DE4317806C1 - Allothermic gas generator and process for generating fuel gas using the allothermic gas generator - Google Patents

Abstract

The invention relates to a process and an apparatus for generating a fuel gas (18) from gasifiable and combustible material (4) such as refuse or from coal (5) or from any mixture of these substances, the material (4) being obtainable from a low-temperature carbonisation stage (A1) to give a solid low-temperature carbonisation product (2, 3, 4), thereupon being freed of metals (A3) and inert matter (A4) and the remaining low-temperature carbonisation residue (4) being ground to a dust (6) and the dust (6), preferably together with any desired amount of admixed directly grindable energy source (5) such as coal or biomass, in an externally heated gas generator (A5) with the exclusion of air or oxygen using steam as gasifying medium generating a gas (9) and a gasifying residue (10) and a combustible crude gas (13) being generated from the gasifying residue (10) and the gas (9) in a high-temperature melt gasifying chamber (A7) with feed of oxygen (11). To generate the steam (8), the process utilises the sensible and latent heat of the crude gas and of heating gases. <IMAGE>

Description

The invention relates to a method for generating a Fuel gas made of gasifiable and combustible material or from this material together with coal, the material is free of metals and inertia and without coal or with any amount of coal added to one fine-grained regrind, hereinafter referred to as dust, ver will grind and be from the dust in an outside heated gas generators in the absence of air or oxygen (allothermic) with water vapor as gasifying agent a gas and a gasification residue is generated.

Such device and method are from the WO 90/02 162 became known.

In the known method, combustible material, especially heterogeneous material such as garbage, one for the public public supply of suitable fuel gas obtained  that from the garbage in an externally heated carbonization gas generators in the absence of air or oxygen without gasification a carbonization gas and a carbonization residue be fathered. Such gasification is "allothermal" records because the process heat via a heat exchanger in the Gasification reactor is introduced. The energy is from egg ner source supplied outside the reactor, so that in the Reak no exothermic reaction with a gasifying agent (e.g. oxygen) must be brought about and none stoichiometric combustion takes place. The result The residual carbon is made from metals and inert substances freed and in a mill to a fine-grained regrind, hereinafter referred to as dust, ground. For this Dust preferably together with any amount mixed coal, optionally ground, and the smolder gas is stored in an externally heated raw gas generator Completion of air or oxygen (allothermic) with water steam as a gasifying agent and a gasification residue Raw gas generated. This raw gas becomes a by purification Clean gas obtained, which can be fed into a public Supply network is suitable. From the gasification residue becomes a flue gas in a gasification residue combustion chamber won, which is used as a heat transfer gas in the process becomes.

In contrast to allothermal gasification, auto thermal gasification is the one required for the gasification process Temperature increase due to heat from the exothermic reak tion of the feed with oxygen. It finds a part wise (substoichiometric) combustion of the feed material instead of.

In the known method, the solids content in  A maximum of three thermal process steps (allothermic Carbonization, allothermic gasification, combustion) treated, the gaseous fraction in a maximum of two process steps (allothermal carbonization, allothermal gasification).

Due to the material limits of the heat exchanger can only reach temperatures up to a maximum in allothermic reactors 850 ° C can be reached. This ends in the known method forth the treatment of the gaseous fraction at 850 ° C. At this temperature there is a risk that possibly still existing dangerous, especially chlorinated, coal water ser substances, e.g. B. dioxins are not yet fully split.

In the known method, only about 95% of the in The energy contained in the feed is won by gasification be. The remaining 5% of the energy is in the closing combustion process won.

In the process, heat exchange processes take place between the Heating gases (heat transfer gases) of the smoldering and gasification level instead. With this arrangement, elaborate too Additional precautions are taken when the concealment level is out of order and only coal is gasified should.

The invention is therefore based on the object, the known The method and the known device to that effect form that contain no dangerous hydrocarbon de, especially dioxin-containing, gases are generated and also without a carbonization gas generator, the combustion of material is possible.

This object is achieved according to the method  solved that from the gasification residue and the gas in one High temperature melting gasification chamber with the addition of Oxygen (autothermal) a combustible raw gas is generated.

According to the invention, the plant is characterized for implementation tion of the method according to the invention in that it egg allothermic (with exclusion of air or oxygen ar processing and with heat exchanger for the entry of the Er gas generators equipped for heating process heat) and has a high temperature melt gasification chamber.

The method and the system according to the invention show in Comparison to waste or coal combustion or in comparison the following about the two known gasification processes Advantages on:

• - The process according to the invention fulfills in its process outline all conditions related to pollutant emissions to a minimum and thanks to the small gas volume and other process advantages ne highly effective and inexpensive gas cleaning. There by that the gas to be cleaned is under pressure, can systems are dimensioned up to 90% smaller the.
• - The expensive high temperature component can break down part of the otherwise required size can be reduced.
• - Flue gas desulphurization plants including the one used raw materials (lime) are saved. The problem Matics of gypsum disposal of flue gas desulfurization location does not apply.  
• - The raw gas is free of dangerous Koh from the start Hydrogen oils, especially free of dioxins. In the high The temperature level of the process is chlorinated coals reliably split hydrogen.
• - The raw gas is free of sticky stock right from the start divide so that oils, phenols and tars quantitatively in the raw gas are undetectable.
• - The oxygen requirement is minimized and essentially water vapor can be used as a gasifying agent. Only 5% of the energy input is in the autothermal Gasification unit, d. H. with oxygen supply, won nen. Due to the low oxygen requirement, none are expensive ren plants necessary, the energy consumption is consumed reduces and no additional emissions.
• - The energy is offered in gaseous form and can therefore de centralized in the process of cogeneration at times about 40% energy savings the.
• - Location problems do not occur, since the fiction procedures replaced coal and waste power plants and there especially the locations of disused coal power works are available.

According to the invention, the temperature is in the high temperature Melting gasification chamber in the range from 1400 ° C to 1800 ° C, preferably at 1600 ° C.

Advantageously, the raw gas is eliminated of sulfur and other elements and chemical ver  bonds creates a clean gas. The after the high temperature stage required direct cooling by water spray reliably prevents the regression of chlorinated coal hydrogen.

In a particularly preferred embodiment of the invention becomes a in an externally heated carbonization gas un ter completion of air or oxygen generated Schwwe lungsreststoff used as material. In this procedure level, metals and other substances are not oxidized or burned, but the substances can be elementary or in shape safe compounds are eliminated. Useful metal le lie after the blurring level - thanks to the reduced Atmosphere of the smoldering process - in metallic bright Form in the discharge. The process allows valuable metals salvage before melting and that in the next process stage fluidized bed gasification of stressful Keep inertia free. The smoldering is taking place partly in a rotating drum with tubular heat metauschern, the temperature in the carbonization gas generator is in the range of 300 ° C to 600 ° C. An energy expenditure The pressing of the material is not necessary. The after Segregation of energetically unusable metals and Inertia remaining carbonaceous charring residue can, possibly together with directly grindable energy like coal or biomass, to dust in a mill be ground.

As a further step towards a chimney-free system or A chimney-free process is used in the carbonization gas ger generated carbonization gas to the gas generator in addition to Ver Schwelungsreststoff supplied.  

The embodiments listed below each perform because in itself a contribution to chimney-free production of a fuel gas and, in their combination, allow these chimney-free production:

• - The sensible warmth of one by burning a part of the combustion gas formed becomes Be heating the carbonization gas generator and then for preheating the fresh air supplied to the combustion chamber and thereafter the preheating of the process water used.
• - The sensible warmth of one by burning a part of the combustion gas formed becomes Be heating the raw gas generator and then for preheating the fresh air supplied to the combustion chamber and thereafter the preheating of the process water used.
• - The sensible heat of the raw gas is used to preheat the Process water used.

In a particularly preferred embodiment of the invention, who the one for the gas generator and the smoldering gas generator the decoupled heating gases used so that now a separate te heating of the two reactors is made possible and the Gas generators work easily even without the carbonization gas generator can.

Before the clean gas is fed into a public ver Supply network is made from the clean gas through carbon monoxide converters and through carbon dioxide washing to the public Supply suitable conversion gas generated.

That with the steam generation from the heating gases and the  Raw gas by cooling to 25 ° C condensate is returned to the fresh water cycle.

Further advantages result from the description and the attached drawing. Likewise, the above can ten and the features listed further fiction individually or in any combination with each other who are used. The mentioned embodiments are not to be understood as a final list, but ha rather exemplary character.

The method and the device according to the invention are in the drawing and are based on an Ausfü Example explained approximately.

Fig. 1 shows schematically the functional blocks of a plant according to the invention for the recovery of energy-containing material and the coupling of these functional blocks.

The path of the various substances in the system according to FIG. 1 is shown by arrows. These arrows are to be understood as pipelines in the case of the transport of a gas, in the case of the transport of solids it can instead also be conveyor belts or other Transportvor devices. In the description, only the arrows that are transported are also used to identify the substances transported. The substances transported by the transport routes are identified in FIG. 1 with reference numerals, the functional blocks each with a letter “A” preceded by a reference number.

Garbage ( 1 ) is fed to a smoldering device A1. The garbage is crushed by shredding rollers (not shown) before being fed to the swelling device A1, and the iron parts are removed by magnetic separators. The Verschwelungsvorrich device A1 has a gas-tight container, the interior of which can be heated via a heat exchanger A2. The interior of the carbonization device A1 is heated to approximately 450 ° C. Metals A3, for example iron, copper, aluminum, tinplate, heavy metals such as so-called inert substances A4, for example stone or glass ( 2 , 3 ) can be sorted out from the residual carbon. This is shown schematically in FIG. 1. The rest of the solid carbonization residue ( 4 ) arrives at a mill system A0, in which it is ground to a fine dust and from where it is fed to a gasification device A5 together with a directly milled energy carrier ( 6 ) such as coal or biomass. During the charring process, a combustible carbonization gas ( 7 ) is produced, which is also fed to the interior of the gasification device A5.

This first stage is the same in others allothermal carbonization applied in modern processes at approx. 450 ° C. This stage of the process is in process garbage recommended as it allows valuable Recover metals before melting and those in the next Stage following fluidized bed gasification of polluting Iners to keep clear. The smoldering takes place in one rotating drum, creating an energy-intensive pressing of the garbage is not required. This level of blurring can also be in a separate location from the rest of the system.

The gasification device A5 has a gas-tight container which is heated to a temperature of, for example, 850 ° C. via a heat exchanger A6. In the Vergasungsvor direction A5 is a fluidized bed gasifier, the inner gasification tank water vapor ( 8 ) is supplied. In contrast, oxygen or air are not added. The gasification device A5 supplies as a starting material a gas ( 9 ) and as a non-gasifiable back a gasification residue ( 10 ), which are fed to a high-temperature melting gasification chamber A7.

With this step, it is possible to increase the allothermal portion to 95% of the energy contained in the feed material. In the gasification device A5, the dust generated in the mill system is gasified together with the supplied energy source ( 6 ) and the waste carbonization gas taken over from the first stage is split. To generate the process steam, the process uses the sensible heat of the heating gases and the Rohga ses, as will be explained below.

Oxygen ( 11 ) or air is supplied to the interior of the high-temperature melting gasification chamber A7. This third stage is therefore an auto-thermal high-temperature melting chamber gasification. This gasification stage enables the high temperatures of, for example, 1600 ° C. which are necessary for the safe splitting of dangerous hydrocarbons. In the high-temperature melting gasification chamber, the gasification residue (5% of the input energy) is subjected to the final gasification and the gas taken over from the second stage is further split. Glazed slag ( 12 ) is led out of the high-temperature melting gasification chamber A7 as a solid residue, which can possibly be used for road construction or can be brought to an ordinary landfill.

The direct cooling A9 (depending on the material, without heat exchanger) of the raw gas ( 13 ) required by the high temperature stage by spraying in water ( 14 ) reliably prevents the recombination of hydrocarbons.

The heat that can still be felt and the latent heat of the gas ( 15 ) leaving the cooling A9 is used to heat the water ( 32 ) required for the water vapor ( 8 ). On the transport route, the raw gas ( 16 ) is converted into a clean gas ( 20 ) in a multi-stage cleaning and conversion process A10, A11, A12, in particular also by sulfur separation.

From this clean gas a conversion gas ( 18 ) is generated by carbon monoxide conversion A13 and by carbon dioxide scrubbing A14, which is suitable for feeding into a public supply network ( 19 ).

Part of the clean gas ( 20 ') is fed to a Brennkam mer A16 and burned, and the sensible heat of the combustion gas ( 21 ) is used to heat the heat exchanger A2 in the carbonization device A1. The sensible heat afterwards of the hot air ( 21 ) leaving the heat exchanger A2 is fed in a chamber A17 via a heat exchanger A18 to the fresh air ( 22 ) supplied from the outside. The fresh air ( 23 ) heated in this way is fed back to the combustion chamber A16 together with the clean gas ( 20 ').

Another part of the clean gas ( 20 '') is fed to a combustion chamber A19. The sensible heat of the gas ( 24 ') is used by the heat exchanger A6 in the gasification device A5. The sensible heat of the hot air ( 24 ) leaving the heat exchanger A6 is used to heat a chamber A18. Via a heat exchanger A20 arranged in this chamber A20, fresh air ( 25 ) supplied from the outside is heated and fed together with the pure gas 20 '' to the combustion chamber A19.

Another part of the clean gas ( 20 ''') is fed to the combustion chamber A21 together with the fresh air ( 26 ) heated in the chamber A18. The combustion gas ( 27 ) thus produced passes into a chamber A23, where it gives off its sensible heat in a heat exchanger A22 to water ( 29 ) that has already been heated to produce water vapor. This water vapor ( 8 ) passes into the gasification chamber A5, where it is used as a gasifying agent. The combustion gas ( 28 ) is returned from chamber A23 to chamber A18.

The already heated water ( 29 ) is won by 3 heat exchangers (A24, A24 ', A24'') from fresh water ( 30 , 31 , 32 ). The heat exchanger A24 is arranged in the chamber A25, where the sensible and latent heat of the gas entering the chamber A25 is used to heat the fresh water ( 32 ). The heat exchanger 24 'in the chamber A25' is emitted on the sensible and latent heat of the hot air coming from the chamber A17 to the fresh water ( 30 ) supplied from the outside. In addition, in the heat exchanger A24 '' arranged in the chamber A25 '', the still noticeable and latent heat of the hot air ( 34 ) coming from the chamber A18 is given off to the fresh water ( 31 ) supplied from the outside and the water is heated in this way.

Furthermore, the condensate A26, A26 ', A26''is returned to the fresh water circuit 30 , 31 , 32 in the steam generation from the heating gases and the raw gas by cooling to 25 ° C.

Plastic pipes are sufficient to discharge the heating gas ( 36 ', 36 ''), which has now cooled to 25 ° C. The emission of pollutants is lower than that of normal gas heating systems.

In this way, the system according to the invention can be fireplace-free be carried out. It can also be carried out without emissions when the pure to heat the allothermic reactions gas, especially hydrogen or oxygen who used the. The combustion of hydrogen with oxygen results water as a combustion product. The condensed water can in turn can be used directly for steam generation.

The low temperature that occurs during the production of oxygen Tur waste heat can be used in the process to preheat the process water be used. A heat dissipation and cooling towers and over district heating systems is superfluous.

The higher the in the gasification facilities A5, A7 pressure, the smaller the dimensions of the Facilities, especially the downstream Reini systems. The dimensions can only be 10% of that of garbage incinerators required. The one in the gas generator A5 prevailing pressure can be up to about 20 bar At atmospheric pressure in the gas generator A5 are for the facilities necessary for pressure generation are not required  Lich.

The invention relates to a method and a device for generating a fuel gas ( 18 ) from gasifiable and ver combustible material ( 4 ) such as garbage, wherein the material ( 4 ) from a carbonization stage (A1) to a fe most carbonization product ( 2 , 3 , 4) is obtainable, then of metals (A3) and inerts (A4) is freed and the ver permanent Verschwelungsreststoff (4) (6) ver ground to a dust and dust (6), preferably together admixed with egg ner any amount Directly grindable energy carrier ( 5 ) such as coal or biomass in a gas generator (A5) which is heated from the outside with the exclusion of air or oxygen with steam as a gasifying agent, a gas ( 10 ) and a gasifying residue ( 9 ) are generated and from the gasifying residue ( 9 ) and the gas ( 10 ) in a high-temperature melting gasification chamber (A7) with the supply of oxygen ( 11 ) a combustible raw gas ( 13 ) is generated. For the generation of water vapor ( 8 ), the process uses the tangible and latent heat of the raw gas and heating gases.

Reference list

A0: mill system
A1: Smoldering device
A2: heat exchanger
A3: metals
A4: Inertia
A5: gasification device
A6: heat exchanger
A7. High temperature melting gasification chamber
A8: slag
A9: cooling
A10, A11, A12: Multi-stage cleaning and conversion process
A13: Carbon monoxide conversion
A14: Carbon dioxide wash
A15: feed
A16: combustion chamber
A17: Chamber
A18: heat exchanger
A19: combustion chamber
A20: heat exchanger
A21: combustion chamber
A22: heat exchanger
A23: chamber
A24, A24 ′, A24 ′ ′: heat exchanger
A25, A25 ′, A25 ′ ′: chamber
A26, A26 ′, A26 ′ ′: condensate
1 : garbage
2 : Inertia
3 : Inertia
4 : residual carbon
5 : ground carbonization residue
6 : grindable energy source
7 : flammable carbonization gas
8 : water vapor
9 : gas
10 : gasification residues
11 : oxygen
12 : glazed slag
13 : raw gas
14 : water
15 : gas
16 : raw gas
17 : Clean gas
18 : conversion gas
19 : Supply network
20 : Clean gas
20 ′ : part of the clean gas
20 ′ ′ : part of the clean gas
20 ′ ′ ′ : part of the clean gas
21 : combustion gases
21 ′ : combustion
22 : Fresh air from outside
23 : heated fresh air
24 : hot air
24 ′ : clean gas
25 : Fresh air from outside
26 : Clean gas and fresh air
27 : Combustion gas
28 : Combustion gas
29 : Heated water
30 : Fresh water
31 : Fresh water
32 : Fresh water
33 : hot air
34 : hot air
35 : Fresh air and clean gas
36 ′ : Cooled heating gas
36 ′ ′ : Cooled heating gas

Claims (36)

1. A method for producing a fuel gas from gasifiable and combustible material or from this material together with coal, the material being freed from metals and inert substances and without coal or with any amount of coal added to a fine-grained regrind, hereinafter referred to as dust referred to, milled len and where a gas ( 9 ) and a gasification residue ( 10 ) are generated from the dust in an externally heated gas (A5) with the exclusion of air or oxygen (allothermic) with steam as the gasifying agent, thereby characterized in that a combustible raw gas ( 13 ) is generated from the gasification residue ( 10 ) and the gas ( 9 ) in a high-temperature melt gasification chamber (A7) with the supply of oxygen ( 11 ) (autothermal). 2. The method according to claim 1, characterized in that the temperature in the high-temperature melting gas solution chamber (A7) in the range from 1400 ° C to 2200 ° C lies. 3. The method according to claim 1 or 2, characterized net that the temperature in the gas generator (A5) in the loading ranges from 600 ° C to 1000 ° C. 4. The method according to any one of the preceding claims characterized in that as a gas generator (A5) a What serdampf fluidized bed reactor with tubular heat exchanger is used. 5. The method according to any one of the preceding claims characterized in that the gas generator (A5) at egg  nem pressure of less than 20 bar, preferably less than 10 bar, preferably at about atmospheric pressure is driven. 6. The method according to any one of the preceding claims, since characterized in that the sensible warmth of the Rohga ses used to heat the water vapor (A25) becomes. 7. The method according to any one of the preceding claims, characterized in that a in an externally heated carbonization gas generator (A1) with the exclusion of air or oxygen (allothermal) generated carbonization residual material ( 4 ) is used as the material. 8. The method according to claim 7, characterized in that the temperature in the carbonization gas generator (A1) in the range from 300 ° C to 600 ° C. 9. The method according to any one of claims 7 or 8, characterized characterized in that as a carbonization gas generator (A1) Rotary drum with tubular heat exchanger is used. 10. The method according to any one of claims 7 to 9, characterized in that in the carbonization gas generator (A1) he produced carbonization gas ( 7 ) is supplied to the gas generator (A5) in addition to the carbonization material ( 4 ). 11. The method according to any one of the preceding claims, since characterized in that from the raw gas by Aus separation of sulfur and other elements and chemical compounds (A10, A11, A12) a clean gas is fathered.   12. The method according to claim 11, characterized in that the sensible warmth of one by combustion (A19) one Part of the clean gas formed combustion gas for Heating (A6) of the gas generator (A5) is used. 13. The method according to claim 12, characterized in that the sensible heat of the combustion gas after heating (A6) of the gas generator (A5) for heating the combustion chambers (A19, A21) supplied fresh air ( 25 ) is used. 14. The method according to any one of claims 11 to 13, characterized in that the sensible heat of a combustion gas formed by Ver combustion (A21) of part of the clean gas for heating (A23) the water vapor ( 8 ) is used. 15. The method according to claim 14, characterized in that the sensible heat of the combustion gas after heating the steam ( 8 ) for heating at least one of the combustion chambers (A19, A21) fresh air supplied is used. 16. The method according to any one of claims 11 to 15, characterized characterized in that the sensible warmth of a ver combustion (A16) of part of the clean gas formed Combustion gas for heating (A2) the carbonization gas generator (A1) is used. 17. The method according to claim 16, characterized in that the sensible heat of the combustion gas after heating (A2) of the carbonization gas generator (A1) for heating fresh air ( 22 ) supplied from the combustion chamber (A16) is used. 18. The method according to any one of claims 10 to 17, characterized characterized in that for the gas generator (A5) and Smoldering gas generators (A1) decoupled heating gases be used. 19. The method according to any one of claims 11 to 18, characterized ge indicates that from the clean gas through carbon monoxide conversion (A13) and carbon dioxide washing (A14) a conversion gas is generated. 20. Installation for carrying out the method according to one of the Claims 1 to 19, characterized in that they egg allothermic (with exclusion of air or acid fabric working and with heat exchanger for entry of process heat equipped for heating) Gas generator (A5) and a high-temperature melting gas solution chamber (A7). 21. Plant according to claim 20, characterized in that the one before the allothermal gas generator (A5) teten allothermal carbonization gas generator (A1). 22. Plant according to one of claims 20 or 21, characterized in that it has at least one mill system (A0) for grinding the material, preferably the Ver sulfur residue ( 2 ), and if necessary of directly milled energy sources ( 5 ) such as coal or biomass or any mixture of the Ver Schwelungsreststoff ( 2 ) and this energy source ( 5 ). 23. Plant according to one of claims 20 to 22, characterized in that it has at least one heat exchanger (A25) for transferring the sensible and latent heat of the raw gas to the water vapor ( 8 ). 24. Plant according to one of claims 20 to 23, characterized ge indicates that they have at least one system for cleaning supply (A10, A11, A12) of the raw gas. 25. Plant according to one of claims 20 to 24, characterized ge indicates that they will reappear for everyone in the facility led partial stream of the clean gas a clean gas firing mer (A16, A19, A21). 26. Plant according to one of claims 20 to 25, characterized ge indicates that they have at least one heat exchanger (A6) to transfer the in the clean gas combustion chamber (A19) generated heat on the raw gas generator (A5) points. 27. Plant according to one of claims 20 to 26, characterized in that it has at least one heat exchanger (A22) for transferring the heat generated in the clean gas combustion chamber (A23) to the water vapor ( 8 ). 28. Plant according to one of claims 20 to 27, characterized ge indicates that they have at least one heat exchanger (A2) to transfer the in the clean gas combustion chamber (A16) generated heat on the carbonization gas generator (A1) having. 29. Plant according to one of claims 20 to 28, characterized in that it has at least one heat exchanger (A20) for transferring the sensible heat of the heat exchanger (A6) of the gas generator (A5) leaving hot air ( 24 ) to the combustion chambers ( A19, A21) supplied fresh air ( 25 ). 30. Plant according to one of claims 20 to 29, characterized in that it has at least one heat exchanger (A25 '') for transferring the sensible and latent heat of the heat exchanger (A6) of the gas generator (A5) leaving hot air ( 24 ) for the water vapor ( 8 ) serving water ( 31 ). 31. Plant according to one of claims 20 to 30, characterized in that it has at least one heat exchanger (A18) for transferring the sensible heat of the heat exchanger (A2) leaving hot air ( 21 ) to the fresh air supplied to the combustion chamber (A16) ( 22 ). 32. Installation according to one of claims 20 to 31, characterized in that it has at least one heat exchanger (A25 ') for transferring the sensible and latent heat of the heat exchanger (A2) of the carbonization gas generator (A1) leaving hot air ( 21 ) for the Has water vapor ( 8 ) serving water ( 30 ). 33. Plant according to one of claims 20 to 32, characterized ge indicates that they have separate heat transfer circuits for the gas generator (A5) and the carbonization gas generator (A1) having. 34. Plant according to one of claims 20 or 33, characterized ge indicates that they are used to treat the pure gas  a carbon monoxide conversion plant (A13) and for carbon dioxide washing (A14). 35. Use of the Schwwelreststoffes ( 4 ), preferably also the carbonization gas ( 7 ), as a feed material for a water vapor fluidized bed gasification reactor (A5). 36. Use of the purified fuel gas ( 18 ) suitable for public supply for feeding (A15) into a public supply network ( 19 ).