EP1436366A1 - Method for the production of current from material containing carbon - Google Patents

Abstract

A method for the production of current from material containing carbon, especially from biomass (2), wherein the material is allothermally gasified in a reactor (1) producing a fluidized bed (5). The gas produced after flowing through cyclone separator is cooled in successive steps. According to said individual steps, harmful substances are removed from the gas by means of condensation and in at least one step harmful substances are also chemically removed from the gas, enabling effective power to be obtained effectively without any problems. The invention is characterized in that part of the gas is combusted in burners in order to heat the fluidized bed (5) and in that the remaining part of the gas is combusted in internal combustion engines (8) and preferably electro-chemically recycled.

Description

 "Process for generating electricity from carbonaceous material"

The invention relates to a method for generating electricity from carbon-containing material, in particular from biomass, the material being gasified allothermally in a reactor to produce a fluidized bed, the gas generated being cooled in successive steps after passing through a cyclone, pollutants being removed in the individual steps the gas by condensing and pollutants are additionally removed chemically from the gas in at least one step.

Methods of the type in question are already known in practice. Biogenic substances such as biomass, organic waste, sewage sludge or liquid manure, animal waste and other carbon-containing compounds are gasified using different processes.

In allothermal gasification processes, the material to be gasified is indirectly heated by external heat. Allothermal gasification processes are particularly important for the future because, unlike autothermal processes, they do not introduce atmospheric nitrogen into the process gas through partial combustion and therefore work with low levels of pollutants. In the case of autothermal processes, the material to be gasified is heated directly by combustion with air or oxygen. This can result in a high pollution of the gas as a result of an unregulated carbonization.

The steam reformer process with circulating fluidized bed is of particular importance in the allothermal processes. In this method, the heat transfer medium, preferably sand or corundum, is heated indirectly to the reaction temperature as a fluidized bed via heat exchangers. The material to be gasified is entered into this fluidized bed. Steam injected into the reformer from below serves to circulate and fluidize the fluidized bed. In addition, the injected steam is used for the thermo-chemical digestion of the biomass.

Allothermic gasification processes are particularly advantageous because they are insensitive to moisture fluctuations in the material to be gasified. With Even the finest dusts can be easily gasified using this process. In addition, this method is insensitive to fluctuations in the geometry of the effective reaction space. It is also of great advantage that almost all carbon compounds can be gasified. The gasification can be regulated at a constant, ideal temperature level, the circulating fluidized bed ensuring a large thermo-chemical breakdown and preventing sintering by ash fractions, which tend to sinter even at low temperatures.

It is known that in allothermic gasification processes, for example the battery parts process, the exhaust gases from the residual combustion process of the material to be gasified are used to heat the heat transfer medium, preferably sand or steel balls, to approximately 1000 ° C. This heat transfer medium is fed to the gasification process and supplies the thermal energy for gasification.

The disadvantage here is that both the exhaust gases and their deposits on the heat transfer medium contaminate and dilute the gas.

Another disadvantage is that the gasification does not take place at a uniform temperature level, but takes place unregulated between 500 and 1000 ° C.

The high inlet temperature of the heat transfer medium of approx. 1000 ° C in the gasification process leads to the sintering and accumulation of residual ash on the heat transfer medium. The gas then has to be cleaned using a dust filter or wet gas cleaning.

When using this process to generate gas in gas engines, the contaminated gas is cleaned in a waste heat boiler via a dust filter with subsequent quenching and fine cleaning.

The current problems of residual gas loads require new approaches, since the waste heat boilers quickly die and the efficiency of the systems decreases.

According to a further process, biomass is finely ground, predried and pelletized and fed to the gasifier. The thermal gasification energy is determined by a Mixture of gas, pure oxygen and steam as hot fluidizing gas supplied to the biomass. The rest of the resulting gas is fed into a waste heat boiler and cleaned in the subsequent dust filter and quench.

In these known processes, it is disadvantageous that pure oxygen must be supplied to the gas, that impurities in the gas can be deposited in the waste heat boiler, and that the fluidizing gas in the reactor has different temperature zones. A very special disadvantage is that the biomass has to be pretreated in a complex manner. It is also state of the art to cool and purify the gas without an upstream cyclone. The combustion air of a gas engine is then fed to a heat generator in combination with an oil burner.

All of the above-mentioned processes have in common that the overall energy recovery of the raw material to be gasified and the gas produced is not optimized. It is also problematic that the essential process steps can only be carried out with the formation of considerable impurities and pollutants.

The present invention is therefore based on the object of designing and developing a method of the type mentioned at the outset in such a way that effective energy generation can be implemented without problems.

According to the invention, the above object is achieved with regard to a method for generating electricity from carbon-containing material with the features of patent claim 1. According to this, a method for generating electricity from carbon-containing material is characterized in that part of the gas is burned in burners for heating the fluidized bed and the remaining part of the gas is burned in internal combustion engines and is preferably used electrochemically.

In the manner according to the invention, it has been recognized that the combustion of part of the resulting gas reduces the supply of extraneous gas. In this respect, the process is particularly economical. Furthermore, it has been recognized that it is precisely the combination of the features of the labeling part, namely combustion of part of the gas in burners and combustion of the rest of the gas in combustion internal combustion engines for electro-chemical recycling, a particularly effective energy production realized. In a particularly refined manner, the method according to the invention makes it possible to use the resulting gas in two ways, namely as a supplier of electrical energy and thermal energy.

The exhaust gases from the internal combustion engines and / or the burners could be used for the thermochemical digestion of the material to be gasified. This specific embodiment advantageously uses waste products of the process for the preparation of the material to be gasified, which are produced anyway.

The exhaust gases from the internal combustion engines and / or the burners could be used to heat and / or dry the material to be gasified. This specific embodiment of the method advantageously uses thermal energy of the method in order to prepare the material to be gasified in such a way that it exhibits particularly favorable reaction properties in the fluidized bed due to its dryness.

The exhaust gases from the internal combustion engines and / or the burners could be used to heat the combustion air of the gas in the burners or a post-combustion boiler. In this specific embodiment, it is advantageous that the fluidized bed can be heated in an energetically particularly advantageous manner, since the energy supply to the burners is reduced by using the exhaust gases.

The exhaust gases from the burners could be directed into a waste heat boiler for steam generation. In this specific embodiment, the energy content of the exhaust gases is used to support the thermo-chemical digestion.

The exhaust gases from the burners could be fed into the waste heat boiler via a steam superheater. This ensures that the process steam required for the thermo-chemical decomposition of the carbon is brought to a suitable reaction temperature. The process steam also serves to fluidize the fluidized bed. In addition, it is advantageously realized that the burner output to be provided is reduced and the circulation of the fluidized bed is accelerated when it comes into contact with the biomass. A condensation steam turbine could be driven by the waste heat boiler. When using highly effective condensation steam turbines, energy is released in the form of warm air in an air condenser at a low temperature level of approx. 45 ° C. This can be channeled through biomass temporarily stored in the warehouse in order to pre-dry it. This significantly improves the overall energy balance. Due to this specific configuration, moist raw materials can also be stored. The targeted drying in this form avoids drying in intermediate storage spaces, which causes transport and storage costs. In addition, when raw materials are stored temporarily, their energy content decreases due to the formation of fungi and lignin degradation.

Part of the steam for the thermal decomposition of the material to be gasified could already be introduced into the screw conveyor of the material to be gasified. As a result of this measure, the material to be gasified is not only dried further during transport but at the same time heated, which has a positive influence on the course of the gasification reaction.

The carbon in the residual ash separated in the cyclone could be fed directly from the cyclone into a steam boiler and burned there. Due to this specific design, even waste products, namely the residual ash, are still used.

Heavy metal compounds could be melted down in the steam boiler. In this specific embodiment, the steam boiler serves as a slag burner boiler that burns the carbon of the residual ash so that the ash is slagged on the one hand and all carbon compounds are used in thermal energy in the form of steam on the other hand. The carbon in the residual ash is burned at a higher temperature level so that the silicon components melt the heavy metal compounds and the ash is rendered inert. This means that it can also be used when contaminated waste wood is used, for example for road construction, which reduces its disposal costs. Low pressure steam could be used as process steam for the allothermic reaction. This enables the allothermal gasification process to be carried out at a low temperature level without causing disposal and energy use problems with a higher carbon content in the ash. If the allothermal gasification temperature is low, less gas is used for the thermochemical digestion. Proportionally more gas is thus available for the internal combustion engines. In addition, the knock number of the gas is improved. Energetic processes at a lower energy level improve the overall balance of the entire process.

Low pressure steam could be directed into the condensing steam turbine. This specific embodiment uses thermal energy in the form of steam in the low-pressure stage of the condensation steam turbine to generate electricity. In addition, the thermal energy is used as process auxiliary energy.

The waste heat from the engine cooling could be used to dry the material and heat the combustion air of the burners. With this specific configuration, the thermal energy that is released during the electrochemical utilization of the gas could be used in an economically sensible manner.

The waste heat from the engine cooling could be used for combustion in the steam boiler. This supports the combustion of the carbons of the residual ash in an energetically particularly advantageous manner. The supply of waste heat enables a suitable activation of the combustion reaction.

The waste heat from the engine cooling could be used for district heating processes. The energy industry in residential areas and residential areas could advantageously be influenced in such a way that heat is generated from waste products for heating purposes.

The exhaust air from an air condenser of the condensation steam turbine could be used for predrying the material to be gasified. With this configuration, the material to be gasified is prepared so that almost No external energy is used to dry the material to be gasified during the gasification process.

The waste heat from gas cooling from 300 ° C to 40 ° C during cleaning and condensation steps could be used to predry the material to be gasified. It is conceivable here that the gas is suddenly cooled in several stages using the energy given off in corresponding temperature stages, with a majority of dioxins and furans cracking and a backward Boudouard reaction being avoided.

By avoiding a Boudouard reaction, the reverse reaction of two parts of carbon monoxide into one part of carbon dioxide and one part of carbon is avoided. Here, a tube bundle heat exchanger, which is arranged downstream of a cyclone, could cool the gas down to 310 ° C without gas components being able to condense. Here, steam of a higher pressure level is generated very effectively using a heat exchanger of inexpensive design.

In the second stage, the gas could suddenly be cooled with water so that sprayed water drops simultaneously form condensation nuclei for the accumulation of pollutants.

In a third stage, the gas could be cooled to such an extent that excess water condenses out and is conducted in a clean cycle via heat exchangers. The condensed water can be fed back to a preliminary stage. It is conceivable that the waste heat from the gas scrubber is used to preheat the condensate.

With a combination of the three stages of gas treatment mentioned above, contaminated woods can also be used. The process is also suitable for the gasification of waste products, for example shredder light fractions, for the generation of electricity or hydrogen. Of course, it is also conceivable here that the process for the gasification of waste products also generates high-energy gas for energetic use in combustion processes, for example in the brick and cement industries. Due to the intensive pre-cleaning of the gas, the exhaust gases from the motors or burners can be directed into highly efficient heat exchangers. Since the gas is free of pollutants, no waste products accumulate on the heat exchanger surfaces, which reduce their efficiency. Therefore, more efficient heat exchangers can be used and no exhaust gas cleaning is required.

The ongoing operating costs for this gas scrubbing process are lower than those of exhaust gas cleaning systems. It is crucial here that the energy yield of the pure process gas can be used up to the condensation area of the water, whereas in the previous processes the condensing out of the carbon and sulfur compounds requires higher process gas temperatures.

Residual ash separated in the cyclone could be gasified autothermally and the resulting gas could be mixed with the gas produced in the allothermal gasification process. The steam boiler, the combustion of the residual ash or the autothermal gasification could be designed in such a way that a lower gasification temperature can be selected in the reformer of the allothermic gasification. This requires low thermal digestion energy, which means that more gas is available for the engines and the gas composition is improved in terms of methane number and overall efficiency. In this embodiment, the knock number is improved by improving the methane number of the gas composition. In this respect, an engine-friendly design of the method is implemented.

The material to be gasified could be introduced into the interior of the circulating fluidized bed. This advantageously realizes that the material to be gasified is gasified particularly uniformly and a gradient formation in the fluidized bed or in the material to be gasified is avoided.

The exhaust gases generated in the steam boiler could possibly be passed through high-temperature-resistant heat exchanger tubes in the reformer with the addition of material to be gasified, and replace the burners in the reformer in whole or in part. This configuration realizes allothermal gasification in a particularly advantageous manner in that the material to be gasified indirectly via hot pipes is gasified. Exhaust gases produced as waste products are used in an advantageous manner.

The condensed hydrocarbons formed during gas cleaning could be fed to the steam boiler. This configuration realizes that not only hydrocarbons from the residual ash are recycled, but also hydrocarbons that are not separated with the residual ash. In this respect, a particularly effective utilization of all hydrocarbons is realized through this process step.

The condensed hydrocarbons formed during gas cleaning could be fed to the allothermic or autothermal gasification process. This ensures that the allothermic or autothermal gasification process is accelerated.

The gas produced in the allothermal gasification process could be dried, whereby carbons are condensed out via a cryogenic process. As a result, aftertreatment of the gas for higher demands is realized. Due to the high hydrogen content of the gas, traces of hydrocarbons can condense out due to their particularly low partial pressure when the already very clean gas is subsequently compressed. This low-volume gas, which is three times higher than that of autothermal gasification processes and has an energy content three times higher than that of autothermal processes, can be effectively cleaned wet in small systems using special processes. This can be done in such a way that it is also suitable for motor-driven power generators, in particular in connection with a cryogenic process, for highly effective, pressure-charged, high-compression engines with electrical efficiencies above 40%.

The cryo process could be carried out by pre-drying before cooling or by cooling alone so that no gas hydrate formation occurs. Depending on the process gas composition and residual water content, this configuration can optionally be carried out by gas predrying or a combination process. This will result in a dry gas if the gas temperature is raised slightly to approx. 20 ° C. testifies which can be passed into standard air filters for engines. In this respect, commercially readily available devices can be used.

Overall, the energy content of process steps is used to support the thermo-chemical digestion in order to use available energies for the generation of electricity, whereby total electrical efficiencies of up to 40% are possible. It is also conceivable that the energy content is used to raise the temperature of the condensate. Overall, even with lower power plants that use renewable raw materials, overall efficiencies of up to 40% are possible.

As an alternative to burning the carbon of the residual ash, stoichiometric gasification is possible using an autothermal gasification process, or, if necessary, using the Karbo-V process, with simultaneous slagging of the residual ash. The resulting gas is mixed with the main stream before gas cooling and gas scrubbing. The advantage in this case is a higher gas volume for highly efficient gas engines. However, capital expenditure must be weighed up here. In addition, the possibility of an overall energetic optimization is created in such a way that the allothermal gasification takes place more energy-efficiently at lower temperatures, for example at 700 ° C. Gasification of the volatile components takes place at higher throughput rates. It is accepted that there is more carbon in the residual ash, which is then also used for thermo-chemical digestion in connection with the steam cycle or gasified in an autothermal or allothermal process.

Within the scope of the method, it is of course conceivable that the residual moisture in the material to be gasified is suddenly converted into vapor by necessary additional process steam. On the one hand, this supports the circulation process and, on the other hand, saves process steam. In addition, thermochemical digestion and mass transport are supported.

It is also possible that the process steam draws gas from the reformer via a Venturi nozzle, possibly for regulating the fluidized bed, and introduces it into the fluidized bed with only a slight loss of temperature, by the amount of process steam for reducing circulation. This creates opportunities for stable allothermic gasification even with higher material moisture or moisture fluctuations.

Another advantage is that the energy recovery of washed-out carbon compounds such as oils, petrol and tars reduces their disposal costs.

There are now various possibilities for advantageously designing and developing the teaching of the present invention. For this purpose, reference is made to the subordinate claims, on the one hand, and to the following explanation of a preferred exemplary embodiment of the method according to the invention with reference to the drawing. In connection with the explanation of the preferred embodiment with reference to the drawing, preferred configurations and developments of the teaching are also explained in general. In the drawing shows the only one

Fig. In a schematic diagram, the method for generating electricity from carbonaceous material.

The method according to the invention shown in FIG. 1 uses a reactor 1 in which the gasification of the biomass 2 takes place. This can process a wide range of different biogenic substances. The biomass 2 is stored in a warehouse 3, which is sufficient for a quantity of approximately 7000 m ³ . This amount has an average residence time of approx. 10 days.

The biomass 2 has different piece or grain sizes. The delivered biomass 2 is processed in a warehouse 3 by processing and conveying systems. Foreign materials such as metals, stones and the like are separated from biomass 2 by means of separators and sieves. The processing takes place in such a way that 1 piece goods of size type G 50 are fed to the reactor. The moisture of the biomass 2 can be subject to strong fluctuations depending on the season. Biomass 2 with a residual moisture of less than 20% is used for the energetically optimized operation of the reactor 1. The biomass 2 is aerated and dried in the warehouse 3. The ventilation and drying of the biomass 2 takes place by means of low-temperature heat, which arises in the overall process. Suction fans suck air at a temperature of approx. 45 ° C. from an air condenser 4 and blow slightly overheated air into special ventilation channels of the bearing 3. In this way, dry values of about 15 to 20% residual moisture of the biomass 2 used are achieved.

The conveyor systems of the warehouse 3 are designed redundantly two-lane, the biomass 2 is conveyed via automatic crane systems. The cranes are equipped with moisture sensors so that an optimal distribution in the area of the individual storage chambers takes place when the biomass 2 is delivered. The conveyor systems within the warehouse 3 work fully automatically, so that no permanent staff is required for this. The exhaust air from the warehouse 3 is passed through a filter system.

The pre-dried biomass 2 is fed to the reactor 1 via screw conveyors. The feed takes place on two opposite sides, so that an optimal loading of the fluidized bed 5 of the reactor 1 is ensured.

The fluidized bed 5 of the reactor 1 is heated by means of burners which are arranged one above the other in the reactor space. The burners are supplied with combustion air via a fan, which is preheated to about 45 ° C. and is drawn off from the air condenser 4.

The burners burn a mixture of air and fuel gas in a ratio of 1.1 to 1.2, with an excess of air. The thermal energy required for the gasification process is provided via fuel gas branched off after a gas scrubbing.

Inner cyclones integrated in the reactor 1 retain entrained bed material, larger ashes and coke particles and feed them back to the fluidized bed 5. The gas leaves the reactor 1 at a temperature of approximately 800 ° C. and is first passed through an external cyclone. There, fine ash and coke particles are separated, which are then used for post-combustion for further energetic use. The hot gas is further cooled in a tubular heat exchanger to approx. 300 ° C and generates steam which is under a pressure of approx. 45 bar.

To fluidize the fluidized bed 5, superheated process steam is blown into the reformer. The hot exhaust gases emerging from the burners are fed to the waste heat boiler 7 after cooling in the steam superheater 6 for further energetic use.

The ash components contained in the biomass 2 are discharged via the external cyclone at the outlet from the reactor 1. This ash fraction contains residual carbon that was not reacted in reactor 1. With the process in question, a very high carbon conversion can be generated, which is higher than 99%. However, the reactivity of carbon and biomass 2 and the temperature of the gasification process play an important role here.

Basically, the higher the operating temperature, the higher the carbon conversion. Here, however, it is important to optimize the system, taking into account the total energy balance, so that the effort for heating the reformer is not too high in relation to the required carbon conversion. Since, with increasing heating power of the reformer, the gas remaining for processing in the combustion engines designed as gas engines 8 decreases, a technically and economically sensible value must be set here. In the present case, a carbon conversion of approx. 95% is considered to be sensible. Sufficient gas is thus available for the gas engines 8 and the residual carbon of the ash fraction is approximately 20 to 50% depending on the ash content of the biomass used.

This stream of solids is fed to a combustion boiler and burned with the addition of a gas stream for auxiliary firing. The heat generated is used to generate low-pressure steam that is placed on the low-pressure rail of a steam System is given. There, this leads to a reduction in the required extraction steam on a steam turbine, so that the electrical output of the turboset increases by this amount. This means that the energy content of the residual carbon can be fully used.

The combustion of the carbonaceous ash flow in the combustion boiler is carried out using a slag burner. The ash is liquefied and slagged in the combustion process. Compared to the disposal of untreated ash, the detoxified ash is easier to deposit due to the lower elution ability, since the water-soluble components contained therein can no longer be washed out. The costs for the disposal of slagged ashes are considerably lower than for untreated ashes, which results in an additional economic advantage.

The cooled gas enters the gas scrubber and is saturated in direct contact with injected water, thereby cooling to around 45 ° C. All high-boiling hydrocarbons are condensed out and the remaining fine ash particles are separated. By regulating a pH value of the circulating water to approximately 5 to 6 by metering in sulfuric acid, a complete absorption of the ammonia contained in the gas can be achieved.

In a further washing section, the absorption of acidic, essentially hydrogen sulfide components contained in the gas takes place.

The condensed tars and residual ash components are concentrated in the circulating water of the gas scrubber. A waste water stream is removed from the gas scrubbing as a result of the excess water which occurs during gas cooling.

Solid components, tars and liquid hydrocarbons are separated from this stream. The remaining waste water is discharged into the sewage system to the waste water system. The cleaned gas is free from tars, acidic constituents etc. and essentially consists only of hydrogen, methane, carbon monoxide and carbon dioxide and can therefore be used directly in the gas engines 8 connected downstream. Part of the gas is used to fire the burners. The remaining portion is used to generate electricity in the gas engines 8.

The gas available after the gas scrubbing is fed into gas engines 8. There are two basic options available for this. On the one hand, self-priming gas Otto engines can be used. On the other hand, the application of a self-priming pilot gas engine with turbocharging is offered. The variant with pilot gas engine is disregarded here, since the investment costs are significantly higher than with conventional gas engines. However, due to the specificity of this unit, for example lower speed, larger cylinders, the operating costs are lower than with Otto engines.

The total electrical output here is around 4.5 MW, the available thermal output at 90 ° C flow temperature is around 2.0 MW.

With regard to the required gas quality, special requirements with regard to the content of tars, silicon and halogens must be met. These requirements are met by the gas scrubbing used and by the characteristic properties of the allothermal gasification process.

The exhaust gases from the individual gas engines 8 are brought together and, after mixing with the exhaust gases from the pulse burners, are passed into the waste heat block. The exhaust gases of the gas engines 8 have a temperature between 500 and 600 ° C, so that after mixing with the exhaust gases of the burners, mixing temperatures of 620 to 670 ° C are reached. This exhaust gas mixture is fed to the waste heat boiler 7 for generating high-pressure steam.

With regard to the emissions to be observed, the required NOx and CO values can be achieved by using catalysts. The mixed exhaust gases from the gas engines 8 and the burners are brought into the waste heat boiler 7. In the waste heat boiler 7, the boiler feed water is heated, the generation of high pressure steam at 45 bar and the superheating of the high pressure steam to approximately 440 ° C.

The high pressure steam generated is fed to a condensation steam turbine 9. The design of the turbine 9 plays a special role here, since the generation of the electrical energy is determined by the turbine efficiency. Since electricity is the main supply product of the plant and has the greatest impact on the overall economy of the plant, a multi-stage machine with high internal efficiency will be used here.

The condensation steam turbine 9 is provided with a tap, from which the need for the low-pressure rail is covered. The steam reformer is supplied with process steam from the low pressure rail.

The low-pressure steam that occurs in the ash afterburning is fed to the low-pressure rail, so that the tapping amount of the turbine 9 is thereby reduced.

Finally, it should be expressly pointed out that the exemplary embodiment described above only serves to discuss the claimed teaching, but does not restrict it to the exemplary embodiment.

Claims

claims 1. A method for generating electricity from carbon-containing material, in particular from biomass (2), the material being gasified allothermally in a reactor (1) to produce a fluidized bed (5), the gas generated being cooled in successive steps after passing through a cyclone, wherein pollutants are removed from the gas by condensation in the individual steps and pollutants are additionally removed chemically from the gas in at least one step, characterized in that part of the gas is burned in burners for heating the fluidized bed (5) and the rest of the gas is burned in internal combustion engines (8) and is preferably used electrochemically. 2. The method according to claim 1, characterized in that the exhaust gases of the internal combustion engines (8) and / or the burner are used for thermo-chemical digestion of the material to be gasified. 3. The method according to claim 1 or 2, characterized in that the exhaust gases of the internal combustion engines (8) and / or the burner are used for heating and / or drying the material to be gasified. 4. The method according to any one of claims 1 to 3, characterized in that the exhaust gases of the internal combustion engines (8) and / or the burner are used for heating the combustion air of the gas or a post-combustion boiler. 5. The method according to any one of claims 1 to 4, characterized in that the exhaust gases of the burners are passed into a waste heat boiler (7) for steam generation. 6. The method according to any one of claims 1 to 5, characterized in that the exhaust gases of the internal combustion engines (8) are passed into the waste heat boiler (7) for steam generation. 7. The method according to claim 6, characterized in that the exhaust gases of the burner via a steam superheater (6) are passed into the waste heat boiler (7). 8. The method according to any one of claims 5 to 7, characterized in that a condensation steam turbine (9) is driven by the waste heat boiler (7). 9. The method according to any one of claims 1 to 8, characterized in that part of the steam for the thermal imposition of the material to be gasified is already introduced into the screw conveyor of the material to be gasified. 10. The method according to any one of claims 1 to 9, characterized in that carbons of the residual ash separated in the cyclone are introduced directly from the cyclone into a steam boiler and are burned there. 11. The method according to claim 10, characterized in that heavy metal compounds are melted in the steam boiler. 12. The method according to any one of claims 1 to 11, characterized in that steam of low pressure level is used as process steam for the allothermic reaction. 13. The method according to any one of claims 8 to 12, characterized in that steam of a lower pressure stage is passed into the condensation steam turbine (9). 14. The method according to any one of claims 1 to 13, characterized in that the waste heat from the engine cooling is used for drying the material and heating the combustion air of the burner. 15. The method according to any one of claims 1 to 14, characterized in that the waste heat from the engine cooling is used for combustion in the steam boiler. 16. The method according to any one of claims 1 to 15, characterized in that the waste heat from the engine cooling is used for district heating processes. 17. The method according to any one of claims 8 to 16, characterized in that exhaust air from an air condenser (4) of the condensation steam turbine (9) is used for predrying the material to be gasified. 18. The method according to any one of claims 1 to 17, characterized in that the waste heat from a gas cooling from 300 ° C to 40 ° C is used in cleaning and condensation steps for the predrying of the material to be gasified. 19. The method according to any one of claims 1 to 18, characterized in that residual ash separated in the cyclone is gasified autothermally and the resulting gas is mixed with the gas formed in the allothermic gasification process. 20. The method according to any one of claims 1 to 19, characterized in that the material to be gasified is introduced into the interior of the circulating fluidized bed (5). 21. The method according to any one of claims 10 to 20, characterized in that the exhaust gases arising in the steam boiler (7) are passed, if necessary with the addition of material to be gasified, through high-temperature-resistant heat exchanger tubes in the reformer, which replace the burners in the reformer completely or partially. 22. The method according to any one of claims 10 to 21, characterized in that the condensed hydrocarbons formed during gas cleaning are fed to the steam boiler. 23. The method according to any one of claims 19 to 22, characterized in that the condensed hydrocarbons formed during gas cleaning are fed to the allothermic or autothermal gasification process. 24. The method according to any one of claims 1 to 23, characterized in that the gas formed in the allothermal gasification process is dried and carbons are condensed out via a cryogenic process. 25. The method according to claim 24, characterized in that the cryo process is carried out by predrying before cooling or by cooling so that no gas hydrate formation takes place.