disposal costs often also considerable energy costs omitted, which may result in a corresponding system amortized after a very short time.

According to the invention it is provided that the combustion of the Smoldering gases at 1050 to 1300 ° C, preferably at 1100 to 1200 ° C. The combustion temperature is controllable essentially by changing the air supply. The advantage resulting from these combustion temperatures consists in the fact that the pollutants mentioned above are largely be decomposed so that the product gas is practical is free of tar components and the like. Regarding the device for performing the described method, consisting of a gasification tank with a Can be loaded from above and in the upper part of the gasification tank arranged pyrolysis chamber, one below the Pyrolysis chamber located reduction chamber, one between these chambers arranged passage opening for the coal from the coking zone and one for heating the fuel enclosing the vertical walls of the pyrolysis chamber Product gas discharge, the task is solved in that on bottom of the pyrolysis chamber essentially one Solids-free and covered up against the pyrolysis chamber or next to the pyrolysis chamber or the reduction chamber arranged combustion chamber is provided in the entrance area at least one air jet nozzle for suction of carbonization gas from the coking zone according to the jet pump principle arranged with the beam direction in the interior of the combustion chamber and that the exit area of the combustion chamber  in the gas flow direction in connection with the reduction chamber stands.

The air jet nozzle is therefore in the entrance area of a combustion chamber attached and emits oxygen-containing gas (expediently Air) at high speed (e.g. 250 m / s) into the combustion chamber. The entrance area of the combustion chamber, in which this air jet nozzle is located in connection with the coking zone of the pyrolysis chamber, while the exit area of the combustion chamber essentially, i.e. at least in the main flow direction of the fuel gases, communicates with the reduction chamber.

The fact that the combustion chamber up against the pyrolysis chamber is covered or spatially next to the pyrolysis chamber or the reduction chamber is arranged, it is essentially from due to gravity from the pyrolysis chamber fuel slipping into the reduction chamber (charcoal or coke) free. Depending on the arrangement and Design of the combustion chamber and especially its cover or delimitation against the pyrolysis chamber and also depending of the arrangement of the passage opening between Pyrolysis chamber and reduction chamber a certain proportion of the Coal from the coking zone, which is essentially pure Carbon consists of a certain part of the combustion chamber or fill in the marginal areas.

Because of the high speed in the entrance area of the Combustion chamber gas (air) flowing out of the air jet nozzle is now also connected to the entrance area of the Combustion chamber related pyrolysis chamber there Existing gas (carbonization gas) according to the jet pump principle (Venturi principle) sucked in and burns together with the Oxygen escaping from the nozzle in the solids-free part the combustion chamber at approx. 1200 ° C. That maybe at the same time dust whirled up in the combustion chamber or in the edge areas of the slid carbon in shape burning of coke or charcoal is of secondary importance  Importance. It is essential that the carbonization gas burns completely at the high temperature mentioned, what by an appropriate size of the combustion chamber and by the fact that the combustion of the carbonization gas in one Part of the combustion chamber, which is essentially solid fuel free, i.e. free of a more or less dense Packing or pouring of solid material takes place, is ensured. Due to the strong air jet from the Nozzle takes place in the solids-free area of the combustion chamber an intense swirling takes place that is not due to dense packed material is prevented, so that the combustion without the formation of cold runners in which carbonization gas is not could burn down completely burned, under largely homogeneous and constant conditions run completely can.

The likewise gaseous combustion products then flow at the outlet of the combustion chamber into the reduction chamber, which otherwise contains practically pure carbon, which at temperatures above 800 ° C, which are generated by the hot combustion gases, gasifies at least partially to CO by reducing the CO ₂ becomes.

It is in preferred embodiments of the invention expedient and advantageous if the passage opening communicates directly with the combustion chamber.

This ensures that a certain part of the fuel from the pyrolysis chamber in the combustion chamber located when the carburetor is started up can be lit and so the process heat at the beginning provides that for the generation of the not yet available Smoldering gas is required.

Furthermore, it is advantageous if a gasification device according to the invention the combustion chamber and the air jet nozzle (s) immediately below the pyrolysis chamber in Area of the passage opening are arranged.  

This arrangement of the firing chamber between the pyrolysis chamber and Reduction chamber has the advantage, among other things, that Heat loss when supplying the carbonization gas to the combustion chamber and when the combustion gases are removed from the combustion chamber avoids and beyond that the compounds mentioned the entrance area to the pyrolysis chamber, the exit area to the reduction chamber and between the passage opening and the combustion chamber to be taken into account in a simple manner are.

According to an advantageous embodiment of the invention provided that the combustion chamber below a conical Taper at the bottom of the pyrolysis chamber as annular combustion chamber is formed and that several Air jet nozzles radially to a centrally just below the tapered air supply line arranged are, between a circular nozzle holder, whose radius is approximately the smallest radius of the conical taper corresponds or is slightly larger, and the edge of the an annular gap is formed as a passage opening becomes.

In cross-section, the conical taper can shape have an overhanging nose, so that the combustion chamber Form an annular at the top of the reduction chamber surrounding and open tunnels. The conical The taper of the pyrolysis chamber forms a funnel, through the central opening one into the side into the pyrolysis chamber incoming air supply line is passed through, the immediately below the circular opening of the Funnel into a circular nozzle holder the air jet nozzles that radiate radially outwards into the combustion chamber are arranged. The diameter of the of the Nozzles or the circle formed by the nozzle holder is included about the same size as the diameter of the funnel opening or something bigger.  

In this way it is used as a passage opening for slipping the coal from the coking zone of the pyrolysis chamber into the Oxidation zone or the subsequent reduction zone of the Reduction chamber formed an annular gap. The carbon (Coke or charcoal) slips out of the pyrolysis chamber this annular gap into the reduction chamber, the Surface of the carbon one under a certain Angle of repose forms a truncated cone. Above the Cone surface, the tunnel-shaped annulus forms the combustion chamber, into which the radially aligned air jet nozzles radiate, due to the high air jet speed through the annular gap of carbonization gas from the area in the coking zone. Can by design in this way at most by the flow of the carbonization gas Carbon particles carried away from the coking zone be opposed to the combustion of the carbonization gases to fuel not yet coked have a disruptive influence.

A particularly preferred embodiment of the invention Device is characterized in that the combustion chamber essentially in the form of a transverse funnel is formed, at the entrance to the tapered At the end of the funnel, the air jet nozzle radiates axially is arranged, and that this input with an upward closed and downwardly open annulus in the lower Area of the coking zone which is essentially connected contains only carbonization gas. The annular space is expedient arranged on the wall of the pyrolysis chamber and stands over pipes or baffles or ducts with the entrance area the funnel-shaped combustion chamber in connection. Since the annulus is closed from above, this can be done by Do not penetrate the fuel that is sliding down at the top, but that which exists in the entire pyrolysis chamber Smoldering gas. This special arrangement means that the air jet, which also axially Entrance of the funnel-shaped combustion chamber is particularly arranged effectively almost exclusively carbonization gas from the combustion zone  sucked in without already at the same time burned or reduced gas from the reduction zone is sucked in. As in the aforementioned embodiment here too no particles of not yet coked get Material into the combustion chamber.

In this embodiment, too, the lower region of the Pyrolysis chamber advantageously conical or funnel-shaped trained so that the carbon from the coking zone can slip into a passage opening, which preferably is arranged so that at least part of the Carbon before or along the exit area of the funnel-shaped combustion chamber gets into the reduction chamber. If necessary, the Combustion chamber baffles or the like arranged, or the combustion chamber is with a more or less inclined funnel axis arranged so that the outflowing combustion gases preferably flow down into the reduction chamber.

The fuel present in the exit area of the combustion chamber again serves for the initial commissioning of the carburetor for preheating.

According to the invention, it is advantageous if in the axis the air jet nozzle, an ignition lance that can be inserted into the nozzle is provided for igniting the fuel.

It is further provided according to the invention that the product gas discharge in the upper area of the gasification tank a pipe connected to a hot gas filter device is at the lower end of a rotary valve for Discharge of accumulated dust in a dust combustion chamber is arranged, which has a connection at its input the air supply line and at its outlet with the lower area of the reduction chamber is connected.

The product gas escaping through the product gas discharge generally entrains a high proportion of dust particles. This applies in particular if fine-grained and / or chip-shaped fuel is already used as the gasification material. Accordingly, the product gas, which emerges at the upper area of the carburetor at a temperature of approx. 400 ° C, passes through a hot gas filter device in which the dust, which mainly consists of carbon and a small part of ash, is separated and, for example, via a rotary valve Dust combustion chamber is supplied. This dust combustion chamber opens into the lower area of the reduction chamber, where mineral ash is separated, and is connected at its entrance to the air supply line, so that the combustion of the carbon dust can be controlled by blasting combustion air through a corresponding nozzle at the entrance to the dust combustion chamber. This produces CO ₂ , which escapes into the reduction chamber via the outlet of the dust combustion chamber and is reduced at the temperatures prevailing there by the excess carbon present there, which is not gasified by the combustion gases from the carbonization gas combustion chamber. The carbon is gasified to CO.

This advantageously results in an additional possibility control the throughput of the pyrolysis material, and so to a really complete gasification of the used Material to arrive at, in addition to the almost completely pollutant-free product gas only mineral ash remains as a solid waste material that settles on the bottom of the Reduction chamber accumulates.

According to the invention it is provided that in the lower area the pyrolysis chamber and in the inlet area of the product gas discharge Pressure measuring points for measurement and monitoring the pressure difference between the pyrolysis chamber and the reduction chamber are provided.

This pressure difference is a measure of the material throughput or for the amount of the accumulating in the reduction chamber Carbon and therefore serves as a control parameter  to control afterburning.

It is advantageous according to the invention if at the bottom End of the gasification tank under the reduction chamber a discharge screw or a rotary valve for discharge the ashes from the ashes of the reduction chamber in an ash container is arranged.

With regular discharge of the ashes and a corresponding one Feed gasification material through the top end the feed opening of the carburetor is thus a continuous operation of the gasification device over a longer period possible. The loading takes place here with fuel also via lock devices, to keep the oxygen content in the pyrolysis chamber as low as possible hold and prevent gas leakage.

Since the fuels to be used may also contain a certain proportion of sulfur, it is provided according to the invention that a lime container is connected to the reduction chamber via a lime supply device. The lime supplied in this way converts with the sulfur contained in the combustion gases, which is often in the form of H ₂ S, to CaS, which is separated in the hot gas filter device and burned in the dust combustion chamber to CaSO ₄ (gypsum) and discharged together with the mineral ash becomes. Because of the reducing atmosphere in the reduction chamber, there is no gaseous SO ₂ (and also not directly CaSO ₄ ), which otherwise arises during the generation of energy through combustion and can only be removed from the combustion gases by complex flue gas scrubbing.

Further advantages, features and possible applications of the present invention result from the following Description of the method and preferred embodiments the associated device based on the corresponding Characters. Show it:  

Fig. 1 shows a gasification tank with the associated devices and an annular annular chamber and

Fig. 2 shows a gasification tank with a transverse, funnel-shaped combustion chamber.

The method is first explained with reference to FIG. 1.

The gasification container is filled with fuel from above through the feed opening 19 . This fuel can be in more or less any form. Depending on the application, the carburettor is either fed with fuel that falls off during production (e.g. wood chips from a sawmill) or with fuel that is as inexpensive as possible, such as household waste (if necessary, shredded and pre-sorted). The material slips out of the pyrolysis chamber 1 through the passage opening 21 into the reduction chamber 2 .

Various options are conceivable for heating up or starting up the carburetor, which depend on the size of the system, the intended operating time and the options and wishes of the operator. For example, charcoal or coke can be charged first until the reduction chamber and the lower part of the pyrolysis chamber are filled, after which the material to be gasified is then refilled. Likewise, a combustion gas can be supplied for preheating, or the material in the area of the combustion chamber 4 and / or in the reduction chamber 2 below it is burned with the supply of air.

In the normal operating state, the fuel in the drying zone 1 has a temperature between 200 and 400 ° C, whereby up to the temperature of 200 ° C most of the H ₂ O, CO ₂ and CH ₄ present in the material have already escaped. The so-called pre-degassing takes place up to the temperature of 400 ° C., whereby primarily CO, CO ₂ and H ₂ O are formed. So-called main degassing takes place up to a temperature of 450 to 500 ° C, during which H ₂ and saturated and unsaturated hydrocarbons escape. The main degassing takes place in the so-called smoldering zone II. The resulting gas mixture is called carbonization gas. The rest of the gases, which are still present in bound form in the fuel, are released at temperatures above 500 ° C in the so-called charring and coking zone III, leaving practically pure carbon in the form of charcoal or coke.

In the method according to the invention, the carbonization gas present in the area of coking zone III is sucked off and burned with the supply of air in a combustion chamber which is essentially free of the solids present in the gasifier. The carbonization gas is burned essentially completely, ie without tar or other residues, essentially producing CO ₂ and H ₂ O. The area of the combustion chamber 4 and the closer surroundings, in which free oxygen is still present, is also referred to as oxidation zone IV. By appropriately controlling the air supply, the temperature of the combustion is preferably set to a value of approximately 1200 ° C. in order to achieve the aforementioned complete combustion.

The combustion gases then enter the reduction zone V below the oxidation zone IV, in which the carbon which has slipped out of the coking zone III reacts at temperatures above 800 ° C. on the one hand with the CO _{2 of} the combustion gases and form CO and on the other hand with the H ₂ O reacts, producing H ₂ and CO.

H ₂ and CO are the main energy sources of the product gas thus created, which also contains N ₂ , certain residual parts of CO ₂ and certain parts of impurity gases, the proportion of which may, however, be in the alcohol range and below. In contrast to other processes, however, the product gas obtained by the process according to the invention contains practically no naphthenes, aromatics, high hydrocarbons and other tar constituents.

The product gas escapes in the lower region of the reduction chamber 2 through the input region 5 , which is also referred to as a swirl chamber, of the product gas outlet 6 , which surrounds the pyrolysis container 1 in the form of a jacket and thus heats or heats up the pyrolysis material, and then at the upper end of the gasification container via a pipeline to enter a hot gas filter device 8 , in which the dust entrained from the reduction zone V or from the swirl chamber 5 is separated, after which the product gas reaches the consumer through the gas outlet 10 . The separated dust separates in the lower area of the hot gas filter 8 and is discharged through a rotary valve 11 into a dust combustion chamber 13 . The dust consists essentially of carbon and some mineral ash and is burned stoichiometrically in the latter with the supply of air, which takes place via an air supply line 9 into the entrance area of the dust combustion chamber 13 . Here again whereby the CO content of the product gas is further increased CO ₂ is formed, which subsequently enters through the output of the dust combustion chamber 13 into the reduction chamber 2 and gasified present there excess carbon to form CO.

The dust combustion, which can also take place above and / or below stoichiometric, allows the amount of carbon gasified in the reduction zone 5 to be controlled, so that the material throughput of the entire gasifier can also be controlled.

In summary, the following advantages are achieved with the method according to the invention:
1. The material used, apart from non-gasifiable mineral components, is completely gasified.
2. The product gas is free from tar contamination.
3. Fine-grained and / or chip-shaped fuel can also be gasified.
4. Only a small amount of mineral ash remains as waste.
5. The material throughput and thus the product gas output is controllable.

In Fig. 1 you can see the gasification tank, which has the shape of a long, upright cylinder with a tapered lid and bottom. The upper part of the gasification container is formed by the pyrolysis chamber 1 , the lower part of the gasification container is taken up by the reduction chamber 2 . The two chambers are separated by a conical taper 24 , which forms a funnel tapering downwards, through the opening of which an air supply line 9 , which enters the pyrolysis chamber 1 at the side, is passed and which merges into an annular nozzle holder immediately below this opening. Be found on the nozzle support radially disposed air jets 3, while between the inner edge of the hopper opening 26 and the nozzle holder in Fig. 1 in cross section, an annular gap is seen, which forms the passage opening 21st

The conical taper 24, which limits the pyrolysis chamber 1 to the bottom, has in cross section the shape of an overhanging nose and thus forms the location at the upper outer edge of the reduction chamber 2, ring tunnel-shaped and to downwardly open the combustion chamber 4, in which the air jet nozzles 3 in the radial direction radiate. In this case, carbonization gas is sucked in from the coking zone III of the pyrolysis chamber 1 through the annular gap 21 through the air jet emerging from the nozzles 3 and burned in the ring-shaped combustion chamber 4 . The combustion chamber 4 is essentially free of solid fuels, since said ring tunnel shape is formed by the overhanging edge of the conical taper 24 , so that the solid carbon material trickling through the annular gap 21 under gravity does not penetrate into the actual combustion chamber.

The product gas finally formed in the reduction chamber, more precisely in the reduction zone V, escapes at a temperature of more than 500 ° C. into the swirl chamber or the inlet 5 of the product gas outlet 6 , which surrounds the pyrolysis container in the form of a cylinder jacket. The inlet 5 is called a swirling space, because in this area a strong swirling up of coal dust and other small particles can be determined by the escaping product gas. An air preheating chamber 27 , in which the combustion air flowing in through the air inlet 18 is preheated and then introduced into the air supply line 9 , is located around the product gas discharge 6 as a further cylinder jacket.

There is a lock inlet 28 above the loading opening 19 .

In the lower cone in the reduction chamber 2 mineral ash is accumulated in an ash chamber 12, which is carried by an underlying discharge screw or rotary valve 14, into an ash container 15th From a scrubber tank 17, via the Kalkzufuhreinrichtung 25 as needed lime in the reduction chamber 2 and the Verwirbelraum 5 are introduced, which reacts with free or bound sulfur to CaS. The CaS, together with other dust constituents, is conveyed through the product gas into the product gas outlet 6 via the pipeline 7 into the hot gas filter device 8 , where the dust is separated off and fed to the dust combustion chamber 13 via a rotary valve 11 .

The dust combustion chamber 13 is connected at its entrance to the air supply line 9 , through which air for blowing the dust in the dust combustion chamber is blown in via a nozzle, not shown.

Since the gasification rate of the carbon in the reduction chamber can be adjusted by the combustion of the dust in the dust combustion chamber 13 , pressure measuring points 16 are arranged in the lower area of the pyrolysis chamber and in the product gas outlet, so that the afterburning is regulated via the pressure difference thus determined between the pyrolysis chamber 1 and the reduction chamber 2 can be. In particular, the pressure in the pyrolysis chamber 1 increases when the amount of carbon in the reduction chamber 2 becomes too large, so that the passage opening 21 may be blocked because the fuel cannot slide down.

In Fig. 2 a further preferred embodiment is described, in which the combustion chamber 4 is formed by a transverse funnel, the tapering inlet opening 22 abuts the wall of the carburetor tank and the outlet opening 23 is somewhat over the central axis of the reduction chamber 2 or the pyrolysis chamber 1 extends. The inlet area 22 of the funnel is connected directly to an annular space 20 in the coking zone in the lower area of the pyrolysis chamber 1 . The annular chamber 20 is arranged circumferentially on the wall of the pyrolysis container 1 , closed at the top and open at the bottom, so that carbonization gas but not solid fuels, apart from coal dust, can enter the annular space 20 . An air jet nozzle 3 is arranged in front of the inlet 22 and blows in the axial direction into the funnel-shaped combustion chamber 4 and sucks in the carbonization gas from the annular space 20 through the air jet entering the funnel at high speed. Due to the funnel shape, the combustion chamber 4 acts as a diffuser. Compared to the combustion chamber 4 , refractory-clad light sheets 29 are attached, which mainly direct the combustion gases emerging from the combustion chamber 4 in the direction of the reduction chamber 2 . The passage opening 21 for the coal from the coking zone III of the pyrolysis chamber 1 lies in front of the outlet region 23 of the combustion chamber 4 . The lower region of the pyrolysis chamber 1 is in turn funnel-shaped in the direction of the passage opening 21 so that the coal slides in the direction of this opening due to gravity.

Arranged in the axis of the air jet nozzle 3 is an ignition lance (not shown in FIG. 2) which can be inserted into the air jet nozzle in order to ignite the carburetor.

All other components of the carburetor of FIG. 2 correspond to the devices described in FIG. 1,.

Claims (12)

1.Procedure for the gasification of carbon-containing fuels by heating the fuel with exclusion of air with formation of carbonization gases in a carbonization zone (II), subsequent carbonization in a carbonization zone (III), oxidation of the coal (coke) formed and the carbonization gases with oxygen supply in an oxidation zone ( IV) and subsequent reduction with the help of coal originating from the coking zone in a reduction zone (V), characterized in that by blowing oxygen-containing gas (air) into a substantially solid-free oxidation zone (IV) the carbonization gas with separation of solid components of the carbonization zone (II) is sucked into the solid-free oxidation zone (IV) and essentially completely burned. 2. The method according to claim 1, characterized in that the combustion temperature of the carbonization gas in the oxidation zone (IV) between 1050 and 1300 ° C, preferably between 1100 and 1200 ° C. 3. Device for performing the method according to claim 1 or 2, consisting of a gasification tank with a top-loading and arranged in the upper part of the gasification tank pyrolysis chamber ( 1 ), a below the pyrolysis chamber ( 1 ) located reduction chamber ( 2 ), one between them Chambers arranged passage opening ( 21 ) for the coal from the coking zone (III) and a product gas exhaust ( 6 ) enclosing the vertical walls of the pyrolysis chamber ( 1 ) for heating the fuel, characterized in that an essentially at the lower region of the pyrolysis chamber ( 1 ) Solids-free and upwards against the pyrolysis chamber ( 1 ) or next to the pyrolysis chamber ( 1 ) or the reduction chamber ( 2 ) arranged combustion chamber ( 4 ) is provided, in its entrance area ( 22 ), which has a connection to the coking zone (III), at least an air jet nozzle ( 3 ) for sucking in carbonization gas from the coking zone (III) after the road hlpumpenprinzip is arranged with beam direction in the interior of the combustion chamber (4) and that the output portion (23) of the combustion chamber (4) is in gas flow direction with the reduction chamber (2) in combination. 4. The device according to claim 3, characterized in that the passage opening ( 21 ) is directly connected to the combustion chamber ( 4 ). 5. Apparatus according to claim 3 or 4, characterized in that the combustion chamber ( 4 ) and the air jet nozzle (s) ( 3 ) are arranged immediately below the pyrolysis chamber ( 1 ) in the region of the passage opening ( 21 ). 6. The device according to claim 5, characterized in that the combustion chamber ( 4 ) below a conical taper ( 24 ) at the lower end of the pyrolysis chamber ( 1 ) is designed as an annular combustion chamber ( 4 ) and that several light jet nozzles ( 3 ) radially at one central Air supply line ( 9 ) opening directly underneath the taper are arranged between a circular nozzle holder, the radius of which corresponds to or is slightly larger than the smallest radius of the conical taper ( 24 ), and the edge of the conical taper ( 24 ) as a passage opening ( 21 ). an annular gap is formed ( Fig. 1). 7. The device according to claim 5, characterized in that the combustion chamber ( 4 ) is designed in the form of a transverse funnel, at the input ( 22 ) at the tapered end of the funnel, the air jet nozzle ( 3 ) is arranged axially radiating, and that this inlet ( 22 ) is connected to an upwardly closed and downwardly open annular space ( 20 ) in the lower region of the coking zone, which essentially contains only carbonization gas ( FIG. 2). 8. The device according to claim 7, characterized in that an insertable into the nozzle ignition lance for igniting the gasification device is arranged in the axis of the air jet nozzle ( 3 ). 9. The device according to one or more of claims 3 to 8, characterized in that the product gas discharge ( 6 ) in the upper region of the gasification container via a pipe ( 7 ) with a hot gas filter device ( 8 ) is connected, at the lower end of which a rotary valve ( 11 ) for the discharge of accumulated dust is arranged in a dust combustion chamber ( 13 ), which has a connection to the air supply line ( 9 ) at its entrance and is connected to the lower area of the reduction chamber ( 2 ) at its exit. 10. The device according to one or more of claims 3 to 9, characterized in that in the lower region of the pyrolysis chamber ( 1 ) and in the inlet region ( 5 ) of the product gas discharge ( 6 ) pressure measuring points ( 16 ) for measuring and monitoring the pressure difference between the pyrolysis chamber ( 1 ) and reduction chamber ( 2 ) are provided. 11. The device according to one or more of claims 3 to 10, characterized in that at the lower end of the gasification container under the reduction chamber ( 2 ), a discharge screw or a rotary valve ( 14 ) for discharging the ash from the ash chamber ( 12 ) of the reduction chamber ( 2 ) is arranged in an ash container ( 15 ). 12. The device according to one or more of claims 3 to 11, characterized in that a lime container ( 17 ) via a lime supply device ( 25 ) is connected to the reduction chamber ( 2 ).