CH644888A5 - METHOD FOR COMBINED WASTE RECYCLING AND WASTE WATER TREATMENT. - Google Patents

Description

The invention relates to a method for combined waste recycling and wastewater treatment, the wastewater being mixed with at least some of the comminuted waste, being separated into organic and inorganic constituents, sedimented inorganic constituents and floating organic constituents of the refuse being removed, and the wastewater stream having dissolved therein and suspended constituents of the waste are passed through a two-stage filter made of non-activated and activated coal in countercurrent to the wastewater, solid waste or a part of the filter coal saturated with dirt load is burned with heat and fuel gas in a first reactor of a multiple reactor kiln Second reactor, the majority of the coal saturated with dirt load is thermally treated for regeneration, the dirt load adhering to the carbon filter being thermally decomposed to produce coal and carbonization gas, and the regenerated Filter carbon of the second reactor, possibly after its activation, is returned to the waste water filter zone.

The invention further relates to an apparatus for performing this method.

DE-OS 25 58 703 discloses a method for combined waste recycling and wastewater treatment. This process works in a relatively simple and economical manner by

1. the waste water serves as a means of transport for the waste and for its separation of inorganic and organic constituents,

2. the waste water contaminated with the waste is cleaned by mechanical and adsorptive filtration using normal and activated carbon;

3. a part of the waste or the activated carbon loaded with dirt is burned and, in addition to a fuel gas, emits the heat required for the thermolysis;

4. The main part of the filter coal loaded with dirt is thermally decomposed in a thermolysis reactor, whereby the filter coal is regenerated and new coal and carbonization gas are obtained.

Although the above method has a number of advantages, it is desirable to improve it for optimal energy use. In addition, it is necessary to eliminate disadvantages and difficulties that occur when carrying out the method. So when using coal or activated carbon, which was produced according to the method of the above-mentioned DE-OS, the coal may be abraded, which leads to coal losses, blockages of the filter towers and contamination of the used water obtained.

The object of the invention is to improve the energy balance of the process by optimally utilizing all energy sources and to ensure the smooth running of the process, which is achieved in particular by a targeted choice of the reaction conditions within the multiple reactor kiln and a corresponding treatment or processing of the products emerging from the multiple reactor kiln shall be.

The object of the present invention is achieved in that the oxygen is fed into the first reactor of the multiple reactor boiler in a substoichiometric ratio in such a way that the pyrolysis process is maintained, the temperature does not rise substantially above 800 ° C., a hydrocarbon-rich fuel gas being obtained and heat being released which heats up the second reactor (this process step is referred to below as pyrolysis); Filter coal saturated with dirt load is degassed in the second reactor in an oxygen-free atmosphere and the dirt load adhering to the filter coal is thermally decomposed, whereby a carbon-rich carbonization gas and coal are obtained (this process step is referred to as thermolysis in the following) and at least part of the carbon dioxide produced or produced in the second reactor regenerated coal is subjected to a pelletizing process.

When defining the method according to the invention, it is stated that the waste water is mixed with at least a small part of the comminuted waste. This is to be understood to mean that part of the waste can also be burned directly in the pyrolysis reactor, insofar as this is necessary - to supply the energy for thermolysis carried out simultaneously in the reactor.

It is also stated in the introduction that the wastewater flow with the constituents of the waste dissolved and suspended therein is passed through a two-stage filter made of non-activated and activated coal that is countercurrent to the wastewater. This is to mean that the wastewater flows towards the outlet of the device (118, Fig. 2b), while the filter devices (114, 126) flow in countercurrent, i.e. from (128) to (124).

If necessary, at least part of the fuel or carbonization gas formed, which contains long-chain hydrocarbons, optionally using the heat content of the gas by means of a heat exchanger, can be broken down into short-chain hydrocarbons in a thermal cracking device.

The multiple reactor reactor provided in the process according to the invention can have several reactors of the first and s

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second type, which preferably represent continuously guided rotary kilns. The first reactor is preferably located in the lower part of the multiple reactor kiln, while the second reactor is preferably arranged in the upper part of the kiln above and in the immediate vicinity of the first reactor, so that it can be heated by the latter by convection heating.

The first reactor is used for pyrolysis of waste, while in the second reactor the coal saturated with dirt is thermolyzed. In addition, the first reactor of the multiple reactor kiln can be charged with saturated normal or activated carbon at periodic intervals,

which is followed by combustion of the coal contaminated with heavy metals and the heavy metals are removed from the reactor together with the ash. In addition, it is possible to load the thermolysis reactor (second reactor) with solid, preferably organic waste or to add waste to the furnace material.

The process according to the invention is characterized by a particularly advantageous combination of different process steps which allow maximum energy utilization of the processes taking place in the multiple reactor kiln, the heat generation during the pyrolysis or combustion being controlled by metered oxygen supply, and the remaining energy in the form of a proportional one hydrocarbon-rich fuel gas is obtained. With the aid of the method according to the invention, it may be possible, depending on the composition of the waste, to operate the combined plant for waste recycling and wastewater purification without the supply of external energy and also to obtain additional energy.

Due to the particularly favorable conditions chosen within the multiple reactor kiln, a filter carbon with good adsorption properties and a carbonization gas that is particularly strongly enriched in hydrocarbons are obtained in the thermolysis step. The special treatment of the fuel or smoldering gases emerging from the multiple reactor kiln produces energy that can be stored, the heat content of the gases being used by means of a heat exchanger in the system to carry out the process according to the invention for predrying, heating the backwashing water or for the thermolysis step. In addition, difficulties in carrying out the method are avoided by a targeted treatment of the filter coal emerging from the multiple reactor kiln. According to the invention, the regenerated filter carbon used in the coarse filter is either pelletized, i.e. to bring it into a compact form of the desired particle size, thereby avoiding signs of abrasion of the coal and the resulting pollution of the water obtained, as well as clogging of filter elements filled with filter carbon, or by pretreating the coal to be activated, used in the fine filter, a filter material with a particularly large surface area , ie with high adsorption capacity. These process steps are explained in more detail below.

According to the invention, the pyrolysis takes place at a temperature which does not substantially exceed 800 ° C. A particularly preferred temperature range is between 500 and 800 ° C. Occasionally, it is also preferred to work at temperatures in the range of 300 to 400 ° C to avoid the evaporation of certain heavy metals.

The oxygen supply to the first reactor takes place in a substoichiometric ratio. The oxygen is metered in such a way that the pyrolysis is maintained, but the temperature is controlled in such a way that it does not essentially exceed 800.degree. The amount of oxygen supplied is advantageously 30 to 90% of the stoichiometrically required amount of oxygen, preferably 50 to 80%. The amount of oxygen depends on the composition of the furnace material to be burned and on its degree of moisture.

The fuel gas generated in the first reactor during pyrolysis is relatively rich in hydrocarbons due to the controlled heat generation; The carbonization gas generated in the second reactor during the thermolysis of the dirt-laden filter coal or solid waste is particularly rich in long-chain hydrocarbons.

The fuel or carbonization gas formed can be used as an additional external energy source for the thermolysis process or as fuel for a separate boiler, gas combustion device, preferably an internal combustion engine, or the like.

It is also possible to treat the fuel or smoldering gas in a cracking device in order to split long-chain hydrocarbons into short-chain molecules, which in turn can be used directly in internal combustion engines, turbines and the like, or which, after liquefaction, represent an easily storable energy source .

According to the invention, it is advantageous to cool the gases emerging from the high-temperature zone to a sufficient extent in order to liquefy them, with a separation into liquid nitrogen and a liquid, combustible, nitrogen-free gas, for example a methane gas, optionally taking place.

In a preferred embodiment of a cracking device which operates with a high degree of efficiency, the long-chain hydrocarbons are split into short-chain hydrocarbons in a low-oxygen, high-temperature zone at a temperature of at least 1300 ° C. The long-chain hydrocarbons can also be cracked in the apparatus mentioned with the exclusion of oxygen, so that there is no combustion or oxidation of the gas obtained.

Said high-temperature zone is usually created within the cracking device by filling flammable substances, such as wood or coal, for example filter coal, into a vertical container, burning them at the lower end of the container by blowing in a metered amount of oxygen, and burning gas into Is directed downward through the device, the amount of oxygen being metered in such a way that a controlled combustion of the substances and the generation of the desired temperature is ensured.

In a preferred embodiment, the combustible substances are introduced into the device, the upper part of the device filled with these substances serving to adsorb the solid and liquid particles carried by the fuel or smoldering gases, while the lower part of the device represents a high-temperature zone.

It is advantageous to pass the resulting exhaust gases through a heat exchanger, the thermal energy being transferred from the exhaust gases to the heat exchange medium. The heat obtained from the exhaust gas can either be used for pre-drying solid waste and / or filter coal saturated with dirt load, or it can be used to support the pyrolysis or thermolysis steps taking place in the multiple reactor kiln. In addition, the heat obtained from the exhaust gas can be used via a second heat exchanger to heat the water used for backwashing the saturated activated carbon in order to facilitate the desorption of the filtered-out substances which adhere to the activated carbon. It is also advantageous to partially remove the exhaust gas

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duct-like contaminants through a carbon filter.

According to the invention, it is particularly provided that the filter coal produced in the second reactor be specially treated in order to avoid difficulties which may arise during the course of the process due to coal abrasion. For this purpose, the regenerated coal, which is relatively soft and has a very different particle size, can be pelletized by one of the conventional methods, if appropriate using a binder. It is particularly necessary, e.g. by means of a sieve to separate the fine coal particles and the coal dust, which are then fed to the pelletizing device, and as pellets to the sieve residue, i.e. can be added to the coarser coal particles. This mixture then serves to fill the coarse filter elements (1st filter section):

To produce activated carbon, the regenerated carbon can be pretreated to give it sufficient hardness and a reasonably uniform particle size.

For this purpose, the coal obtained in the second reactor is preferably finely ground and e.g. mixed with tar or pitch in a weight ratio of 10: 1 to 5: 1. This coal / tar or -Pech mixture can then be compacted using high pressures, preferably 1000 to 2000 kp / cm2, and at temperatures just above the softening point of the respective tar or pitch. The coal / tar or pitch mixture obtained is then usually ground down to the desired particle size. This can preferably be done with the help of a roller mill in order to keep the fine fraction as low as possible. Of course, other grinding plants, such as Cross beater mills can be used.

The particle size to which the filter carbon is ground depends on the intended use: Activated carbon, which is used for liquid cleaning, should preferably have a particle size between 0.5 and 1.5 mm. The activated carbon used for gas cleaning preferably has a particle size of 2 to 3 mm.

If the coal to be activated later is used exclusively for gas purification, the following preferred method can be used: The coal obtained from the second reactor is finely ground, mixed with tar or pitch in a weight ratio of 10: 1 to 5: 1 and then at high pressures, preferably 1000 kp / cm2, and at temperatures that are just above the softening point of the tar or pitch used, extruded directly into moldings of the desired size with the help of extrusion presses.

The chip granules obtained in this way, or the moldings of the desired size, can then be activated in an activation device using hot steam or chemicals using a method customary in industry. An activated carbon with a particularly high adsorption capacity is obtained. This activated coal is preferably pelletized in a pelletizer.

The figures represent advantageous embodiments according to the invention, which do not result in any restriction, and are to be explained in the following:

Fig. 1: Schematic flow diagram of the inventive method for combined waste recycling and wastewater treatment:

2a and 2b: combined method for waste recycling and wastewater treatment according to the invention:

3: schematic flow diagram of the production route, the use and regeneration of normal and activated filter carbon according to the invention;

4: Front view, in cross section, of the multiple reactor boiler according to the invention;

FIG. 5: side view, in cross section, of the multiple reactor kiln shown in FIG. 4 along the line 5-5;

Fig. 6: Cracking device according to the invention.

1 shows a schematic flow diagram of the material flow in the treatment of solid and liquid waste in the waste recycling and wastewater treatment plant 102 according to the invention. The plant comprises a multiple reactor digester 104. The solid waste to be processed, which i.a. Food waste, paper, plastics, oil and tar residues, old tires, wood, glass, ash and the like can be pretreated by magnetic tape separation, defibration and flotation in the wastewater,

that it consists essentially of organic components for further treatment. In the multiple reactor kiln 104, the solid waste is pyrolyzed in a first reactor in a low-oxygen atmosphere to produce heat, fuel gas and ash.

The wastewater can include both urban wastewater and industrial wastewater. A multi-stage carbon filter 106 is used to purify the waste water so that it can be used at least for industrial purposes. The carbon filter 106 is a two-stage filter which consists of a coarse and a fine filter. The filter coal of the coarse filter is periodically regenerated together with the particles and sludge adhering to the coal in the kiln 104, i.e. subjected to heat treatment in the absence of oxygen. The newly won and regenerated coal compensates for coal losses.

2a and 2b, supplemented by FIG. 3, show an overview of the procedure of the waste recycling and wastewater treatment plant 102. A wastewater inlet duct 108 leads wastewater via a settling basin 110 and a sieve 112 to the coarse filter 114. The final one then takes place in the fine filter 116 Purification of the water that leaves the system via outlet channel 118.

The coarse filter 114 consists of a large number of coarse filter elements 120, which can be lifted and lowered to leave the coarse filter for regeneration or can be returned to it. Each filter element 120 is filled with normal filter carbon of a suitable particle size, preferably with pelletized filter carbon. The coarse filter elements are moved from the end of the filter 122 to the beginning of the filter 124 when operating in countercurrent to the waste water flow.

The fine filter 116 also consists of a series of fine filter elements 126, which are also moved in stages in countercurrent to the waste water from the lower end 128 to the upper end 130. The fine filter can be cleaned by backwashing, if appropriate in backwashing devices 134 provided for this purpose. The backwashing water is preferably taken directly from the outlet channel 118 and can be stored for a while in the reservoir 136, which is equipped with heating spirals 138. The water contaminated by the backwash flows through the return line 140 back to the waste water inlet 108. For waste treatment, the solid waste is unloaded into a bunker 160, where a first treatment or separation of the waste takes place by means of a magnetic tape 162, the conveyor belt 166, the shredding rollers 164 . The substances are separated in the settling tank 110 with a density> 1 and removed with the aid of the cup conveyor 168. A series of air nozzles 170 ensure thorough mixing of waste water and waste, which makes it easier to separate them into organic and inorganic components. A sponsor 132

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transports floating organic matter to the two storage chambers 172 of the multiple reactor kiln 104. In addition, further waste can be continuously transported to the storage chambers via the conveyor belts 174.

The multiple reactor kiln 104, in which the pyrolysis and thermolysis of garbage and / or filter coal loaded with dirt load takes place simultaneously in different reactors, is shown in FIGS. 4 and 5. The reactors 178 are used for burning or pyrolysis of waste and / or filter coal loaded with dirt. Saturated filter coal or waste is thermolysed in reactor 186.

The housing 222 delimits the interior of the kiln 190. The shafts 224 are mounted on bearings 226 and are driven by the drive device 228 with the motor 230. Via the openings 232 for filling and emptying with a door 234 and a door 236 with a further device for closing the doors, the furnace material is filled into or emptied from the reactors. Doors 234 and 236 have hinges 262. In addition, the reactors 178 are equipped with the air inlet 238, the outlet for fuel gas 240, the convex sieves 242. The reactor 178 is also connected to the gas line 184, which has the check valve 246, and the cracking device 192, the washer 196, the internal combustion engine 202, the generator 204, and the branch line 248 with the valve 250.

The waste container 252 has the closure plate 254, which separates the collecting space 256. The articulated plate 258 with the heat insulation 260 is located at the lower end of the collecting space 256.

The collecting space 264 which is to be opened downwards is delimited by the plate 266 which is provided with a joint. After thermolysis or pyrolysis, the solid materials are released from the reactors into the funnel-shaped containers 268 and 270. The latter are equipped with heat exchanger spirals 272 and the slide 274. The conveyor belt 276 is located under the containers 268, 270.

In addition, air can be supplied into the interior of the kiln 190 via the air inlet line 278 with the valve 280. The gas line 282 with the valve 284 is located above the thermolysis reactor 186. The thermolysis reactor 186 is also equipped with a heat transfer line 288.

The coal formed in reactor 186 is classified using screen 290 (FIG. 3). Larger coal particles can be used directly in the coarse filter 114. The sieved smaller coal particles and the coal dust are shaped in the pelletizing device 292 (FIG. 3) into pellets of the desired particle size. These pellets also serve to fill the coarse filter elements 120. To produce activated carbon, the filter carbon originating from the reactor 186 is pretreated, i.e. it is finely ground in a grinding plant, then optionally pelletized and in turn ground to a desired grain size. The activation takes place in the activation device 294,

which is optionally followed by a further pelletizing device 296. The activated carbon obtained serves to fill the fine filter 116 or can be used for commercial purposes.

The above explanations clearly show that the waste recycling / waste water treatment system 102 can produce and regenerate the normal carbon and activated carbon required for cleaning the waste water in full.

6 shows a cracking device 192 according to a preferred embodiment according to the invention. The cracking device consists of a vertical double-walled container 298 in which an inner container 300 is suspended from the upper end 302 of an outer, carrying container 304. The inner container has an upper end 306, which is covered with an opening plate 308 that can be opened. The lower end of the inner container 300 has the constriction 310 and the sieve 312. Another screen 316 is located underneath.

A circular air supply line 318 surrounds the constriction 310. This air supply line 318 has a plurality of air nozzles 320 which serve to blow combustion air or oxygen into the interior of the container 300 directly via the sieve 312. Line 184 introduces the gas to be cracked into the upper portion of inner container 300 and ends in a downward hood 322. The interior of container 300 is filled with relatively large particles of a combustible material, preferably wood, so that it is fills the main part of the interior between the sieve 312 and the gas discharge hood 322. The wood immediately above the sieve 312 is ignited and oxygen for combustion is introduced via the air nozzles 320, so that a high-temperature zone is formed which, however, occupies only a relatively small area above the sieve, while the remaining combustible material inside the container 300 stays comparatively cool. After the high temperature zone has reached the desired temperature, the fuel or carbonization gas is introduced into the cracking device via line 184 and hood 322. In addition, the blower 324 is operated, whereupon a slight vacuum forms in the outer container 304, as a result of which the gas introduced via the hood 322 through the cool zone of combustible material and the high-temperature zone into the annular space 326 between the vessels via the suction line 328 and that Blower 324 is withdrawn.

The cracked gas obtained can either be fed directly to an internal combustion engine 202 or liquefied in the liquefaction plant 206 and optionally separated into a gas preferably based on methane and liquid nitrogen.

Periodically, the cracking device is supplied with new combustible material via cover 308. This feeding can also take place in a continuous manner.

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6 sheets of drawings

Claims (26)

644 888 1.Procedure for combined waste recycling and wastewater treatment, whereby the wastewater is mixed with at least part of the shredded waste, it is separated into organic and inorganic constituents, sedimented inorganic constituents and noting organic constituents of the waste are removed, the waste water flow with dissolved and suspended therein Components of the waste are passed through a two-stage filter made of non-activated and activated coal in countercurrent to the wastewater, solid waste in a first reactor of a multi-reactor kiln or part of the filter coal saturated with dirt load is burned to produce heat and fuel gas, in a second reactor most of the coal saturated with dirt load is thermally treated for regeneration, the dirt load adhering to the carbon filter being thermally decomposed to produce coal and carbonization gas, and the regenerated filter carbon of the second Reactor is returned to the wastewater filter zone, characterized in that the oxygen supply to the first reactor of the multi-reactor boiler takes place in a substoichiometric ratio such that the pyrolysis process is maintained, the temperature does not substantially rise above 800 ° C, a hydrocarbon-rich fuel gas being obtained and Heat is released which heats up the second reactor; Filter coal saturated with dirt load is degassed in the second reactor in an oxygen-free atmosphere and the dirt load adhering to the filter coal is thermally decomposed, a carbon-rich carbonization gas and coal being obtained; and at least part of the coal produced or regenerated in the second reactor is subjected to a pelletizing process. 2. The method according to claim 1, characterized in that the regenerated filter carbon of the second reactor is activated before being returned to the waste water filter zone. 2nd PATENT CLAIMS 3rd 644 888 lyse and a second reactor for thermolysis is supplied. 3. The method according to claim 1, characterized in that the first reactor is arranged in the lower part in the immediate vicinity of the other reactors of the multiple reactor. 4. The method according to claim 1, characterized in that the second reactor is arranged in the upper part of the multiple reactor 5. The method according to claim 1 to 3, characterized in that the furnace material located in the reactors of the boiler is continuously mixed, the mixing optionally being carried out by rotating the reactors about a horizontal axis. 6. The method according to claims 1 to 5, characterized in that the multiple reactor kiln comprises several reactors of the first and second type. 7. The method according to claim 1, characterized in that the combustion of the solid waste takes place in the first reactor of the multiple reactor kiln at 500 to 800 ° C. 8. The method according to claims 1 to 7, characterized in that the oxygen supply in the first reactor of the multiple reactor is 30 to 90% of the stoichiometrically required amount of oxygen. 9. The method according to claim 1, characterized in that from the filter coal or regenerated coal obtained in the second reactor, the coal particles which are below a desired particle size and the coal dust are separated, the separated coal is pelletized into coal pellets, and then optionally the pelletized coal is mixed with the previously separated coarser coal particles. 10th 10. The method according to claim 9, characterized in that the pelletized coal and / or the sorted coarser coal particles are used as filter coal in the first filtration section. 11. The method according to claim 1, characterized in that the coal produced in the second reactor of the multiple reactor boiler is activated after pretreatment and optionally pelletized. 12. The method according to claim 11, characterized in that the newly obtained or regenerated filter carbon is finely ground before activation and mixed with tar or pitch in a weight ratio of 10: 1 to 5: 1, the mixture obtained using high pressures and at temperatures, which are above the softening point of the respective binder, compacted and then ground down to the desired particle size. 13. The method according to claim 11, characterized in that the newly obtained or regenerated filter carbon is finely ground before activation and mixed with tar or pitch in a weight ratio of 10: 1 to 5: 1, the mixture obtained using high pressures and at temperatures, which are above the softening point of the respective binder can be pressed directly into shaped articles of the desired size using extrusion presses. 14. The method according to claim 1, characterized in that the fuel or carbonization gas for the splitting of long-chain hydrocarbons into short-chain hydrocarbons is passed through a low-oxygen high-temperature zone with a temperature of at least 1300 ° C. 15 15. The method according to claim 14, characterized in that the splitting of the fuel or smoldering gases takes place in the absence of oxygen. 16. The method according to claim 14, characterized in that said high-temperature zone is generated by filling flammable substances in a vertical container, burning them at the lower end of the container by blowing in a metered amount of oxygen, and the fuel gas in the downward direction by the device is passed, the amount of oxygen being metered in such a way that a controlled combustion of the substances and the generation of the desired temperature is ensured. 17. The method according to any one of claims 14 to 16, characterized in that combustible substances are introduced into the device, the upper part of the device filled with these substances being used for the adsorption of the solid and liquid particles carried by the fuel or smoldering gases, while the lower part of the device represents a high temperature zone. 18. The method according to claim 14, characterized in that the gases emerging from the high-temperature zone are cooled to a sufficient extent to liquefy them, with a separation into liquid nitrogen and a liquid, combustible, nitrogen-free gas optionally taking place. 19. The method according to claim 14, characterized in that the gases coming from the high temperature zone for energy generation are introduced into a gas combustion device. 20th 20. The method according to any one of claims 14 to 19, characterized in that the resulting exhaust gases are passed through a heat exchanger, the thermal energy being transferred from the exhaust gases to the heat exchange medium. 21. The method according to claim 20, characterized in that at least part of the thermal energy obtained from the exhaust gases is a first reactor for Pyro5 22. The method according to claim 20, characterized in that the heat obtained from the exhaust gas is used for pre-drying solid waste and / or filter carbon saturated with dirt load. 23. The method according to claim 20, characterized in that the exhaust gas is passed through a carbon filter to remove particulate contaminants. 24. The method according to claim 14, characterized in that the heat obtained from the exhaust gas is used via a second heat exchanger to heat the water for backwashing saturated activated carbon in order to facilitate the desorption of the filtered-out substances which adhere to the activated carbon. 25. The apparatus for performing the method according to claim 1, with a waste water supply with sedimentation tanks, coarse and fine filter elements located therein with coal or activated carbon, as well as waste crushing devices, a multiple reactor with a pyrolysis reactor as the first reactor and a thermolysis reactor as the second reactor, the immediate are arranged in spatial proximity, waste or filter coal pre-drying devices, characterized by a pelletizing device downstream of the thermolysis reactor for pelleting the emerging coal and grinding devices, and a cracking device for splitting the fuel in the fuel or. Long-chain hydrocarbons containing carbonization gas. 25th 30th 35 40 45 50 55 60 65 26. Use of the hydrocarbon-rich carbonization gas obtained by the process according to claim 1 for the production of short-chain hydrocarbons in a thermal cracking device.