DE2927240A1 - METHOD AND SYSTEM FOR GASIFYING STUFFED FUELS - Google Patents

Abstract

Fuel such as bituminous coal, lignite, wood, straw and similar, is carbonized at approximately the atmospheric pressure in a first stage by indirect heating between 300 and 600`C while stirring constantly (1). The hot gases released are mixed with preheated air and partially burnt (27) in a second stage. Simultaneously, they are thermally cracked at temperatures comprised between 850 and 1200`C, and they are passed through a reaction zone (35) comprised of low carbonization coke obtained during the first stage. In a third stage, the coke is subjected to a partial combustion, for example by means of air and steam. The gas mixture being initially at a temperature comprised between 900 and 1200`C is sucked through a reaction zone formed with the low carbonization coke where the gas temperature is reduced due to an endothermal reaction and where the calorific capacity of the gases is simultaneously increased. Those gases and the gases coming from the second stage are conveyed towards heat-exchangers (44 to 46) and to gas scrabbers (61).

Description

Process and system for gasifying lumpy

Fuels The invention relates to a method for gasifying Lumpy fuels, such as bituminous coal, lignite, wood, straw and the like. Like., Under at least approximately atmospheric pressure, in which the fuels in a first stage of the process by indirect heating at temperatures between 300 and 600 OC carbonized under constant circulation and in a second process stage the hot smoldering gases by mixing with preheated air, at the same time thermally cracked at temperatures of 850 to 1200 OC and then passed through a reaction zone formed from the low-temperature coke in the first stage will.

The invention also relates to a system for carrying out a such procedure.

In the past few decades there has already been a large number of procedures and plants for gasification, pyrolysis and / or high temperature distillation of fuels of the most varied kinds have been developed, at least partially also in the Have been put into practice. It was always an initial one Smoldering and / or coking of the abandoned fuels in the absence of air by direct or indirect heating, through which the volatile components if necessary expelled from the solid fuels with thermal cracking and deposited will. The coke formed during this process could - depending on its type and composition of the fuels used - either deducted as a salable end product or by a more extensive thermal treatment by adding steam are decomposed into combustion gases, preferably containing CH4, CO and H2. So is z. B. in DE-PS 972 468 a method for generating a fuel gas from bituminous Fuels described, in which the fuels in a first chamber of a usual Degassed coke oven block and the distillation gases obtained via pipes and a template can be transferred into a second, identically designed chamber, in which the glowing, already fully cooked distillation residues from a previous one Find degassing process. This chamber is penetrated from the outside through the chamber walls Heat supplied. To control the composition of the fuel gases generated, finely atomized fuel, e.g. B. oil or tar, together with the hot raw gas inserted into the second chamber. The finely atomized fuel in the connecting line Together with the hot raw gases, a warm aerosol forms in the gap volume of the glowing coke is split. In addition to spraying liquid fuel water or steam can also be added to the raw gases to be in to carry out the water-gas reaction with the glowing coke of the second chamber. To A fuel gas enriched in terms of its calorific value can be used in this process are generated, but the coke in the second chamber takes only a very small amount Quantities participate in the reactions, so that gasification of this coke is not or in occurs only to an insignificant extent in practice.

So this process is primarily based on using only fuels low impurities, d. H. low ash and sulfur content as input materials limited.

A complete conversion of e.g. B. hard coal or lignite with high sulfur and ash content is not easily possible because the resulting Coke is difficult to process further.

In DE-OS 24 08 461 is a method and a system for generating of synthesis gas using a tapping generator charged with coke described, in which the fully cooked coke batch of the generator in the heated state the upstream coking furnace via a pressure lock into the tapping generator is introduced.

In this way, the heat content of the coke remains for the downstream Gasification process received. Some of the distillation gases obtained are used for indirect heating is used in the coking chambers while another part is in the Tapping generator is conducted.

The gasification agent consists of a mixture with hot water Saturated oxygen, to which air can be added if necessary, and from water vapor. This gasification agent passes through a heat exchanger with temperatures 0 between 200 and 300 C in the lower part of the previously charged with hot coke Tapping generator. The hot combustion gases are dedusted and give their heat content to waste heat boiler before it is fed to a wash cooler as synthesis gas, The coking gases can be mixed with the gasifying agent formed from oxygen and water vapor mixed and introduced into the coke filling of the tapping generator.

The disadvantage of this known procedure is, on the one hand, that it is extraordinary high technical equipment costs and, on the other hand, the relatively high temperatures of the generated synthesis gas.

In a method for extraction described in DE-PS 424 724 of low-boiling hydrocarbons from carbonization gases are carbonized coal in one The jacket-heated rotary drum is carbonized, the carbonization gases are separated from the carbonization coke withdrawn from the drum and placed in an externally heated tube rsys-em thermally cracked at temperatures of approx. 700 OC, so that the split off low-boiling hydrocarbons. A gasification of the coke is not provided.

Furthermore, a method for generating fuel gases is already over lumpy garbage and other waste materials described in DE-PS 24 32 504, at which the garbage untreated in a smoldering drum at temperatures between 300 and 600 OC carbonized, the carbonization gases separate from the solid ones Smoldering residues withdrawn and in a further process stage by adding predetermined Amounts of combustion air heated to approx. 1000 OC and thermally cracked in the process be made, whereby they are made of glowing coke and possibly

flow through other carbon carriers formed reaction zone. Included the strongly endothermic water gas reaction takes place, through which the sub-stoichiometric combustion and fractions of elementary elements resulting from cracking Carbon (soot) together with water vapor and carbon dioxide in appropriate amounts transferred to carbon monoxide and hydrogen. Because of the heat consumption In these reactions there is an intensive cooling of the approx. 1000 OC hot Crack gases to a withdrawal temperature of approx. 500 OC within a flow path of approx. 500 mm.

In this process, the glowing foreign coke remains in the reaction zone largely uninvolved in the reactions taking place, d. H. he serves on the one hand as a heat store and on the other hand as a carrier for the soot particles of extraordinary large surface. The solid carbonization residues discharged from the rotary drum are sorted into smoldering coke, other usable as well as worthless residues. A gasification of the low-temperature coke is not provided for in this known method.

The object of the invention is to provide a method and a system for gasifying of ash- and sulfur-rich bituminous fuels to show in which the continuously generated fuel gases are largely free of environmentally harmful impurities, z. B. hydrogen sulfides, and are at the same time a relatively high calorific value own.

This object is achieved in that in a third Process stage of the low-temperature coke by introducing a gaseous oxygen carrier is partially burned in a sub-stoichiometric ratio that the obtained between initially 900 to 1200 OC hot gas mixture through an immediately following, is sucked through the reaction zone formed from the low-temperature coke, in which through endothermic reactions lower the gas temperatures and at the same time the calorific value the gases is increased, and that then these gases with the fuel gases from the second process stage mixed and the mixture obtained in a known manner heat exchangers and is fed to washers.

This process according to the invention has advantages over known fuel gasification processes a number of advantages, including the extremely simple process management and control and on the other hand in the quality of the fuel gas, which one high calorific value and also practical with ash or sulfur-rich feed materials Free of sulfur, chlorine-heavy metal compounds and harmful hydrocarbons is. The above-mentioned method also offers the possibility of fuels can be effectively and completely gasified with ash contents of up to 30% by weight. Besides can also use other different fuels, such as ash-rich coking coal, lignite, Peat, and also wood, wood shavings, straw and the like, serve as feed materials.

According to the invention, the coke in the fuel gas reactor fulfills several Functions. Once it serves to support the cracking processes of the carbonization gases their substoichiometric partial combustion, on the other hand they are stored at the Partial combustion and the cracking process produced soot particles on the smoldering coke grains starting with extraordinarily large surfaces are formed. the Carbonization gases react with the deposited soot, with consumption of noticeable Heat from the smoldering gases carbon monoxide and hydrogen according to the well-known water gas equations arises. Corresponding processes also play out for the conversion of the Partial combustion of the smoldering coke in the lowest zone produces gas mixtures. By the continuous burning of the coke in the lowermost reaction zone results a gradual lowering movement of the entire coke filling over the various Reaction zones.

The speed of this gradual lowering movement and thus also the intensity of the gasification of the low-temperature coke can be achieved in the simplest way by itself the corresponding adjustment of the amounts of combustion air and steam is controlled will.

The admixing of the fuel gases generated by the sensible heat produced steam in the combustion air has the advantage of being intensified the water gas reactions in the third process stage.

For a continuous and even process it is useful if, on the one hand, the carbonization gases and, on the other hand, the combustion air for the smoldering coke evenly distributed over the entire reactor cross-section are introduced into the reaction zones formed from the low-temperature coke. To this The purpose is partial combustion with simultaneous thermal cracking of the carbonization gases with intensive turbulence in one of the lumpy coke containing the lumpy coke Water gas reaction zone separate reaction space. For even distribution the combustion air for the low-temperature coke can expediently come from a pressure chamber under the ash conveyor through this into the combustion zone to be introduced.

The plant for carrying out the method includes an indirect over their hollow jacket, preferably heated by exhaust gases, and one with the Smoldering gases and the smoldering coke from the smoldering drum are fed in shaft-shaped Fuel gas reactor as well as auxiliary units, air preheaters and scrubbers for the generated Fuel gases, according to the invention in the fuel gas reactor an upper partial combustion and a cracking zone for the carbonization gases, a subsequent one filled with carbonization coke Water gas reaction zone for the cracked carbonization products, followed by a discharge zone for the fuel gases generated, followed by a water gas reaction zone filled with low-temperature coke for the reaction products from the partially burning coke and then downwards then a hot combustion zone for the low-temperature coke with feed lines for the preheated combustion air and steam is formed.

Appropriately, is between the upper partial combustion and cracking zone a gas-permeable zone for the carbonization gases and the adjoining water-gas reaction zone Partition wall provided with advantage as a uniformly perforated ceramic plate is trained.

Further advantages are the subject of subclaims.

In the following, embodiments of an inventive Gasgenerating arlage described in detail with reference to the drawing. Own: Fig. 1 the block diagram of a first embodiment, Fig. 2 shows the fuel gas reactor the system according to FIG. 1 in an enlarged schematic representation, FIG. 3 the block diagram another version with joint charging of the fuel gas reactor with carbonization gas and smoldering coke.

The gas generating plant shown in Fig. 1 contains as main units a smoldering drum 1, a fuel gas reactor 2 and a gas engine 3.

The lumpy bituminous fuels are fed through a funnel 4 with locks 5, 6 arranged in an entry shaft 7 and a horizontal conveyor 8 inserted into the entry end of the rotary drum 1. The rotary drum 1 consists of the actual smoldering drum, in which hollow, essentially longitudinally directed Internals 11 are arranged in the form of longitudinal ribs or blades. This smoldering drum 10 is surrounded by a jacket 12, which is connected via a line 13 to the exhaust system 14 of the gas engine 3 is in communication. This is how the heating takes place Rotating drum indirectly through the exhaust gases from the gas engine 3, which are at a temperature of approx. 600 OC. For the start-up and / or emergency operation is an additional burner on the drum discharge side 15 provided, the exhaust gases flow into the shell space 12 and the carbonization of the fuel inside the drum. In normal operation, however, is sufficient the heat supply in the exhaust gases of the gas engine 3 for complete carbonization of fuels also with high ash and water content to intensify the Heat transfer between the hot exhaust gases and the carbonized material are the hollow internals 11 flowed through by the hot exhaust gases, which on the one hand increase the heat transferring surfaces and on the other hand through the conveying effect These internals also improve the heat transfer to the task or Schwelgut. With an appropriate design of these internals 11, their interiors can be enlarged that they themselves form the jacket 12.

After flowing through the internals 11 or the drum shell 12 the exhaust gases are indicated via a line 16 with metering valve 17 atmosphere discharged. The line 16 is through a branch line 18, a fan 19 and a Metering valve 20 with the burner 15 or the distribution chamber 21 on the inlet side connected in the drum shell 12 to the temperature of the heating gases by admixing predetermined, to control gas quantities that have already cooled down.

The inclination of the rotary drum 1 can be adjusted in the usual way on - not shown - bearing and drive rollers stored.

The Schwelyas generated in the rotary drum 1 is at 0 temperatures from 400 to 500 C at the discharge end of the drum via pipes 22 to a burner 23, which opens into the upper part of the fuel gas reactor 2. Direct a feed line 25 for the combustion air ends upstream of an ejector part 24, those in the ejector part 24 and the adjoining diffuser 26 of the burner 23 with the carbonization gases to obtain partial combustion of the carbonization gases intensively is mixed.

The fuel gas reactor 2 has one of internals in its upper part free chamber 27, in which an intense Swirling the partially burned carbonization gases flowing in through the burner 23 takes place. In this The thermal cracking takes place in the chamber through the substoichiometric partial combustion Carbonization gases heated to approx. 1000 to 1200 OC take place.

This chamber 27 is delimited at the bottom by a partition 28, which consists of a ceramic plate of approx.

100 to 200 mm thick, in which a large number of holes 29 are provided in a suitable size. The flow resistance of the or plate 28 or the holes 29 is selected so that in chamber 27 a slight overpressure prevails, the one over the entire cross section of the shaft-shaped fuel gas reactor uniform flow through the plate 28 is guaranteed.

At a predetermined distance below the gas-permeable partition 28 is at least one entry conveyor 30 is provided as an entry organ having hydraulically or pneumatically operated piston valve 31. This entry conveyor 30 is the coke from the discharge end of the rotary drum 1 via a Slide 32 and a pressure-tight Dosierradeinrichtung 33 supplied. The entry conveyor 30 charges the fuel gas reactor 2 via a lateral, sealed inlet opening 34 with the coke produced in the rotary drum 1. The charging of the fuel gas reactor takes place in such a way that a sufficient height of the coke bed 35 in the fuel gas reactor is present At a predetermined distance below the entry conveyor designed as an annular channel 36 is provided for the exhaust for the combustion gases, which consists of a Variety of radial 36 & openings in the reactor wall.

The reactor bottom is through a discharge conveyor 37 for the ash and slag of the coke formed by a motor 38 via a gearbox 39 is driven.

Below this discharge conveyor 37, which is designed as a rotating grate, is a discharge chute 41 sealed by piston valve 40 is provided, through which the ashes or ashes that have been loosened and crushed by means of the discharge conveyor 37

Slag is discharged. In the interior of this discharge chute 41 open air and steam lines 42.

From the fuel gas vent, which is designed as an annular channel 36, one leads Hot gas line 43 to an air preheater 44 and to evaporators 45, 46. The air preheater is via a hot air line -47 with one to the pipe 25 via a metering valve 49 leading air line 48 and an air line 50 and another metering valve 51 connected to the air connections 42. In the evaporators 45 and 46 are means Dosing pumps 53, 54 supplied amounts of water evaporated, which once via a Steam line 55 into the hot air line 48 downstream of the valve 49 and to the other Via a further steam line 56 into the hot air line 50 downstream of the metering valve 51 are fed in.

The fuel gases flow from the heat exchangers 44 to 46 via a Gas line 60 in a washer 61 shown only schematically, in which Pollutants and other by-products may be separated in several stages.

The cleaned fuel gas is fed to the gas engine 3 via a line 62, the output shaft of which is coupled to a generator 63.

The following is the operation of the system described above and in particular the fuel gas reactor (with reference to FIG. 2) described in detail.

The bituminous fed via an endless conveyor (not shown) Fuels such as sulphurous and ash-rich hard coal, lignite, peat, wood and Wood waste as well as straw and other organic components pass through the funnel 4 by alternately actuating the piston slides 5, 6 in the entry shaft 7, from which it by means of the screw conveyor 8 into the interior of the smoldering drum 10 must be entered. After drying in the left part of the smoldering drum in FIG. 1 The degassing of the fuels starts at approx. 200 OC, which can reach temperatures of approx. 500 OC at the right discharge end of the drum is continued continuously. The carbonization gases are released by the ejector effect of the burner 23 via the lines 22 at temperatures of approx. 400 to 500 OC. At the same time the coke is used Via the discharge chute 32, the metering wheel 33 and the entry conveyor 30 in the Fuel gas reactor 2 entered below the partition 28.

The reactions occurring in the Schwelgafblaufe are based on the following 2 described in detail. The carbon dioxide gas is produced by the admixture of metered amounts of air in the burner 23 partially burned and flow with comparatively high kinetic energy in the empty chamber 27, in which intense turbulence of gases 1 take place. These eddy currents cause that in the entire chamber a temperature of about 10C0 OC prevails, at which the thermal cracking of the Carbonization gases take place with a high degree of efficiency. Maintaining the temperature is ensured by the introduction of appropriate amounts of air and thus through the intensity of the carbonization gas combustion achieved. The partially burned and cracked smoldering gases flow through the holes 29 in the partition 28 into the coke bed 35, the surface of which is heated to a temperature of around 900 to 1000 oC. The cracking process and in the sub-stoichiometric combustion of the carbonization gas-forming fractions elemental carbon (soot) is deposited on the surfaces of the charcoal grains and react with the combustion products as well as with the water vapor under carbon monoxide, Hydrogen and possibly methane formation. These processes are strongly endothermic, so that from the partial combustion and cracking zone I through the partition 28 into the water gas reaction zone II inflowing gases in the coke layer 35 from initially 900 to 1000 OC to a Extraction temperature of approx. 500 OC cooled by the endothermic reaction processes through the openings 36a in the refractory masonry walls of the reactor 2 and the annular channel 36 are discharged (withdrawal zone III) via the line 50, the Annular channel 42 and the openings 42a in the reactor wall in the space 41 under the Combustion air introduced by the conveyor flows through the spaces between the conveyor grate bars 37 through and there is a partial combustion at V directly above the conveyor grate 37 of the smoldering coke in a temperature range of 1000 to 1200 OC. The intensity this partial combustion is achieved by adjusting the air supply by means of the metering valve 51 reached. The gases formed by the partial combustion of the low-temperature coke flow through the zone IV of the coke bed and are through the outlet openings 36a, the annular channel 36 and the fuel gas line 43 withdrawn from the fuel gas reactor.

Due to the steam added to the combustion air, they take place with this flow through the coke filling in reaction zone IV also strongly endothermic reactions Increase in calorific value and at the same time Temperature decrease - corresponding to the reactions in zone II that shown in FIG The main components and functional features of the system correspond to those according to FIG. 1. The components which correspond to one another have reference numerals extended by 100 marked. This system is particularly suitable for feed materials which the smoldering coke accumulating in the smoldering drum is on the one hand sufficiently granular is to together with the carbonization gases via the burner 123 in the fuel gas reactor to be able to be introduced, and 1 this a coke bed of sufficient gas permeability bilc.et, on the other hand, however, the coke should be removed from the combustion gases in room 127 are also swirled around a reactor over the entire cross section of the fuel gas To enable largely uniform deposition.

With regard to the investment costs, this version offers the Advantage that the separate entry conveyor 30 for the Schwelkoks'die gas-tight Dosing wheel sluice 33 can be omitted. A continuous addition to the coke bed 135 in the reactor 2, the perforated partition is missing in this embodiment 28 according to FIG. 1. It follows that the variant according to FIG. 3 is technically simpler is built up that the control of the process sequence, however, fewer options for intervention offers, since all of the smoldering coke extracted from the smoldering drum 410 is immediate enters the fuel gas reactor. The other units (such as heat exchangers, scrubbers, Gas engine etc.) of this system correspond to that of FIG. 1, so that on their graphic representation could be dispensed with.

The invention is not limited to the embodiments shown and described limited. For example, the preheating of the combustion air and / or the steam generation for the water gas reaction in the third process stage further utilization of the waste heat of the exhaust gases of the gas engine take place.

There is also the possibility of thermal cracking the combustion gases obtained on the one hand and the gasification on the other hand of the low-temperature coke obtained fuel gases to be withdrawn separately from the fuel gas reactor and to further treat them according to their possibly different chemical composition.

Although the utilization of the fuel gases in a gas engine is one of the most energetic the most favorable options, since the exhaust gases from the engine are used for heating the smoldering drum can be used, the generated fuel gases can also be used for other purposes for heating purposes or as a chemical raw material. In In this case, the indirect heating of the smoldering drum by the generated, approx. 600 OC hot fuel gases take place themselves, which then pass through the hollow jacket or the hollow internals in the drum are passed through.

For special purposes, especially for the use of fuels with a high ash content, in which the incombustible components stick together and sintering, another process and plant variant is suitable for which the smoldering coke in the reactor shaft wholly or partially in the state of a calmed fluidized bed (fluidized bed) is added. This is done in the bottom Air chamber creates a sufficiently high overpressure that is too even over the Gas flows distributed in the bottom cross-section in the low-temperature coke filling. Should the to the Generation of the fluidized bed the amount of gas required for partial combustion If the amount of air required for the coke is exceeded, this can cause combustion air either a corresponding partial amount of generated fuel gas and / or a corresponding one Partial amount of exhaust gases are added. At least some of these exhaust gases from the internal combustion engine (gas engine) operated with the generated fuel gas Thermally cracked in the hot partial combustion zone. The mixed fuel gases on the other hand preferably have a fluidic carrier function for generation of the fluidized bed.

Claims (25)

Claims 1. A method for gasifying lump fuels, such as bituminous coal, lignite, wood, straw and the like, at least approximately Atmospheric pressure at which the fuels are carried out in a first process stage indirect heating at temperatures between 300 and 600 oC with constant circulation carbonized and in a second process stage the hot carbonization gases by mixing partially burned with preheated air, at the same time at temperatures from 850 to 1200 OC thermally cracked and then cracked by one from the low-temperature coke in the first Stage formed reaction zone are passed through, characterized in that In a third process stage, the low-temperature coke is introduced by introducing a gaseous one Oxygen carrier (air) is partially burned in a substoichiometric ratio, that the generated gas mixture between initially 900 and -1200 OC by a immediately following reaction zone formed from the low-temperature coke is sucked through is, in which by endothermic reactions the gas temperature is lowered and at the same time the calorific value of the gases is increased, and that then these fuel gases and the Fuel gases from the second process stage in a known manner and heat exchangers Be fed to washers. 2. The method according to claim 1, characterized in that that the combustion and gasification air for the low-temperature coke to achieve the water-gas reaction metered amounts of steam are added. 3. The method according to claim 1 or 2, characterized in that the Fuel gases from the second process stage with the fuel gases from the third process stage mixed and fed together to the air preheaters and washers. 4. The method according to claim 1, characterized in that the partial combustion with simultaneous thermal cracking of the carbonization gases with intensive turbulence of the reacting gases in one of the water gas reaction zone containing the lumpy coke separate reaction chamber is carried out and that the reaction products obtained the water gas reaction zone is evenly distributed over its entire cross section flow through. 5. The method according to any one of the preceding claims, characterized in, that the generated fuel gases in a range between the second and the third Process stage are removed. 6. The method according to any one of the preceding claims, characterized in, that the slag and ash formed in the third process stage are mechanically comminuted is discharged. 7. The method according to any one of the preceding claims, characterized in, that the smoldering coke in the third process stage from the combustion and gasification air The flow is evenly distributed over the entire cross section, and that-the Amount of Schwelkoks this third process stage is adjusted so that by the endothermic water gas reactions that take place the fuel gases generated are sufficient fed to the heat exchangers cooled at temperatures in the range from 400 to 700 OC will. 8. The method according to any one of the preceding claims, characterized in, that the generated fuel gas is used in an internal combustion engine, the exhaust gases and represent the heating medium for the charring in the first process stage. 9. The method according to any one of the preceding claims, characterized in, that the intensity of the gasification of the smoldering coke and thus the height of the reaction zone in the third process stage by adjusting the coke introduced into the low-temperature coke Amounts of combustion air is controlled. 10. The method according to any one of the preceding claims, characterized in, that the combustion air for the smoldering gases and for the smoldering coke through the approx. 500 OC hot fuel gases are preheated. 11. The method according to claim 2, characterized in that the dem Smoldering coke supplied in metered amounts of steam by utilizing the sensible Heat of about 500 OC hot fuel gases is generated. 12. The method according to any one of the preceding claims, characterized in, that the smoldering gases and the smoldering coke from the first process stage together are fed to the second process stage. 13. The method according to any one of claims 1 to 11, characterized in that that the carbonization gases and the carbonization from the first process stage are each separate withdrawn and fed to the second process stage. 14. Plant for carrying out the method according to one of the preceding Claims, with a smoldering drum heated indirectly via its hollow jacket and a shaft-shaped one charged with the smoldering gases and the smoldering coke from the smoldering drum Fuel gas reactor as well as air preheaters and a washer for the fuel gases generated, characterized in that the fuel gas reactor has an upper partial combustion and Crack zone I for the smoldering gases, followed by an adjoining zone filled with smoldering coke Water gas reaction zone II for the cracked carbonization gases, followed by a common discharge zone III for the fuel gas generated, then one with Smoldering coke-filled water gas reaction zone IV for the reaction products of the partially burning coke and then a hot combustion zone V for the low-temperature coke with feed lines (42, 142) for the preheated combustion air and possibly the steam. 15. Plant according to claim 14, characterized in that in the upper, Partial combustion and cracking zone I designed as a free swirl chamber (37) Ejector burner charged with the carbonization gases and the preheated air (23, 123) is arranged 16. Plant according to claim 14 or 15, characterized in that that between the upper partial combustion and cracking zone I and the adjoining one Water gas reaction zone II a gas-permeable partition (28, 29) is provided. 17. Plant according to claim 16, characterized in that the partition (28) is an evenly perforated ceramic plate. 18. Plant according to one of claims 14 to 17, characterized in that that on the fuel gas reactor (2) below the partition (28) an entry device (30) is arranged for the low-temperature coke. 19. Plant according to one of claims 14 to 18, characterized in that that the trigger (36) for the generated fuel gases as an annular channel on the outer circumference of the Fuel gas reactor (2) is formed, which over a plurality of in the circumferential direction evenly distributed radial openings (36a) with an inclined underside with the coke filling (35) is in connection in the fuel gas reactor (2). 20. Plant according to one of claims 14 to 19, characterized in that that a discharge conveyor (37 to 39) for the ash at the bottom of the fuel gas reactor (2) and slag and connections (42, 42a) for the preheated combustion air and possibly the steam are arranged. 21. Plant according to claim 20, characterized in that under the A discharge conveyor designed as a rotating grate (37) has a sealed distribution chamber (41) is provided for the combustion air, which the combustion air through the rotating grate (37) evenly distributed over the entire cross-section of the reactor introduced into the carbonization gas filling. 22. Plant according to one of claims 14 to 21, characterized in that that the entry conveyor (30) for the low-temperature coke has a piston valve as a conveyor and sealing member. 23. Plant according to claim 14, characterized by a common Rotary drum discharge (132) for the carbonization gases and the carbonization coke. 24. Plant according to one of the preceding claims, characterized in that that to form a so-called calm fluidized bed in the distribution chamber (41) a sufficiently high gas pressure is set. 25. Plant according to claim 24, characterized in that the fluidized bed generating medium in the distribution chamber (41) is a mixture of fuel-burning air, Steam, recirculated fuel or carbonization gas generated in the reactor and / or exhaust gas from the gas engine operated with the fuel gas.