DE102012103034B3 - Catalytic thermolytic treatment of organic waste, comprises e.g. mixing shredded waste in feeding device with aggregate mixture and tar originating from the process, and supplying obtained mixture into vertically disposed main reactor - Google Patents

Abstract

Catalytic thermolytic treatment of organic waste, in which the shredded organic waste is decomposed in an indirectly heated main reactor (1), comprises: e.g. (a) mixing the shredded waste in a feeding device (41) together with an aggregate mixture and tar originating from the process by a horizontally arranged feed screw (4); (b) supplying the obtained mixture into a vertically disposed main reactor; and (c) conveying the resulting raw gas and the primary coke through the transfer in to a coke reactor (2) which is arranged parallel with the main reactor. Catalytic thermolytic treatment of organic waste, in which the shredded organic waste is decomposed in an indirectly heated main reactor (1), comprises: (a) mixing the shredded waste in a feeding device (41) together with an aggregate mixture and tar originating from the process by a horizontally arranged feed screw (4); (b) supplying the obtained mixture into a vertically disposed main reactor, in which through a first conveying device (11) in a period of 20-60 minutes, preferably 35-45 minutes feed located on the bottom transfers to the top at 500-550[deg] C; (c) conveying the resulting raw gas and the primary coke through the transfer in to a coke reactor (2), which is arranged parallel with the main reactor; (d) downwardly moving by a second conveying device, where the coke in the primary coke and further crude gas are decomposed by after decomposition process; (e) supplying the coke at the bottom of the coke reactor by a third conveying device for coke activation; (f) heating the raw gas resulting from the main reactor and from the coke reactor, in a gas reactor, and supplying through the transfer line into a tar treatment reactor (64), where pollutants are cleaned by the treatment with a second aggregate mixture of and is supplied to a tar distillation, in which tar and particulate matter are deposited, the crude gas in a connected condenser is cooled to 150-120[deg] C, in which the oil components and the residues of second aggregate mixture are deposited and processed in a gas treatment with the addition of an additive mixture to synthesis gas; (g) supplying the synthesis gas together with the synthesis gas resulting in coke activation for heating the combustion chamber, which surrounds and heats the main reactor, coke reactor and the gas reactor; (h) supplying the synthesis gas, which is not needed for heating, to an energetic use; (i) recirculating the deposited tar in the tar distillation to the feeding device continuously; (j) using a mixture of urea and ammonium carbonate in a ratio of 1:2 in an amount of 1.5-3.5% of the shredded waste mass as an aggregate mixture; (k) using a mixture of ethylene glycol and ethanolamine in the ratio of 3:1-5:1 in the amount of 1.5-3.5% of the shredded waste mass as the aggregate mixture; (l) using a mixture of ethylenediamine, EDTA dipotassium salt and tetrabutyl phosphate in the ratio 10:2:1-5:1:1 in the amount of 0.5-1.5% of the shredded waste mass is used as the aggregate mixture. An independent claim is also included for a device for thermal processing of organic waste, comprising a material feed, a reactor block, a tar precipitation, gas scrubbing, the evaporator and the activated coke treatment, where (i) the material feed comprises a funnel-shaped feeding device and the feed screw, which is located below, whose outlet opens into the lower end of the main reactor, and the material feed further comprises devices for introducing the aggregate mixture and merges the tar originating from the process, (ii) the reactor block comprises a combustion chamber, which is heated from the synthesis gas at 500-550[deg] C, where the vertically disposed the main reactor extends through the combustion chamber, in which an inner conveying device is driven in the form of a motor, through which a perforated conveyor screw encloses in the upper region, the coke reactor is arranged in parallel with the main reactor in the combustion chamber, in which further inner conveying device is driven in the form of the motor, through which a completely perforated conveyor screw encloses, and the transfer connects the main reactor and the coke reactor at their upper ends, (iii) a gas reactor is arranged in the combustion chamber downstream to the main reactor and the reactor coke, where the gas reactor is parallel and perpendicular to the main reactor and the reactor coke, where the third conveying device for the coke is connected with the coke reactor through a tunnel above and opens at the upper end in the transfer line for the tar treatment reactor, (iv) the tar precipitation comprises the transfer line, tar treatment reactor and tar distillation, where tar treatment reactor is connected on gas reactor by the transfer line, where the tar distillation is located below tar treatment reactor, in which the aggregate mixture injected in the tar treatment reactor can flow in the tar distillation, where a gas line leads from the tar distillation for gas cleaning, and another line for tar transport leads from the bottom of the tar distillation for feeding device; (v) the gas scrubbing comprises a capacitor for the deposition of evaporated aggregate mixture in the tar distillation, a collecting container, which captures these aggregate mixture, the catalytic treating pipe, a further capacitor, a gas scrubber and the gas dryer, which are connected with each other through a respective gas lines, (vi) the evaporator, which is connected with the outlet of the gas scrubbing, in which a heating pipe is supplied with a part of the waste heat of the combustion chamber as the heating medium, and a further line, which leads from the evaporator for coke activation and is used for steam supply for coke activation; and (vii) the activated coke treatment is located below the gas reactor and consists of the third conveying device, which begins at the lower discharge port of the coke reactor and opens into the coke activation, where the coke activation and the capacitor serves for condensation of the steam, which is not converted in the coke activation.

Description

The invention relates to a method and a device for the catalytic thermal processing of organic waste. It is particularly suitable to work up organic waste to activated coke and fuel gas while avoiding harmful by-products such as dioxin and furans.

Since 2005, the deposition of organic waste, such as plastics of all kinds, waste wood, paper, rejects, shredder fractions z. B. from car recycling, sorted household waste, bitumen, waste oils, used tires, Siebresten and textiles only allowed if the Glückückstand is below 3 wt .-%. Organic waste with a higher incineration residue must currently be separated into secondary raw materials and residual waste in a complex process. This can then be worked up only by pyrolysis or combustion.

With high water and / or a large proportion of plastic combustion and pyrolysis is not without problems. During combustion, the large chlorine content of z. As PVC, PCB and dioxin formation is an environmental problem dar. In addition, the high cost of this thermal utilization to name a disadvantage. In pyrolysis further problems have occurred, for. B. settling and constipation from tars and dusts in the gas line.

Furthermore, it has already been proposed, organic waste in particular shredded from household waste, scrap tires, biomass, plastics, intensive with an olefin mixture, especially waste oil in a ratio of organic waste to olefin mixture of 5: 1 to 2: 1, preferably 7: 2 to 5: 2 to mix a homogeneous suspension to subject this mixture to a heat treatment at temperatures of 200 ° C to 500 ° C, preferably 250 ° C to 300 ° C and solidify by cooling.

Ultimately, out of the DE 10 2007 047 931 A1 a method is known in which to be produced by thermolytic workup of organic waste activated coke and high calorific fuels. For this purpose, the shredded and dried organic waste in a main reactor to be decomposed into coke, oil and gas. Subsequently, the organic waste is ground and fed to the main reactor with the addition of a first aggregate mixture. This aggregate mixture causes a dioxin formation is prevented. In contrast to real catalysts, part of the substance enters into the starting product of the reaction.

In a main reactor, the organic waste is decomposed at temperatures of 500 to 650 ° C by thermolysis in coke, oil and gas.

The oily gas is fed to a condenser 7 with the addition of a second aggregate mixture to avoid any tar and dust settling by a conveyor 6. There, the oily gas is separated into a liquid and a gaseous phase.

The oil-free gas is then washed out with the addition of a third additive mixture in a wet gas cleaning and dried in a gas dryer. A disadvantage of this method and the proposed plant for this purpose that the process requires expensive excipients and is difficult to control.

The object of the invention is therefore to propose a simpler process for the treatment of organic waste, as well as uses for the produced by the process tar and dioxinfreie products in which the recyclables contained therein can be supplied to a further effective recovery.

According to the invention this object is achieved by a method according to the features of the main claim 1.

This method provides optimum results when operated according to the method steps of claims 2 to 5.

The inventive method for the catalytic thermal processing of organic waste for the thermal processing of organic waste assumes that shredded organic waste in an indirectly heated main reactor ( 1 ) are thermally decomposed.

For this purpose, the shredded waste (IN) in a loading device ( 41 ) together with an aggregate mixture (ZM1) and from the process derived tar (T) in a horizontally arranged feed screw ( 4 ) before passing to the main vertical reactor ( 1 ).

In this case, a mixture of urea and ammonium carbonate in the ratio 1: 2 in an amount of 1.5% to 3.5% of the mass of shredded waste (IN) is used as the additive mixture (ZM1).

In the main reactor ( 1 ), the mixture at temperatures of 500 to 550 ° C by an internal conveyor ( 11 ) in the form of a feed screw driven by a motor (M) in the upper region over a period of 20 to 60 minutes, preferably 35 to 45 minutes, from the feed below to the transfer above ( 12 ).

The materials of the additive mixture (ZM1) give off ammonia at 500-550 ° C, which reacts with the split-off chlorine, formed hydrochloric acid or mercaptans and avoids a competing reaction with the hydrocarbons and aromatics and the formation mainly of chloroaromatics. Furthermore, phenols and phenolic compounds react with the ammonia, so that their phenolic group is deactivated or blocked. As a result, no reaction between phenols and chloroaromatics can take place. This excludes the formation of dioxins and furans.

That in the main reactor ( 1 ) resulting raw gas (RG) and the primary coke are by a transfer ( 12 ) in parallel to the main reactor ( 1 ) arranged coke reactor ( 2 ).

Here they will be replaced by another conveyor ( 21 ) in the form of a by a motor (M) driven, fully perforated screw conveyor moves down, being decomposed by a Nachzeretzungsprozess the primary coke in coke (K) and other raw gas.

Due to the construction of the main reactor ( 1 ) and the coke reactor ( 2 ), the cracking process is very well controlled, so that the decomposition of the plastic and cellulose components by the addition of the additive mixture (ZM1) is controlled to the desired end products.

This control occurs both in the main reactor ( 1 ) as well as in the coke reactor ( 2 ) using the screw conveyor.

At the bottom of the coke reactor ( 2 ), the coke formed is conveyed by means of a further conveying device ( 51 ) of coke activation ( 52 ).

That in the main reactor ( 1 ) and in the coke reactor ( 2 ) resulting raw gas (RG) is in the gas reactor ( 3 ) and via a transfer ( 61 ) into the tar treatment reactor ( 64 ).

In the transfer ( 61 ) are two spiral brushes ( 62 ), which rotate about their longitudinal axis. They are alternately driven by a drive ( 63 ) from the gas reactor ( 3 ) into the tar treatment reactor ( 64 ), sprayed there with the additive mixture (ZM2) and thus cleaned of dust and tar.

Here, a mixture of ethylene glycol and ethanolamine in a ratio of 3: 1 to 5: 1 in an amount of 1.5% to 3.5% of the mass of shredded waste (IN) is used as the additive mixture (ZM2).

Aggregate Blend (ZM2) is a substance that forms chelate complexes with heavy metals and dihydric phenols, amines and thiols and separates them from the gas stream. These land in the tar distillation ( 65 ) and are pumped together with the sparingly soluble tars and passed to the feed tank.

By treatment with a second additive mixture (ZM2), the raw gas (RG) is purified of pollutants and a tar distillation ( 65 ), are deposited in the tar and suspended matter.

In a condenser (K1) connected thereto, the raw gas is cooled to 150 to 120 ° C, whereby the oil components and remainders of the second aggregate mixture (ZM2) are deposited.

The gas, which is largely freed from tar and dust, cooled to 120 to 150 ° C. in a condenser (K1), is introduced into a collecting container ( 71 ) and is separated from unreacted aggregate mixture (ZM2). It is then added to a catalytic treatment tube ( 72 ) placed in the combustion chamber.

In this, long-chain hydrocarbons are decomposed or fragmented in the raw gas (RG) by catalysts based on silicate and alumina.

Subsequently, in a condenser (K2) by cooling to 30-40 ° C still remaining in the gas remaining oils deposited. Thereafter, the gas is a gas scrubber ( 73 ) and washed out there with the additive mixture (ZM3). This additive mixture (ZM3) consists of a mixture of ethylenediamine, EDTA-dipotassium salt and tetrabutyl phosphate in a ratio of 10: 2: 1 to 5: 1: 1 and, depending on the composition waste (IN) in an amount of 0.5% used up to 1.5% of the mass of shredded waste (IN).

They neutralize the remaining inorganic substances such as HCI, SO2, SO3, NO, NO2 and other hydrogen halides. The end products are water-soluble and are used in the evaporator ( 8th ) using the waste heat (AW) from the combustion chamber ( 10 ) separated. These substances contain nitrogen, potassium, phosphates and calcium. These salts (S) can be used in the fertilizer sector.

Part of the waste water (AW) of the gas scrubber ( 73 ) is pumped ( 75 ) again the gas scrubbing ( 73 ) after it has been enriched with the aggregate mixture (ZM3). The remaining wastewater (AW) is removed in an evaporator ( 8th ) by means of a part of the waste heat (AW) of the combustion chamber ( 10 ) evaporated.

Finally, the gas is after a treatment in the gas dryer ( 74 ) fed as synthesis gas (SG) for further use.

The resulting water vapor (D) is the Koksaktivierung ( 52 ).

Here, the glowing coke (K) from the coke reactor ( 2 ) is reacted with water vapor (D), so that in the coke activation ( 52 ) Activated coke (AK) and synthesis gas (SG) are formed, wherein the synthesis gas (SG) is energetically used after drying in the condenser (K3).

For further explanation, the following is based on the sketch 1 a device according to the invention for the thermal work-up of organic waste, to be presented for carrying out the method. The sketch shows

1 the process scheme of a plant according to the invention.

This consists of the material supply 4 . 41 , the reactor block 10 . 1 . 2 . 3 , the tar separation 61 to 65 , the gas cleaning 71 to 75 , the evaporator 8th and activated coke processing 51 . 52 and K3.

The material feed 4 . 41 , consists of a predominantly funnel-shaped feeding device 41 and a feed screw located thereunder 4 whose exit into the lower end of the main reactor 1 flows together.

In the material feeder 4 . 41 open further facilities for introducing an aggregate mixture ZM1 and derived from the process Teer T.

The reactor block 10 . 1 . 2 . 3 includes a synthesis gas SG heated to temperatures of 500 to 550 ° C combustion chamber 10 through which is the vertically arranged main reactor 1 extends.

The main reactor 1 encloses an internal conveyor 11 in the form of a driven by a motor M, perforated in the upper region screw conveyor.

Parallel to the main reactor 1 is in the combustion chamber 10 a coke reactor 2 arranged, which is another internal conveyor 21 in the form of a driven by a motor M, fully perforated screw conveyor encloses.

A handover 12 connects the main reactor 1 and the coke reactor 2 at their upper ends.

In the combustion chamber 10 is behind the main reactor 1 and the coke reactor 2 also to these parallel and perpendicular to the gas reactor 3 arranged by a tunnel above the conveyor 51 for the coke with the coke reactor 2 is connected and at the top in the transition 61 to the tar treatment reactor 64 empties.

The tar separation 61 to 65 is made up of transition 61 , Tar treatment reactor 64 and tar distillation 65 together, the tar treatment reactor 64 by means of transfer 61 at the gas reactor 3 connected.

The tar distillation 65 is thus below the tar treatment reactor 64 so that one in the tar treatment reactor 64 Injected aggregate mixture ZM2 into the tar distillation 65 can flow.

From the tar distillation 65 leads a gas line for gas purification 71 to 75 ,

From the swamp of tar distillation 65 leads another line for tar transport to the feeder 41 ,

The gas cleaning 71 to 75 consists of a condenser K1 for the separation of tar distillation 65 vaporized aggregate mixture ZM2, a sump 71 collecting this aggregate mixture ZM2, the catalytic treatment tube 72 , another condenser K2, the gas scrubber 73 and the gas dryer 74 , which are each interconnected via gas lines.

The catalytic treatment tube 72 is in the combustion chamber 10 housed and is heated by this to the reaction temperature of the catalyst contained therein.

With the outlet of the gas scrubber 73 is the evaporator 8th connected to the over a heating line, a portion of the waste heat AW of the combustion chamber 10 is supplied as a heating medium.

Another line leads from the evaporator 8th for coke activation 52 and serves the steam supply.

The activated coke treatment 51 . 52 and K3 is below the gas reactor 3 and sits down from the conveyor 51 located at the lower discharge opening of the coke reactor 2 begins and in the coke activation 52 opens, the coke activation 52 and the capacitor K3, which is the condensation of in the coke activation 52 unreacted steam serves, together.

At the bottom of the gas wash 73 is a pump 75 connected, the part of the waste water W, after it has been enriched with the additive mixture ZM3, in the gas scrubbing 73 pumps it back.

LIST OF REFERENCE NUMBERS

61-65

tar precipitation

71-75

gas cleaning

1

main reactor

2

Koksreaktor

3

gas reactor

4

screw feed

8th

Evaporator

10

combustion chamber

11

First conveyor

12

handing over

21

Second conveyor

41

feeder

51

Conveyor

52

Koksaktivierung

61

reconciliation

62

to brush

63

drive

64

Teerbehandlungsreaktor

65

tar distillation

71

Clippings

72

treatment tube

73

gas scrubbing

74

gas dryer

75

pump

AK

activated coke

AW

waste heat

D

Steam

IN

scraps

K

coke

K1

Capacitor 1

K2

Capacitor 2

K3

Capacitor 3

M

engine

RG

raw gas

SG

synthesis gas

S

salts

T

tar

W

sewage

ZM1

Aggregate mixture 1

ZM2

Aggregate mixture 2

ZM3

Aggregate mixture 3

Claims (7)

Process for the catalytic thermal treatment of organic waste, comprising shredding organic waste in an indirectly heated main reactor ( 1 ) are decomposed, wherein 1.1. the shredded waste (IN) in a feeder ( 41 ) together with an aggregate mixture (ZM1) and from the process derived tar (T) by a horizontally arranged feed screw ( 4 ) and 1.2. a vertically arranged main reactor ( 1 ), 1.2.1. in which they are transported by a conveyor ( 11 ) over a period of 20 to 60 minutes, preferably 35 to 45 minutes, from the bottom feed to the top handover ( 12 ) and 1.2.2. while exposed to temperatures of 500 to 550 ° C, 1.3. the resulting raw gas (RG) and the primary coke by a transfer ( 12 ) in parallel to the main reactor ( 1 ) arranged coke reactor ( 2 ), 1.4. and by another conveyor ( 21 ) are moved down, being decomposed by a Nachzersetzungsprozess the primary coke in coke (K) and other raw gas, 1.5. the coke at the bottom of the coke reactor ( 2 ) by means of a further conveyor ( 51 ) of coke activation ( 52 ), 1.6. that in the main reactor ( 1 ) and in the coke reactor ( 2 ) resulting raw gas (RG) in the gas reactor ( 3 ) and heated via a transfer ( 61 ) the tar treatment reactor ( 64 ), 1.6.1. purified by the treatment with a second aggregate mixture (ZM2) of pollutants and a tar distillation ( 65 ), in which tar and suspended matter are separated, 1.6.2. in a condenser (K1) connected to it, the crude gas is cooled to 150 to 120 ° C, whereby the oil components and remains of the second aggregate mixture (ZM2) are deposited, 1.6.3. and finally in a gas treatment ( 71 to 74 ) with addition of an additive mixture (ZM3) to synthesis gas (SG), 1.7. this synthesis gas (SG) together with the in the coke activation ( 52 ) synthesis gas (SG) for heating the combustion chamber ( 10 ), the main reactor ( 1 ), Coke reactor ( 2 ) and gas reactor ( 3 ) and heated, 1.8. that ultimately not needed synthesis gas (SG) is used for energy purposes, 1.9. continue in the tar distillation ( 65 ) deposited tar (T) to the feed device ( 41 ), 1.10. as additive mixture (ZM1) a mixture of urea and ammonium carbonate in a ratio of 1: 2 in an amount of 1.5% to 3.5% of the mass of shredded waste (IN) is used, 1.11. as additive mixture (ZM2) a mixture of ethylene glycol and ethanolamine in the ratio 3: 1 to 5: 1 in an amount of 1.5% to 3.5% of the mass of shredded waste (IN) is used, 1.12. as aggregate mixture (ZM3), a mixture of ethylenediamine, EDTA-dipotassium salt and tetrabutyl phosphate in the ratio 10: 2: 1 to 5: 1: 1 in an amount of 0.5% to 1.5% of the mass of shredded waste (IN ) is used. Process according to claim 1, characterized in that in the coke activation ( 52 ) the glowing coke (K) from the coke reactor ( 2 ) is reacted with water vapor (D), so that in the coke activation ( 52 ) Activated coke (AK) and synthesis gas (SG) are formed, the synthesis gas (SG) is used after drying in the condenser (K3) for heating. A method according to claim 1 or 2, characterized in that in the tar distillation ( 65 ) of tar and dust largely freed, cooled in a condenser (K1) to 120 to 150 ° C raw gas (RG) in a collecting container ( 71 ) separated from unreacted aggregate mixture (ZM2) and in a catalytic treatment tube ( 72 ), which is placed in the combustion chamber is supplied, 3.1. in which are constructed by catalysts based on silicate and alumina, long-chain hydrocarbons are radically decomposed or fragmented from the raw gas, 3.2. Subsequently, in a condenser (K2) by cooling to 30-40 ° C still remaining in the gas deposited oils, then 3.3. is the gas of a gas scrubber ( 73 ), washed out there with the additive mixture (ZM3) and 3.4. after a treatment in the gas dryer ( 74 ) used as synthesis gas (SG) for energy. Method according to one of claims 1 to 3, characterized, 4.1. that the wastewater (AW) of the gas scrubber ( 73 ) partially via a pump ( 75 ) again the gas scrubbing ( 73 ) after it has been enriched with the aggregate mixture (ZM3), and 4.2. that the remaining wastewater (AW) in an evaporator ( 8th ) by means of a part of the waste heat (AW) of the combustion chamber ( 10 ) is evaporated, 4.2.1. wherein the resulting water vapor (D) for coke activation ( 52 ) is being used. Method according to one of claims 1 to 4, characterized in that in the transition ( 61 ) two spiral brushes ( 62 ), which are alternately driven by a drive ( 63 ) into the tar treatment reactor ( 64 ), sprayed there with the additive mixture (ZM2) and thus cleaned of dust and tar. Device for thermal processing of organic waste, for carrying out the method according to one of claims 1 to 5, wherein 6.1. these from the material feed ( 4 . 41 ), the reactor block ( 10 . 1 . 2 . 3 ), the tar separation ( 61 to 65 ), gas purification ( 71 to 75 ), the evaporator ( 8th ) and activated coke treatment ( 51 . 52 and K3), with 6.1.1. the material feed ( 4 . 41 ), from a predominantly funnel-shaped feeding device ( 41 ) and a feed screw arranged underneath ( 4 ) whose exit into the lower end of the main reactor ( 1 ), 6.1.1.1. and in the material feeder ( 4 . 41 ) other facilities for the introduction of an aggregate mixture (ZM1) and tar derived from the process (T), 6.1.2. the reactor block ( 10 . 1 . 2 . 3 ) from a synthesis gas (SG) heated to temperatures of 500 to 550 ° C combustion chamber ( 10 ), 6.1.2.1. through which the main reactor ( 1 ), 6.1.2.1.1. an internal conveyor ( 11 ) in the form of a screw conveyor driven by a motor (M) and perforated in the upper part, 6.1.2.2. that parallel to the main reactor ( 1 ) in the combustion chamber ( 10 ) a coke reactor ( 2 ), 6.1.2.2.1. the one another an internal conveyor ( 21 ) in the form of a fully perforated auger driven by a motor (M), 6.1.2.3. a handover ( 12 ) the main reactor ( 1 ) and the coke reactor ( 2 ) at their upper ends, 6.1.3. in the combustion chamber ( 10 ) behind the main reactor ( 1 ) and the coke reactor ( 2 ) to these parallel and also perpendicular to the gas reactor ( 3 ), 6.1.3.1. through a tunnel above the conveyor ( 51 ) for the coke with the coke reactor ( 2 ) and at the top in the transition ( 61 ) to the tar treatment reactor ( 64 ), 6.1.4. tar separation ( 61 to 65 ) from reconciliation ( 61 ), Tar treatment reactor ( 64 ) and tar distillation ( 65 ), the tar treatment reactor ( 64 ) by means of transfer ( 61 ) at the gas reactor ( 3 ), 6.1.5. and tar distillation ( 65 ) so below the tar treatment reactor ( 64 ), 6.1.5.1. in the tar treatment reactor ( 64 ) injected aggregate mixture (ZM2) into the tar distillation ( 65 ), 6.1.5.1.1. from tar distillation ( 65 ) leads a gas line for gas purification ( 71 to 75 ), 6.1.5.1.2. another line for tar transport leads from the bottom of tar distillation ( 65 ) to the loading device ( 41 ), 6.1.6. the gas purification ( 71 to 75 ) consists of a condenser (K1) for the separation of tar distillation ( 65 ) evaporated aggregate mixture (ZM2), a collecting container ( 71 ), of the collects this aggregate mixture (ZM2), the catalytic treatment tube ( 72 ), another condenser (K2), the gas scrubber ( 73 ) and the gas dryer ( 74 ), which are connected to each other via gas pipelines, 6.1.6.1. wherein the catalytic treatment tube ( 72 ) in the combustion chamber ( 10 ) and is heated by this to the reaction temperature of the catalyst contained therein, 6.1.7. with the outlet of the gas scrubber ( 73 ) is the evaporator ( 8th ), which is connected via a heating line, a part of the waste heat (AW) of the combustion chamber ( 10 ) is supplied as heating medium, 6.1.7.1. another line leads from the evaporator ( 8th ) for coke activation ( 52 ) and serves to supply steam for coke activation ( 52 , 6.1.8. activated coke treatment ( 51 . 52 and K3) is located below the gas reactor ( 3 ) and is made up of the conveyor ( 51 ), which at the lower discharge opening of the coke reactor ( 2 ) and into coke activation ( 52 ), the coke activation ( 52 ) and the condenser (K3), the condensation of the in the coke activation ( 52 ) unreacted steam, together. Device according to claim 1, characterized in that a pump ( 75 ) at the bottom of the gas scrubber ( 73 ), which, after being enriched with the aggregate mixture (ZM3), enters part of the waste water (W) into the gas scrubber ( 73 ) pumps back.

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