DE102005026027A1 - Process and assembly to treat organic household waste prior to disposal in a sequence of reactors in which they are hydrolysed and/or fermented under moist conditions - Google Patents

Abstract

Disclosed are a method of treating waste with organic matter, with uniform method steps depending on Grain size of the waste mixture different pulpers to release of the organic components in a dilution liquid and different ones Reactors to carry a hydrolysis and / or a wet rot, and suitable pulper and reactors. Furthermore, a suitable waste treatment plant is disclosed.

Description

The The invention relates to a process for the treatment of organic waste Ingredients according to the preamble of claim 1, a pulper for dissolving organic matter of Waste in a dilution liquid according to the generic term of claim 5 or 19, a reactor for carrying out a Hydrolysis and / or wet rot according to the preamble of claim 28 or 36 and such a pulper and / or Reactors containing waste treatment plant.

With the introduction the separate collection of organic household waste in Europe has increasing the mechanical biological treatment (MBT) of municipal waste Gained importance. The degradation of the biogenic mass is microbial, whereby a distinction is made between aerobic and anaerobic microorganisms can be. The aerobic conversion ultimately leads to the end products carbon dioxide and water and is called rotting. The anaerobic conversion is typical of the fermentation, The final products include methane, ammonia and hydrogen sulfide.

Known Procedures look different depending on the nature of the waste mixtures Process steps for waste treatment. The individual provision individual process equipment is very expensive.

In the DE 196 48 731 A1 An aerobic process is described in which the organic components of a waste fraction are washed out in a percolator and the residue is dried or dumped after drying, for example.

The percolation can be carried out, for example, in a box percolation plant according to WO 97/27158 A1. Also promising were experiments with a Siedeperkolationsanlage according to the DE 101 42 906 A1 , in which the percolation is operated in the boiling range of the process water.

The withdrawn from the percolator organically highly polluted discharge water is fed to the anaerobic degradation of a biogas plant, wherein the organic content implemented by means of methane bacteria and for energy production fed to a biogas combustion is. The above-mentioned aerobic treatment of waste in one Percolator has proven to be extremely competitive to the anaerobic processes and is becoming increasingly important.

In the EP 0 192 900 B1 the so-called Valorga process is described - in which the fermentation takes place in a fermenter, which is fed from below. The waste to be treated is guided in a plug-shaped manner to a discharge, which is arranged below the radially outer inlet opening. The promotion of the waste is carried out by injecting compressed biogas via gas nozzles which are arranged in several sectors of the fermenter, wherein each sector can be controlled individually in order to maintain the plug flow of the waste between the inlet opening and the discharge opening.

In the EP 0 476 217 A1 is disclosed a heated fermenter, fed in the fresh and digested as bacterial inoculum the fermenter and the resulting digestate are transported via a stirrer to a Faulgutaustrag. Such addition of inoculum can also in the Valorga method described in accordance with the EP 0 192 900 B1 be provided.

The EP 0 794 247 A1 discloses a fermenter in which the fermentation product is introduced into a rotating drum in which a spiral is arranged. About this spiral, the digestate is grafted from the entrance to Faulgutaustrag. This promotion can be done by forward and backward rotation of the drum, the forward rotation, ie the transport of the fermentation in the direction of Gärgutaustrag takes longer than in the opposite direction, so that a predetermined residence time of the fermentation is achieved.

at the above-described known method is treated dry waste, of a comparatively high dry matter content (TS) of more than 25%.

In the treatment of flowable, moist waste, for example, according to the DE 197 04 065 A1 So-called pulper (Pulper) used in which the waste is diluted with a diluent and torn by means of a mixer and crushed, so that a suspension is formed and organic components in solution in the dilution liquid go. In the known solution, the mixing is carried out by means of a stirrer, the blades are designed so that in sections, a vertical flow is formed in the pulper. A disadvantage of this solution is that, on the one hand, a considerable outlay on equipment is required to form the complex geometry of the stirrer blades, and, on the other hand, these blades are subject to considerable wear due to the floating and impurities contained in the suspension.

In the DE 196 24 268 A1 is a fermentation process for waste in a flowable form, disclosed. In this case, a multi-chamber reactor is used, wherein the transport of the fermentation product can take place from an inlet opening through the chambers to a discharge opening via an agitator. The multi-chamber reactor is assigned a common gas space from which the biogas produced during the fermentation process is withdrawn. The metabolism can be controlled individually in the individual chambers by means of different process control, for example via heat exchangers, addition of inoculum etc.

Since the waste to be treated also contains a not inconsiderable proportion of heavy and foreign substances, in particular the solutions with mechanical conveying agents ( EP 0 794 247 A1 . EP 0 476 217 A1 . DE 197 04 065 A1 . DE 196 24 268 A1 ) subjected to relatively heavy wear, since the funds used and other installations can be damaged by the sediments with the Stör- / Schwerstoffen.

In contrast, lies The invention is based on the object, a uniform method to treat waste with organic matter. Furthermore, it is an object of the present invention pulper and Reactors for use in such a method and a appropriate waste treatment plant to accomplish.

These The object is achieved by a method having the features according to the claim 1, a pulper with the features of claim 5 or 19, a reactor with the features of claim 28 or 36 and by a waste treatment plant solved with the features of claim 41.

One according to the invention preferred Method has a mechanical treatment of the waste, a solution organic components in a pulper, a hydrolysis of the the pulper withdrawn biological contaminated suspension in a reactor and a fermentation in a fermentation stage on, wherein the process water obtained in the hydrolysis or the fermenter circulated as circulating water becomes. According to the invention is dependent from the grain size of the mechanically processed Waste mixture of the pulper to be used in the plant and / or Reactor selected. This has the advantage that the process for different waste mixtures is identical and only the plant parts pulper and reactor depending of the grain size to select the waste are. A preferred "marginal grain size" is about 80 mm.

advantageously, is additional for hydrolysis, a wet rotting or wet oxidation provided, the in a reactor corresponding to the hydrolysis reactor.

to Introduction of a substantially solids-free biological Suspension in the fermenter can suitable separation steps for separating contaminants, heavy materials, fibrous materials, etc. be provided.

According to the invention the solution the organic components at a maximum grain size of about 80 mm in a pulper, instead of a known mechanical agitator a quasi-pneumatic agitator in which by injecting gas, preferably air, through the Suspension in the pulper mixed and the organic components as a solution in the dilution water, through the one suspension flow in the pulper is produced.

These pneumatic solution has virtually no wear and can be with much less implement device-technical effort as it is the conventional solutions the case is. It turned out that the organic components in much shorter Time to be solved in the constructions with mechanical agitator can.

The Mixing can be continue to improve when the gas injection nozzles part of a gas flow pump are about the periodically or continuously pumped around the suspension within the substance removal container is. The gas can also be pressed into the bottom of the substance removal container so that too the accumulating there sturgeon / heavy materials be mixed with the gas.

These Gas flow pump preferably has an inner tube, at the bottom End portion of the suspension or flow-through nozzle plate with gas injection nozzles is arranged and whose upper end portion has an outlet opening for in the Inner tube transported suspension is formed.

at a particularly effective working embodiment is at a distance to the outlet arranged a baffle plate against which the gas flow pump funded Blend at high speed bounces and unlocked becomes. The organic components pass into the water phase. Inert material and sand sink down and can be removed. In the suspension containing pulps and solids rub during this advancement towards the baffle plate together and in addition of persistent organic components freed.

In a preferred embodiment The baffle plate is partially bounded by a gas removal space, via which the recirculated gas is drawn off.

at huge container volumes It may be advantageous to arrange several gas flow pumps in the substance dissolving tank.

It becomes according to the invention particularly preferred when the inner tube is double-walled, the gas injection nozzles are then arranged either in the inner cylinder chamber or in the annular space and the other space is used to hold a heating medium, so that the inner tube simultaneously acts as a heat exchanger, over the the suspension is kept at a process temperature.

The Mixing leaves continue to improve when on the outer circumference of the inner tube baffles arranged for flow guidance are. Since these baffles are fixedly arranged in the pulp container, their Minimal wear.

at certain applications It may be advantageous to operate several pulpers in series.

One Inventive pulper for Solve organic Ingredients of waste with a minimum grain size of about 80 mm in a dilution liquid according to the invention at least one mechanical agitator before, its respective adjacent stirring elements opposite directions of conveyance exhibit. This has the advantage of being in the pulper itself Mixture between the stirring elements towards each other or promoted away from one another so that improved abrasion and thus improved solution the organics can be achieved.

Preferably are the stirring elements Rotor blades arranged on a rotor whose blade pitch angle each about 180 ° to each other are offset. The number of rotor blades is arbitrary, however If an even number, for example 6 rotor blades, is preferred.

The rotor blades can evenly on the Rotor from an entry lock for the waste up to an exit opening for separated disturbance / heavy materials be distributed.

As well It is conceivable that the pulper several parallel rotors having, wherein the rotor blades each of the individual rotors form an overlap area.

at a particular embodiment can in the area of the discharge opening arranged a gas injection to the Aufwirbelung the Stör- / Schwerstoffe be. It is possible that the injected gas is circulated so that the required amount of gas is reduced.

Of the pulper can be in longitudinal section have a rectangular shape, with its length L1 at least four times Height h1 equivalent.

According to the invention is at the hydrolysis and / or wet rot of the suspension from the waste with a maximum grain size of about 80 mm a reactor with a mechanical mixer for mixing the substance mixture and with a guide tube, which uses the Embraces mixer. The mixer is controlled in this way, that the substance mixture from a reactor head side to the reactor bottom side through the draft tube is sucked, being outside of the guide tube forms an ascending loop-shaped flow.

to Optimization of the hydrolysis or wet rotting, the guide tube has an axial renewal to change his length or height. Furthermore you can several guide tubes, for example 3 guide tubes, with correspondingly reduced Diameter be arranged in a reactor.

Of the for the Hydrolysis or wet rot needed Oxygen can over an oxygen injection near the bottom and / or in the area of Mixing done.

To regulate the amount of oxygen to be injected, an O ₂ probe may be provided which detects the O ₂ content, so that in response to these signals, the axial extension, the axial position of the guide tube and / or a mixture mixture level is adjustable so that preferably one optimal, ie almost 100%, oxygen utilization takes place.

Exemplary geometric relationships are, for example:
The guide tube height H1 corresponds to 8 to 10 times the guide tube diameter d1,
the effective diameter d2, ie the inner diameter of the reactor, corresponds to 4 to 6 times the guide tube diameter d1,
the ground clearance H2 from the reactor bottom to the guide tube corresponds to 1 to 2 times the guide tube diameter d1, the distance between the mixture mixture and the guide tube corresponds to 2 to 3 times the guide tube diameter d1,
the variable height adjustment H4 between the mixture mixture and the guide tube is 0.5 to 2 times the guide tube diameter d1,
the flow velocity v1 of the circulating flow is between 0.1 m / s and 0.8 m / s,
the guide tube diameter d1 is depending on Stoffge mixed composition and the dry matter content between 0.5 m and 1.5 m.

Overheating the mixture of substances can effectively by a cooling medium flowing around the guide tube be prevented.

Basically several hydrolyses or wet rots can be arranged in series.

One inventive reactor for processing a supplied organically loaded suspension consisting of a waste mixture with a minimum grain size of about 80 mm, has as a mixing device for mixing of the substance mixture a blowing device for gas, preferably oxygen.

The Gas injection is preferably carried out via a plurality of gas injection nozzles near the bottom of the reactor and is over a gas measuring probe adjustable.

preferably, the gas is over a pump in the circuit feasible.

to increase the mixing can in the reactor resulting exhaust gases also in the mixture near the ground the engine over a fan be pressed in.

A with the pulper executed Waste treatment plant preferably has a solids preparation for separating and washing the purged / sediment taken from the pulper.

According to the invention, the Waste treatment plant also a separation stage for separating Fibers or the like of the removed from the pulper have open-digest suspension. This separation stage preferably has a car wash and a drainage press up, over which cleaned the separated fiber / floating matter and one fed further use can be.

In addition to The Faserstoffabscheidern the waste treatment plant with a sand wash designed for washing fine sand be, after the separation of the fibers still in the remaining Suspension (dilution water) included is.

The The dilution water containing the organic components is preferably fed to a fermenter, by converting these organic constituents to biogas and / or as mixed water of a wet rot or wet oxidation fed become.

The dilution water freed from the organic components then becomes again to the pulper recycled, with excess water a Wastewater treatment plant supplied can be.

The the pulper supplied Solid fractions are preferably by an upstream solids treatment minimized.

It has been shown that the Lead time through the treatment plant according to the invention of conventional around 61 days can be reduced to about 29 days if the open-minded Suspension of the pulper undergoes hydrolysis at least as part of stream and then from Fiber and solids is released, the solids at least as a partial stream the wet rot or wet oxidation to obtain a go through oxidized substance mixture.

at the hydrolysis, the suspension of the pulper aerobically acidified and the not yet digested organic material also open-minded, so that the Fermenter additional Material can be fed is.

Also Is it possible, at least a partial stream downstream in one of the hydrolysis Separator separated solids a drying and compaction for the production of fittings for gasification and incineration plants. Preferably, the Compaction under low pressure and with admixture of a binder, as an adhesive until Verglühung in the gasification and Incinerator works. The binder can during waste treatment self-generated, for example, separated plastics, or delivered be.

For the gasification process have to the fittings in the glowing State "gasification stable", that is, until the form remains intact for ashing.

In one embodiment of a treatment plant, the suspension treated during the hydrolysis is fed directly to the fermenter. Since the then discharged during the fermentation discharged wastewater may still have a high solids content, this should not be added to the dilution water or circulating water. However, an admixture can be achieved by substantially separating the solids from the wastewater in a separation plant, so that the wastewater is free of solids. The dewatered solids can then be subjected to a wet rotting, wherein for optimum adjustment of the solids content, a partial stream of the solids-free wastewater ver again with the solids to a suspension is miscible.

at another embodiment In a treatment plant, the solids get out of the hydrolysis into the wet rotting or wet oxidation. It is by fumigation with Oxygen, the non-anaerobically degradable organics respirates and the Nitrogen expelled as ammonia.

The after the wet oxidation oxidized mixture can a separation plant with a solids separator, a Feststoffsieb- and washer and a dewatering press supplied become. It is possible that incurred in the solids separator wastewater as dilution water for the pulper to use and / or supply the wastewater treatment plant. Of the in the dewatering press resulting raw compost can be disposed of immediately.

preferably, is the mixture in the wet rotting mixed water, which in the Mixing of the circulating water with the wastewater of the fermenter arises, fed.

The in the wet rotting resulting oxidized substance mixture may be a separation plant for the production of raw compost and wastewater. It can the wastewater is mixed with the dilution water and / or fed into the wastewater treatment plant. Of the Raw compost may be subjected to rotting for drying and / or be disposed of immediately.

The in the hydrolysis and wet scrubbing exhaust gases can a Luftwäscher supplied for the liberation of ammonia become.

The Processing plant has particular for mechanically treated waste mixtures with a maximum grain size of about 80 mm the pulper according to the invention with pneumatic agitator and for hydrolysis and / or wet oxidation, the reactor of the invention with mechanical agitator on.

For mechanical treated waste mixtures with a minimum particle size of about 80 mm is preferably the pulper according to the invention with mechanical stirrer and for the hydrolysis and / or for wet oxidation of the reactor according to the invention with pneumatic agitator used. The latter can also be used with the smaller corm sizes become. The "Grenzkorngrösse" can depending on vary from the waste to be treated, these are 80 mm to be seen as an example.

advantageously, can at least in the reactor for the wet oxidation with appropriate operation, a sanitation of the substance mixture in the reactor.

To Relief of the gases produced during hydrolysis and wet oxidation of ammonia can be an air scrubber be provided, in which the ammonia is washed out.

other advantageous developments of the invention are the subject of further Dependent claims.

in the The following are preferred embodiments of the invention explained in more detail with reference to schematic drawings. Show it:

1 a schematic representation of a pulper according to the invention for waste mixtures with an approximate grain size less than 80 mm;

2 a schematic cross section of the pulper 1 ;

3 . 4 Cross sections of alternative embodiments of a pulper;

5 to 7 Schematic representations of different operating states of the pulper 1 ;

8th a variant of the pulper according to 1 ;

9 a waste treatment plant with a pulper according to 1 .

9a an alternative operating case 9 in a simplified and enlarged view (see also 19 )

9b another alternative case of operation 9 in a simplified and enlarged view (see also 19 )

10 a detailed view of a hydrolysis and a wet rotte 9 .

11 two in-line pulper according to the invention 1 .

12 a longitudinal section through an alternative pulp according to the invention for waste mixtures with an approximate grain size greater than 80 mm,

13a to 13d exemplary cross sections through the pulper after 12 .

14 a series connection of the pulper 12 .

15 a longitudinal section through a preferred embodiment of a reactor for the hydrolysis or wet scrubbing for waste mixtures with an approximate grain size less than 80 mm,

16 a cross section through a further preferred embodiment of a reactor for the hydrolysis or the wet rot,

17 a series connection of several reactor in the hydrolysis, and

18 a series connection of several reactor in the wet rotte

19 a simplified process diagram of the waste treatment plant according to the invention,

20 a hydrolysis reactor for waste mixtures with an approximate grain size greater than 80 mm,

21 an alternative wet rottereactor for waste mixtures with an approximate grain size greater than 80 mm,

22 a detailed substance separation system 19 .

23 a detailed separation system 19 and

24 a detailed process scheme of compacting 19 ,

In 1 is the basic structure of a pulper 1 represented in the organic components of a supplied input material 2 , preferably waste in a dilution liquid, for example dilution water 4 be solved, so that in the pulper 1 a mixture 8th is present, which has a dry matter content of about 5 to 10%.

Preferably, it has the pulper 1 added waste mixture on a grain size of about 80 mm at the maximum. The trash 2 and the dilution water 4 are each via entry locks 10 a pulp container 6 fed. A floor 12 of the substance removal container is conical and opens into a discharge opening 14 with an outlet lock 16 , over the conical bottom 12 settling interfering / heavy materials 18 can be deducted. In the area of the conical bottom 12 is another exit lock 16 educated about those in the pulper 1 digested organism-loaded suspension 20 subtracted and according to 9 prepared and then in the circulation as dilution water 4 via the entrance lock 10 is fed again.

Inside the fabric dissolving container 6 is a gas flow pump 24 arranged over the - as will be described in more detail below - the mixture 8th is mixed within the substance solution container. At the in 1 illustrated embodiment has the gas flow pump 24 an inner tube 26 , which is coaxial with the pulp container 6 is arranged and at his in 1 underlying inlet opening a nozzle plate 27 with a variety of gas injection nozzles 28 has, by a gas, preferably air can be pressed into the inner tube. The nozzle plate 27 can from the suspension 8th to be flowed around. The gas injection nozzles 28 are via a compressed air line 30 and a controllable by the plant control valve control 32 with a medium-pressure storage or air chamber 34 connected via an air compressor 36 is charged to a pressure of, for example 3 to 8 bar. This sucks via a suction line 38 transport air 40 from a gas exhaust room 42 at the head 22 of the substance removal container 6 on - ie, this transport air 40 is also circulated and by the appropriate control of the control valve 32 from the wind boiler 34 via the compressed air line 30 and the gas injection nozzles 28 in the inner tube 26 pressed.

About a Umschalteinrichtung- and / or metering device 66 downstream of the air compressor 36 can the wind boiler 34 with the control valve, ie the pulsation to be bypassed. This is a bypass line 154 piloted, the downstream of the control valve 36 into the compressed air line 30 empties. In this case, the mixture can 8th with the blower pressure, which is 1.5 times the manometric height, circulated.

Furthermore, in the compressed air line 30 a switching and / or metering device 66 be provided, from which a press-fit 156 in the discharge opening 14 of the pulper 1 extends. As a result, the interfering and heavy materials can be moved and mixed with compressed air, so that the adhering organics separates and into the mixture 8th passes.

2 shows schematically the cross section of the substance removal container 6 with the concentrically arranged gas flow pump 24 in which the inner tube 26 with a double jacket 46 is provided, which is flowed through by the so-called heating medium. Here are the gas injection nozzles 28 in the interior, from the inner tube 26 embraced cylinder space arranged.

In an alternative variant according to 3 can the gas injection nozzles 28 also in the double jacket 4b umgriffenen annular space may be arranged so that the heating medium flows through the central cylindrical space.

For very large container volumes, it may be advantageous to use several, for example, three gas pumps 24a . 24b . 24c in the substance dissolving tank 6 to arrange.

At a distance above an outlet opening of the inner tube 26 is a flapper 44 arranged that the gas exhaust room 42 limited in sections and laterally from the transport air 40 can be flowed around.

For heating the suspension 8th to the process temperature is the inner tube 26 with a double jacket 46 provided, wherein in the resulting annular space, a heating medium is guided, so that the inner tube 26 acts as a heat exchanger. The coat of the substance removal container 6 can be provided with an insulation.

For fabric release, this is in the fabric release container 6 inserted input material 2 first by feeding the recirculated dilution water 4 adjusted to a dry matter content TS of about 5 to 10%. Subsequently, by controlling the control valve 32 Compressed air via the gas injection nozzles 26 pressed. In the illustrated embodiment, a pulsating operation is preferred, wherein the pulse interval is for example about 5 to 10 seconds. The process temperature is over that in the double jacket 46 flowing heating medium to a temperature between 50 to 70 ° set. By this Druckluftpulsation arise in each case inside the gas flow pump 24 Compressed air bubbles 50 Similar to a piston of a piston pump mixture / suspension 8th from the ground 12 suck it in, so that inside the inner tube 26 an upward suspension flow 48 arises. This sucked suspension then hits at high speed, which can be in the range between 10 to 20 m / s on the baffle plate 44 on, by the impact and friction energy is a mechanical digestion and the organic components in the dilution water 4 go into solution.

The the inner tube 26 flowing compressed air 52 flows around the baffle plate 54 and is then in the area of the gas exhaust space 42 largely relaxed and used as transport air 40 from the compressor 36 sucked and again the wind boiler 34 supplied - the compressed air circuit is closed.

Inertstoffpartikel contained in the waste, sand, Stör- / Schwerstoffe etc. are dissolved and sink to the conical bottom 12 down. Furthermore, fibers are released and go into suspension, which are cleaned by the shear forces introduced films and other solids content of adhering organic components. The accumulating impurities / heavy materials are via the outlet lock 16 and the discharge opening 14 on the ground 12 of the substance removal container 6 deducted. It was found that with the pulper of the invention, the organic components can be brought into solution much faster and with less device complexity than is the case with conventional pulpers, in which mechanical stirrers or the like are used.

The function of the gas flow pump 24 be again on the basis of 5 to 7 explained in more detail.

In 5 is the substance dissolving container 6 shown in the filled state of rest, in which the input material 2 by adding dilution water 4 is adjusted to the stated dry matter content of 5 to 10%. A level 54 of the substance mixture is adjusted so that it is below the upper outlet opening of the inner tube 26 the gas flow pump 24 lies. By the basis of 1 explained pneumatic circulation is caused by the upward suspension flow 48 Suctioned suspension and against the baffle plate 44 hurled and then flows back into the inner tube 24 and from the jacket of the fabric dissolving tank 6 limited annulus down. The proportion of the upwardly promoted suspension is so great that the level 54 within the substance removal container 6 by the amount Δh according to 6 decreases. Upon completion of air injection, d. h, in each case after the end of a compressed air pulse, the suspension column sinks within the inner tube 26 downwards (see 7 ) and the level 54 in the annulus 56 rises again until the ground state according to 5 - the next press cycle can begin. Due to the above-described flows within the substance removal container 6 and by the impact of the suspension on the baffle plate 44 an extremely intensive mixing of the suspension takes place, so that the organic constituents of the input material 2 be brought into solution very quickly and with high efficiency and also suspended the fibers and the Stör- / suspended matter sedimented. Because of this intensive mixing within the substance removal container 6 Virtually no moving components are required, is the wear of the pulper according to the invention 1 minimal compared to conventional solutions.

The mixing can be further improved if according to 8th in the annulus 56 Built-in, for example, downwardly inclined baffles 58 be provided by the. downwardly directed suspension flow ( 6 ) must be flowed around, so that further shear forces are introduced into the suspension. Because these baffles 58 are arranged stationary, their wear is also minimal. In the illustrated embodiment, the baffles 58 change wise on the inner circumferential shell of the substance removal container 6 and on the outer jacket of the inner tube 26 arranged so that in the annulus 56 the illustrated wavy flow results. Of course, instead of the baffles 58 also other internals or packing can be used.

In 9 a waste treatment plant is shown in which the above-described pulper 1 according to 1 is used.

In this waste treatment plant are the pulper 1 preceded by some steps for the separation of solids. This is the waste to be processed 60 first - if necessary after comminution - a sieve 62 supplied, which is designed in the illustrated embodiment as a rotary screen. The sieve overflow 64 with a grain size between 80 to 200 mm is then a material switch or switching and / or metering device 66 either eliminated directly or separated by an additional step. In the illustrated embodiment, via the switching and / or metering device 66 a partial flow or the entire solids flow to a sighting system 68 be guided, in which the sieve overflow 64 in heavy and impurities 70 as well as polluted light materials 72 separated, which are each eliminated.

The organically rich sieve run 78 can via a switching and / or metering device 66 a mixing plant 74 be fed, in which he with a partial flow of the denitrified dilution water 4 diluted and by means of a mixer 268 to a suspension 76 is processed with a solids content of 5% to 15%.

The suspension 76 becomes the entry lock 10 of the pulper 1 fed. impurities 160 , such as tapes, ropes and cables, are via a mechanical device of the mixing plant 74 from the suspension 76 separated and ejected.

The in the pulper 1 accumulating impurities / heavy materials 18 become from the pulper 1 over the outlet lock 16 deducted and a washing device 80 fed by containing persistent organic matter in a purification zone 106 by means of supplied operating water 82 getting cleaned. The cleaned heavy materials / contaminants 84 then become a ferrous metal separator 86 and a non-ferrous metal separator 88 supplied, so that the material flow 84 accordingly in a ferrous content 90 a non-ferrous metal component 92 and other substances 94 is split.

The over the exit lock 16 from the pulper 1 withdrawn digested suspension 20 is shared with the polluted service water 96 from the washing device 80 a pulp separator 98 supplied, which in turn is designed as a rotary screen. In this pulp separator 98 become fiber and floating matter 100 of organically-containing water 102 separated. The fiber / floating matter 100 be in a Feststoffsieb- and washer 104 by adding process water 82 cleaned, that of a cleaning zone 106 the washer is supplied. This cleaning process can additionally be supported by the cleaning zone 106 circulating water 108 is supplied to the conditioning circuit for the dilution water 4 is branched off.

The two washing facilities 80 . 104 are executed in the described embodiments in each case with obliquely inclined spiral conveyors, via which the respective stream to be cleaned to one of the cleaning zones 106 promoted and finally on a solids outlet 110 is deducted. In the cleaning zone 106 each organic components are replaced by the solids. In the case where a very intensive cleaning is required, this cleaning is essentially by means of process water 82 with lower requirements for this cleaning, the proportion of circulating water 108 be enlarged.

The cleaned and over the solids outlet 110 the car wash 104 stripped solid and fibrous materials 112 are then in a dewatering press 114 drained and the dehydrated solids 116 a thermal utilization or a Nachrotte fed for later landfilling.

That in the dewatering press 114 resulting, dissolved organics containing water 118 then with the from the cleaning zone 106 effluent laden with organic wash water 120 verschmischt. This stream contains a proportion of fine sand in a sand scrubber 122 is separated. The material flow is also the organikhaltige water 102 from the pulp separator 98 fed. In the sand scrubber is the fine sand content 124 by the action of a stirrer 126 separated, over a Sandaustrag 123 dissipated and by adding process water 82 purified from adhering organic components. The pre-cleaned fine sand 124 then becomes a fine sand washing facility 128 supplied, the basic structure of the washing device 80 . 104 corresponds, so that further explanations are unnecessary. The cleaned fine sand 130 can then be recycled for use in civil engineering and road construction.

The highly polluted circulating water present after the sand washing 132 it will then in a cache 134 cached and by means of a pump 136 either a fermenter 138 supplied or as circulating water 132 directly to a heat exchanger 140 supplied in which it by means of a heating medium 142 heated to the process temperature and then as a dilution water 4 via the entrance lock 10 in the pulper 1 is initiated. The heating medium 142 can also be used to heat the double jacket of the gas flow pump 24 be used.

Depending on the process, the organic component of the fermenter becomes 138 supplied water by methanation in biogas (methane gas) 144 implemented.

The effluent discharged from organic after the fermentation step 146 is then with the possibly existing circulating water 132 mixed and in the heat exchanger 140 brought to process temperature. In the cycle not needed excess water 147 becomes a wastewater treatment plant 148 fed and the purified wastewater 150 knocked off and discharged into the sewer. A partial stream of purified wastewater 150 is called process water 82 to the washing facilities 80 . 104 . 128 as well as the sand scrubber 122 led, so that the operating water cycle is closed.

Organic, in the digested suspension 20 containing components can be separated even faster from the waste, if via a switching and / or metering device 66 the disrupted suspension 20 of the pulper 1 first an aerobic hydrolysis or acidification stage 162 is fed and after a treatment time of 1 to 4 days, the suspension 20 of solids in the pulp separator 98 and the sand scrubber 122 is released. Subsequently, the thus treated suspension 21 as organically highly loaded circulating water 132 in the cache 13 stored and the fermenter 138 fed.

The separated solids and fibers 100 of the pulp separator 98 , followed by the Feststoffsieb- and washer 104 and drainage press 114 are passed through a switching and / or metering device 66 as dehydrated solids 116 with a dry matter content of 35% to 60% DM of a wet rot 164 fed and there via a switching and / or metering device 66 with the mixed water 158 diluted to a dry matter content of 5 to 15%.

After a residence time of 3 to 10 days in the wet rotte 164 becomes the oxidized and de-stained substance mixture 23 discharged and in a separation plant 168 freed of solids. The resulting almost solids-free wastewater 170 is then used as dilution water 4 the pulper 1 and / or via a switching and / or metering device 66 the wastewater treatment plant 148 fed. The resulting raw compost 212 is disposed of.

The hydrolysis 162 and at the wet-rotting 164 resulting exhaust gases are common in an acidic air scrubber 172 freed from ammonia.

through the above-described waste treatment plant can be the organic Components of the waste with a very low technical device Separate effort and the remaining material flow into usable or disposable streams of particles separate.

According to 9 it is also possible in an operating case, the separating device 98 . 104 . 114 . 122 . 128 to drive around and in the hydrolysis 162 prepared suspension 21 directly to the fermenter 138 to be supplied, via a switching device and / or metering device 66 a suspension mixture 133 from the organically highly polluted wastewater 132 and the prepared suspension 21 will be produced. The wastewater containing solids 146 of the fermenter 138 is via a switching device and / or metering device 66 wet rotting or wet composting 164 supplied as digestate.

The oxidized substance mixture 23 after the wet rot 162 is then according to 9a for separating the solids of a substance separation with a filter device 206 , a sand washer 122 and a dewatering press 208 undergo. The solids-free wastewater obtained during separation 170 is used as dilution water or circulating water 4 used. The solids separated during the separation of substances 212 can a rotting 214 being subjected to that in the rotting 214 resulting dry product 216 a screening 218 passes through, in which the remaining materials 224 and compost 212 is separated. The remaining materials are z. B. a material recovery.

If the fermenter 138 predominantly with the solids-containing suspension 21 after hydrolysis 162 can be loaded, the loaded with solids wastewater 146 only in the circulation of dilution water 4 be introduced if as in 9 indicated and in 9b enlarged shown the solids and fibers previously in a separation plant with the solids deposition 98 , the Sieb sieve and washer 104 and the downstream dewatering press 114 were separated. The regulation or control of the wastewater 146 via a switchover and / or Do siereinrichtung 66 , The in the fermenter 138 fermented and in the separation plant 98 . 104 . 114 separated solids 116 become the wet rot 164 fed, being in the separation plant 98 . 104 . 114 pressed-off sewage water 171 at least as a partial stream again for mixing with the solids 116 is used to one in the wet rot 164 adjust ideal dry matter content. For example, the dry matter content may be between 5-15%. The excess of the sewage water 171 is called circulating water wastewater 170 the wet rot 164 slammed and is thus as dilution water 4 for example the pulper 1 fed.

According to the invention, the final concentration of the waste-laden wastewater 146 from the fermenter 138 in the separation plant 98 . 104 . 114 As a result, that by the at least partial recycling of solids-free sewage water 171 to the pressed solids 116 the solids content in the wet rot 164 can be optimally adjusted and the wet rottereaktor 192 is considerably smaller dimensions and the excess solids-free digested water 171 into the circulation of dilution water 4 can be pressed.

10 shows a process scheme with the hydrolysis 162 , the wet rot 164 , the separation plant 168 as well as with the acidic air scrubber 172 ,

With the hydrolysis 162 becomes the digested suspension 20 aerobic acidified and organic material is digested so that it also fermentation in the fermenter 138 is available. Of the non-anaerobically degradable substances, the adhesive grain and the dirt are separated.

The hydrolysis 162 essentially comprises a reactor 174 in which a mechanical stirrer 176 for mixing the substance mixture is arranged (see. 12 ). Near the bottom of the reactor 174 is a blowing device 178 designed to inject oxygen through an oxygen supply 180 is fed. Above a mixture of substances 186 is an exhaust room 188 formed in which the hydrolysis 162 resulting exhaust gases 190 collect.

The digested suspension 20 of the pulper 1 is near the bottom above the blowing device 178 the reactor 174 fed. By the introduction of oxygen and by the operation of the stirrer 176 the mixture is mixed and after a treatment time of 1 to 4 days as a prepared suspension 21 near the substance mixture mirror 186 taken.

In the wet rotten 164 The non-anaerobically degradable organics are inhaled and the nitrogen expelled as ammonia. In the wet rotten 164 By fumigation the circulation water 132 . 133 . 4 entickickt and thus prevents a concentration of ammonium, which is the biology in the fermenter 138 disturbs and inhibits the gas production and degradation performance.

The wet rot 164 essentially has a reactor 192 in which a stirrer 194 for mixing the substance mixture 23 is arranged (see. 12 ). Near the bottom of the reactor 192 is a blowing device 196 provided for the injection of oxygen, which has the same oxygen supply 180 like the hydrolysis 162 is fed. Above a mixture of substances 198 is an exhaust room 200 for collecting the resulting exhaust gases 202 educated.

To overheat the mixture in the wet rotte 164 To avoid is a refrigeration unit 182 intended. The refrigeration unit 182 is with a lead 184 and a return 204 connected, which dip into the mixture. To cool the mixture is by the flow 184 and the return 204 Promotes coolant, whereby excess heat in the mixture can be dissipated.

The solids 116 be near the stirrer 194 in the reactor 192 filled. In addition, the heavily ammonia contaminated mixed water 158 above the solids 116 in the mixture 192 directed. The mixture of substances is passed over the stirrer 194 and the oxygen introduced and after a residence time of 3 to 10 days the reactor 192 as treated and oxidised substance mixture 23 taken and the separation plant 168 fed.

The separation plant 168 comprises a filter device 206 and a dewatering press 208 , The treated and oxidized substance mixture 23 becomes the filter device 206 , fed. The resulting almost solids-free wastewater 170 becomes the dilution water 4 and / or the wastewater treatment plant 148 fed. Accumulating solids and fibers 220 be in the dewatering press 208 , For example, a classifying press, further treated. The one in the dewatering press 208 resulting press juice 210 gets back into the filter device 206 guided. The resulting dehydrated raw compost 212 can via a switching and / or metering device 66 a rotting and / or drying 214 be subjected.

In the rotting 214 becomes the dehydrated raw compost 212 to a separable dry product 216 processed with a dry matter content of 75% to 85%. The rotting 214 closes a separator 218 in which the inert substances 222 get to the deposit and the restli materials 224 recycled material.

Those in the exhaust fumes 190 . 202 of the hydrolysis reactor 174 and the wet rottereactor 192 collected exhaust gases 188 . 200 become a mixing container 226 of the acidic air-washer 172 fed and freed from ammonia. With addition of hydrochloric or sulfuric acid 228 can be used as a commercial product ammonium chloride or sulfate 230 be won. It collects in the bottom area of the mixing container 226 a water-acid mixture 232 that's about a spraying device 234 with a circulation pump 236 the mixing container 226 removed and re-sprayed on the head, so that it with the exhaust gases 188 . 200 can respond flatly. Depending on the degree of treatment of the water-acid mixture 232 becomes a part in the circulation via a switching and / or metering device 66 as finished commercial product ammonium chloride or sulphate 230 taken. The resulting in this process entstickte exhaust air 238 can in a downstream cleaning stage 240 Odorless as purified process air 242 be delivered to the atmosphere.

11 shows a variant of a pulper, through which a quasi-continuous operation can be driven. In this embodiment, two or more pulp containers 6 connected in series, each with an in 10 Gas pump, not shown, is executed.

The mechanically processed input material 2 becomes the first pulp container 6a via the entrance lock 10 fed and by adding dilution water 4 adjusted to the predetermined dry matter content. The accumulating Stör- / Schwerstoffe 18 be over the arranged on the ground outlet lock 16 withdrawn and in the substance dissolving tank 6a accumulating, thoroughly mixed by the pneumatic agitator open-minded suspension 20 by pressing a slider 152 in the further substance dissolving container 6b initiated wherein the promotion preferably takes place without a pump by gravity. In this, by means of the pneumatic agitator, a further digestion, wherein the resulting suspension 20b then over a slider 152 one or more substance removal containers (not shown) or based 9 described treatment by means of Faserstoffabscheiders 98 , the scrubber 122 and the fermenter 138 is supplied. The in the liquor container 6b accumulating impurities / heavy materials 18b will be deducted again on the ground. The setting of the dry matter content TS in the substance dissolving tank 6b takes place either as a function of the TS content in the pulper 6a or it can also be in the fabric dissolving tank 6b be added directly dilution liquid, so that the TS content in each pulp container 6a . 6b , ... is individually adjustable.

In 12 is a basic construction of an alternative pulper 1.1 represented in the organic components of the input material supplied 2 , and / or the screen pass 78 the sieve 62 in the dilution water 4 be solved. Preferably, the pulper becomes 1.1 according to 12 for the treatment of coarse residual waste and the pulper 1 according to 1 used for the treatment of organic waste in monocharges. The grain size of the waste mixture supplied (after mechanical treatment) is preferably at least 80 mm. The mixture 8th is in the pulper 1.1 diluted to a dry matter content of about 1-15%. The pulper 1.1 has a pulp container 6 with a longitudinal shape substantially "lying" rectangular shape with the length L1 and a height h1. Preferably, the height-length ratio h1: L1 ≥ 1: 4 is satisfied.

The trash 278 and the dilution water 4 become the pulp container 6 each via an entrance lock 10 supplied in a left end portion as shown. In one as shown in the 12 right end portion of the fabric container 6 is a conical bottom 12 executed in a discharge opening 14 with an outlet lock 16 which overflows on the ground 12 settling interfering / heavy materials 18 can be deducted. Above the conical bottom 12 is another exit lock 16 educated about those in the pulper 1 digested organism-loaded suspension 20 deducted, according to the above 9 prepared and then as dilution water 4 via the entrance lock 10 is fed again.

In the interior of the substance removal container 6 is a stirrer 270 with a motor driven rotor 272 arranged substantially over the entire length L1 of the substance removal container 6 extends and on which a variety of rotor blades 276a , b, c, 278a , b, c are arranged. Preferably, an even number of rotor blades 276 . 278 selected. The exemplary embodiment shown, for example, six rotor blades 276 . 278 , but other numbers are conceivable.

The rotor blades 276 . 278 each have about 180 ° to each other offset blade pitch, so that the rotor blades 276a . 278a and 276b . 278b and 276c . 278c each have an opposite conveying direction. Thus, the mixture becomes 8th between the rotor blades 276a . 278a and 276b . 278b and 276c . 278c brought together, which in each case an abrasion-promoting swirling 280a . 280b . 280c training and the organic is in a solution. At the same time forms between the rotor blades 278a . 276b and 278b . 276c a counter-turbulence 282a . 282b through which the mixture is separated and thus also favors the abrasion and the transition of the organic in solution is supported. The interfering / heavy materials 18 sink in the mix 8th down and are eg via a screw conveyor 284 to the conical bottom 12 and thus to the outlet lock 16 promoted.

In part to the Stör- / Schwerstoffen 18 To completely remove adhering organics from these, a gas injection device is provided, via which preferably compressed air into the discharge opening 14 by means of a press-fit line 156 and a compressed air compressor 36 pulsed, ie discontinuous, or is blown continuously, causing the Stör- / Schwerstoffe 18 up to a certain distance h2 to the mixing level 286 rising up. The distance h2 can be selected variably by the amount and intensity of the gas injection. Preferably, the entire interior of the substance dissolving container 6 with the mixture 8th filled, being at one the bottom 12 opposite ceiling section a fireplace 288 is arranged, in which the mixture 8th rises. Above the mixing level 286 is in the fireplace 288 a gas exhaust room 240 formed by a suction line 38 with the compressed air compressor 36 is connected, so that the compressed air 52 the gas injection device can be driven in the circuit.

Furthermore, in the area of the discharge opening 14 the process water 82 the wastewater treatment plant 148 as well as the circulating water 108 , which is the processing circuit for the dilution water 4 is diverted into the substance dissolving container 6 be initiated, so that the Stör- / Schwerstoffe 18 the substance dissolving container 6 leave as purified or clear solids.

For setting an optimum process temperature in the substance dissolving tank 6 this can at least partially from a double jacket 46 be surrounded by a heating medium 142 to be led. In addition, an isolation 47 be provided, which is the substance dissolving container 6 and the double jacket 46 encloses.

The 13a Figure -d show exemplary cross-sectional shapes of the pulper 1.1 out 12 , Here is the dashed circle shown 290 for the circular path, the rotor blades 276 . 278 describe with their leaf tips.

That's the way it is 13a conceivable, the pulp container 6 with a circular cross section or according to 13b with two parallel longitudinal walls 292 . 294 to carry out, over a semicircular bottom wall 295 connected to each other. It is also possible to use the substance dissolving container 6 according to 13c as a polygon, in particular as a hexagon, with a bottom wall 295 a short transverse span has as an opposite ceiling wall 297 , In 13d is a pulp container 6 with a rectangular cross section with arched longitudinal walls 292 . 294 realized, wherein in the interior of the substance dissolving container 6 two parallel rotors 274 . 296 are arranged, the rotor blade tips each have a circular path 290 . 298 describe together an overlap area 302 form.

According to 14 can use several pulpers 1.1 be connected in series, the downstream substance dissolving container 6n with the in the upstream substance removal container 6a resulting suspension 22 is charged. The gas injection preferably takes place via a common compressed air compressor 36 , The discharged interfering / heavy materials 18 are preferably via a common conveyor 304 , For example, a screw conveyor, the washing device 80 and thus the further process steps according to 9 fed. Alternative to 9 can in the cleaning zone 106 the washing device 80 the circulating water 108 be initiated.

15 shows a preferred embodiment of a hydrolysis reactor 174 for waste mixtures with a maximum grain size of about 80 mm. The wet rot reactor 192 is essentially the same as the hydrolysis reactor for such grain sizes 174 constructed so that the following explanations also for this reactor 192 or for the wet rot 164 be valid.

The reactor 174 for the hydrolysis 162 has a stirrer inside 176 with adjustable capacity, preferably a paddle agitator. The stirrer 176 is of a double-walled draft tube 244 encompassed, the front side of the reactor bottom 246 and reactor head 248 is spaced and preferably completely immersed in the mixture. The stirrer 176 is controlled such that a circulating flow 250 results, wherein the substance mixture in the 15 from top to bottom through the guide tube 244 is promoted and outside the draft tube 244 an ascending loop-shaped flow 252 formed.

The guide tube 244 has an annular space between its inner and outer walls 166 that with an upper lead 184 and a lower return 204 a cooling unit, not shown, is connected. When controlling the cooling unit of the annulus 166 flows through a coolant, whereby overheating of the mixture can be prevented.

It is an oxygen supply 180 provided, which optionally over arms 254 . 256 . 258 near the bottom or in the area above and below the stirrer 176 into the substance mixture oxygen can blow. The poor 254 . 256 . 258 can have a variety of gas injection nozzles and are via valves 262 individually opened and closed. The one for the hydrolysis 162 oxygen required can be present both as liquid, industrial oxygen, ie> 95% O ₂ , as well as in an air separation plant as enriched oxygen, d. h> 95% O ₂ , be treated. In low-weight mixtures, it is also possible ambient air from the atmosphere in the reactor 174 to blow.

In the head area of the reactor 174 an exhaust gas chamber is formed 190 for collecting in the hydrolysis 162 resulting exhaust gases 188 , The exhaust room 190 is determined by the mixture of substances 186 limited. The exhaust gases 188 can over a line 262 in the reactor head 248 to the acidic air scrubber 172 flow out.

Via a head-side, length-adjustable axial extension 264 of the draft tube 244 Can the oxygen bubbles that are with the loop-like flow 252 move upwards through the stirrer 176 be sucked again, so that a nearly 100% utilization of the existing oxygen is realized.

Oxygen utilization can be via an O ₂ probe 266 in the pipe 262 by determining the injected oxygen and the setting of the extension 264 be regulated. However, it is also possible, the oxygen utilization via an axial displacement of the entire guide tube 244 and / or a change in the substance mixture level 186 to optimize.

Hereinafter, preferred conditions for optimized oxygen utilization are exemplified:
The guide tube height H1 corresponds to 8 to 10 times the guide tube diameter d1.

The effective diameter d2, ie the inner diameter of the reactor 174 , corresponds to 4 to 6 times the guide tube diameter d1.

The ground clearance H2 from the bottom of the reactor 246 to the guide tube 244 corresponds to 1 to 2 times the guide tube diameter d1.

The distance between the mixture mixture 186 and the draft tube 244 corresponds to 2 to 3 times the guide tube diameter d1.

The variable height adjustment H4 between the mixture mixture 186 and the draft tube 244 is 0.5 to 2 times the guide tube diameter d1.

The inflow velocity v1 of the circulating flow 250 moves between 0.1 m / s and 0.8 m / s.

Of the Guide tube diameter d1 is depending on mixture composition and the dry matter content between 0.5 m and 1.5 m.

According to 16 can also have several above-mentioned guide tubes 244 in the reactor 174 be provided. For example, three ducts, 244a . 244b . 244c standing in a triangle.

According to the 17 and 18 it is to optimize the hydrolysis 162 or the wet rot 164 conceivable, several reactor 174 respectively. 192 to connect in series. In each case, the processed substance 21 . 21a . 21b or the oxidized substance mixture 23 . 23a . 23b a renewed hydrolysis 162a . 162b or wet rot 164a . 164b undergo. The reactor 174 respectively. 192 however, they can also be operated in parallel.

In 19 a schematic of a second process scheme for waste treatment of waste with organic components is shown. The reference numerals are according to the first process scheme according to 9 so as to avoid a repetition, a detailed consideration of the common facilities and material flows is dispensed with.

At the beginning of waste treatment, the waste to be treated becomes 60 initially a sieve 62 fed, which is designed for example as a rotary screen. The trash 60 preferably has a dry matter content of 45-60%. The resulting sieve overflow 64 can either be disposed of directly or at least as a partial flow of a sighting system 68 for separating the sieve overflow 64 in Stör- / Schwerstoffe 70 as well as polluted light materials 72 are fed, which can then be subsequently removed.

The organically rich sieve run 78 can at least as a partial stream of a mixing plant 74 be supplied in which he with a partial stream of a denitrified dilution water 4 diluted and by means of a mixer 268 to a suspension 76 is processed with a solids content of 5-15%. Furthermore, via a mechanical device of the mixing plant 74 impurities 160 , such as straps, ropes and cables, from the suspension 76 separated and ejected. The thus processed and the coarse impurities 160 liberated suspension 76 becomes the entry lock 10 of the pulper 1 respectively. 1.1 fed.

The in the pulper 1 . 1.1 contained interfering / heavy materials 18 be via the exit lock 16 the substance dissolving container 6 deducted and a washing device 80 fed, in which the Stör- / Schwerstoffe 18 adhering organic components in a cleaning zone 106 by means of supplied operating water 82 getting cleaned. The thus cleaned Stör- / Schwerstoffe 84 can then be a ferrous metal separator 86 and a non-ferrous metal separator 88 be fed so that the flow of the Stör- / Schwerstoffe 84 into an iron-containing fraction 90 and a non-ferrous metal component 92 and other substances 94 is split.

The over the exit lock 16 from the pulper 1 . 1.1 withdrawn digested suspension 20 becomes a hydrolysis 162 respectively. 162.1 undergo. Preferably, in the hydrolysis 162 . 162.1 set a dry matter content of 5-15%. The nitrogen-laden exhaust gases 188 the hydrolysis 162 . 162.1 become an acidic air scrubber for denitrification 172 and then after passing through a cleaning step 240 for the removal of de-nitrogenised exhaust gases from odorous substances as purified process air 240 delivered to the atmosphere.

The in the hydrolysis 162 . 162.1 prepared suspension 21 becomes a mass separation plant 300 for separating the organically highly loaded liquid 132 from the substantially organics-free solids 116 the suspension 21 fed. Almost as a by-product falls in this substance separation 300 cleaned fine sand 130 which can be taken from the process.

The liquid 132 is in a cache 134 stored and depending on the need for biogas production a fermenter 138 and / or as circulating water, a heat exchanger 140 supplied in which it by means of a heating medium 142 is heated to process temperature and then as dilution water 4 for the pulper 1 . 1.1 can be used.

The solids 116 preferably have a dry matter content of 5% and become a wet rot 164 respectively. 164.1 - Also referred to as wet oxidation - subjected. The wet oxidation 164 . 164.1 and at the concomitant denitrification resulting exhaust gases 200 are heavily loaded with nitrogen and are used to denitrify the acidic air scrubber 172 fed.

That in wet oxidation 164 . 164.1 oxidized substance mixture 23 becomes a separation plant 168 fed, from the one raw compost 212 excreted and on the other solids-free wastewater 170 as dilution water 4 the pulper 1 . 1.1 supplied and / or in a wastewater treatment plant 148 for removal as wastewater 150 is cleaned in the sewer. A partial stream of purified wastewater 150 is called process water 82 in the cleaning zone 106 the washing device 80 as well as to the material separation plant 300 guided. Likewise, a partial stream of purified wastewater 150 as process water 82 with the partial flow of circulating water 132 after the fermenter 138 mixed.

In the fermenter is under the influence of methane bacteria from the organically highly polluted circulating water 132 biogas 144 won. In this case, discharged wastewater falls 146 on, as deflated foul water 159 wet oxidation 164 . 164.1 can be supplied. The one for wet oxidation 164 . 164.1 Unused stream of wastewater 146 can as excess water 174 the wastewater treatment plant 148 be supplied.

Furthermore, in 19 shown that the dehydrated solids 116 at least as a partial stream after passing through a drying 311 a compacting plant 312 for producing a fuel for thermal / material utilization in a gasification or incineration plant 317 can be supplied, one in a liquefying 313 and / or a treatment and metering device 314 processed binder 315 for use as an adhesive of the compacting plant 312 is supplied.

The following is a more detailed description of the hydrolysis 162.1 , the wet oxidation 164.1 , the substance separation plant 300 , the separation plant 168 as well as the compaction.

In the hydrolysis 162.1 becomes like in the hydrolysis 162 with the reactor after 15 the disrupted suspension 20 roughly cleaned and organic matter so digested that it fermentation in the fermenter 138 is available. Furthermore, the non-anaerobically degradable substances are separated from adhesive grain and dirt.

According to 20 takes place for mixtures with a minimum particle size of about 80 mm, the hydrolysis 162.1 essentially in a reactor 174 , near the ground 246 a blowing device 178 for injecting oxygen, thereby resulting in a rising in the mixture helical flow 252 is formed, by means of which the mixture is mixed. Accordingly, no mechanical agitator is necessary. The injection can be pulsed or continuous.

The feed of the reactor 174 with the suspension 20 from the pulper 1 . 1.11 and the removal of the hydrolyzed suspension 21 takes place in each case in a middle reactor section.

The blowing device 178 includes at least one lance or an arm 254 with a plurality of nozzles for injecting the oxygen into the mixture of substances with an oxygen supply 180 communicates. Preferably, pure oxygen is injected through the nozzles.

The injected oxygen and the hydrolysis 162.1 accumulating exhaust gases 188 collect above a mixture of substances 186 in an exhaust room 190 , As in the hydrolysis 162 a part of the oxygen is CO ₂ -athalated, ie rendered inert, is for optimum regulation of the oxygen supply 180 in the reactor head 248 an O ₂ measuring probe 266 intended.

To enhance the mixing of the mixture in the hydrolysis reactor 174 can at least a partial flow of the exhaust gas 188 via a suction line 38 , a compressed air compressor 36 , a press-fit line 136 as well as an arm 306 , which is provided with a plurality of nozzles and as shown in the 20 above the lance 254 the blowing device 178 is arranged to be impulsively or continuously injected into the mixture. The injected exhaust gases 188 also form an ascending helical flow 308 out, dealing with the flow 252 of the injected oxygen to a total flow 310 superimposed.

The exhaust gases not injected into the substance mixture 188 be like already under 19 described the acidic air scrubber 172 fed to denitrification.

Preferably, the dry matter content of the mixture is 5-15% and the temperature of the mixture in the reactor 174 70 ° C. This temperature is sufficient to dissolve fat or fat compounds. To keep the 70 ° C constant, is an insulation 47 provided by the cooling liquid of a refrigeration unit 182 is flowed through.

In the wet rot or wet oxidation 164.1 becomes like the wet rotten 164 with the wet rottereactor according to 15 The non-anaerobically degradable organics respire and the nitrogen is expelled as ammonia. In the oxidation 164.1 By fumigation the circulation water 132 . 133 . 4 entickickt and thus prevents a concentration of ammonium, which is the biology in the fermenter 138 disturbs and inhibits the gas production and degradation performance.

The wet oxidation 164.1 takes place for mixtures with a minimum particle size of about 80 mm according to 21 essentially in a reactor 192 who is the reactor 174 the hydrolysis 162.1 equivalent. This is also the case of this reactor 192 a ground-level pulse-like and discontinuous operated blowing device 178 for blowing in oxygen and for mixing the substance mixture in the reactor 192 on. For controlling the oxygen supply 180 is a prescribed O ₂ measuring probe 266 intended.

Likewise, those in the wet oxidation 164.1 resulting exhaust gases 200 be injected by means of a return back into the mixture at least as a partial stream implusively or discontinuously. The non-recirculated exhaust gases 200 be according to 19 the acidic air mixer 172 fed to denitrification.

Furthermore, there is an isolation 74 with a refrigeration unit 182 provided for setting a constant temperature of the mixture.

Furthermore, the feeding takes place in the substance separation 200 dehydrated solids 116 as well as the sewage water 159 of the fermenter 138 and the removal of the oxidized substance mixture 23 like the material flows 20 . 21 in the hydrolysis 162.1 in a middle reactor section. Preferably, in the reactor 192 set a dry matter content of 5-15%. The supplied sewage water 159 mainly serves as dilution water.

The main difference between the hydrolysis reactor 174 and the wet oxidation reactor 192 is that in wet oxidation 164.1 more oxygen is pressed into the mixture in order to convert the substances that have not yet gone into solution in such as well as to de-embroider the mixture This has the advantage that a Nachrottung 214 as in the process scheme 9 and 10 can be omitted, which, among other things, significant cost reductions are possible.

In addition to the respiration of non-anaerobic degradable organics and the expulsion of nitrogen as ammonia can in the wet oxidation 164 . 164.1 also depending on the type of control, a sanitation of the substance mixture in the reactor 192 respectively. Not only the solids in the mixture can be used 116 but also the wastewater mixed with and without solids 146 of the fermenter 138 be sanitized. Likewise, wastewater from composting plants can be treated with the help of wet oxidation 164 . 164.1 be sanitized.

By sanitizing in wet oxidation 164 . 164.1 the possibility is given, both hygienized solids (compost) and a mixture of solids and process waters or wastewater or pure process water or speci to use all wastewater directly on an agricultural basis.

Preferably, the sanitation is carried out in the wet oxidation 164 . 164.1 at the beginning of wet oxidation 164 . 164.1 because the prevailing high temperatures also cause an improvement in the microbial availability of the organic substances. However, it is also conceivable to sanitize at the end of wet oxidation 164 . 164.1 perform.

The Sanitation times are from the prevailing temperatures dependent, so that different sanitation times must be maintained depending on the temperature. For example, one required by the German Biowaste Ordinance Hygienizing performance at 70 ° C over a Period of one hour can be achieved. At lower temperatures must the Residence time can be extended accordingly.

The Hygienisation is especially relevant for all biomass feedstocks, which are to be supplied to an agricultural use. These include in particular Organic and green waste, waste from agriculture and energy crops, kitchen and canteen waste, sewage sludge and special process and wastewater. Europe can This biomass products are counted from the total waste.

22 shows a schematic structure of the mass separation plant 300 , The in the hydrolysis 162 . 162.1 prepared suspension 21 is shared with the polluted service water 96 from the washing device 80 a pulp separator 98 fed, which is exemplified as a rotary screen. In addition, this can be done in the wastewater treatment plant 148 gained process water 82 the pulp separator 98 be supplied as a dilution. In the pulp separator 98 become fiber and floating matter 100 from organically containing water 102 separated.

The fiber and floating matter 100 be in a Feststoffsieb- and washer 104 by adding a partial flow of the process water 82 in a cleaning zone 106 cleaned. This cleaning process can be assisted by the fact that through the cleaning zone 106 additional circulating water 108 which is the circulation of the dilution water 4 in front of the heat exchanger 140 is branched off. In the cleaning zone 106 become the organic components of fiber and floating matter 100 detached from this. If a very intensive cleaning is required, the cleaning zone becomes 106 in addition, the process water 82 fed. For less intensive cleanings, the proportion of circulating water 108 be enlarged.

The cleaned off and over a solids outlet 110 the car wash 104 stripped solid and fibrous materials 112 be in a dewatering press 114 drained and the dehydrated solids 116 become the wet oxidation 164 . 164.1 undergo.

That in the dewatering press 114 accumulating, laden with organic water 118 is combined with that from the cleaning zone 106 effluent laden with organic wash water 120 mixed a sand scrubber 122 fed. Likewise, the organics-containing water 102 the sand scrubber 122 be supplied. In the sand scrubber 122 becomes the fine sand portion 124 by the action of a stirrer 126 separated and the at the fine sand portion 124 adhering organic components by adding the process water 82 replaced. The so-cleaned fine sand 124 then becomes a fine sand washing facility 128 supplied, the basic structure of the washing device 80 respectively. 104 according to 19 equivalent. The cleaned fine sand 130 can then be recycled for use in civil engineering and road construction.

The liquid which accumulates during the sand-washing and which is heavily loaded with organic matter 132 is like already under 19 described in the cache 134 cached and a fermenter 138 supplied and / or as circulating water 132 used.

According to 23 is at the separation plant 168 the oxidized substance mixture 23 wet oxidation 164 . 164.1 together with the process water 82 and mixed water 121 from a Feststoffsieb- and washer 104 and a dewatering press 114 a pulp separator 98 for recovering the solids-free wastewater 170 supplied, which as under 19 described the wastewater treatment plant 148 and / or as a dilution water 4 for the pulper 1 . 1.1 is used.

The pulp separator 98 is exemplified as a rotary screen, wherein the separated fiber and floating matter 100 the solid sieve and washer 104 be fed in their cleaning zone 106 the adhering organic components by means of the process water 82 and / or the diverted circulating water 108 be separated. The after the cleaning zone 106 dehydrated and purified solids 112 be via a solids outlet 110 withdrawn and in the dewatering press 114 to that already in the 19 called raw compost 212 compacted.

That in the dewatering press 114 squeezed with organics highly contaminated water 118 gets along with the wash water 120 the solid sieve and washer 104 as the mixed water 121 the pulp separator 98 fed.

According to 24 are used in the compaction to produce fuels for the gasification or incineration plant 317 out 19 the dehydrated solids 116 a drying 311 subjected to drying 311 becomes an emerging dry matter mixture 311.1 with a water content of preferably 15% to 25% of a compacting plant 312 , in particular a briquetting or pelletizer with integrated mixer or extruder or a bar press fed. The compaction is preferably carried out under low pressure, wherein the dry material mixture 311.1 a binder is mixed as an adhesive to the formed under low pressure fittings 312.1 such as briquettes and pellets until annealed 317 together. The compaction under low pressure and with the addition of the binder 315 has the advantage that the energy required to produce the fittings 317 reduced and the wear of plant components of Kompaktieranlage 312 such as the mixer is reduced. Thus, the compaction invention requires 312 with the binder 315 about 20 kW of electricity and causes wear costs of about 1EUR / Mg to 6EUR / Mg, whereas in a conventional compaction for the production of 1Mg pieces from waste 100 kW electric current and wear costs are incurred by 15EUR, resulting in total costs / Mg of about EUR50.

The adhesive 315 is primarily from the screen overflow produced 72 obtained, which consists of about 80% of plastics and in a liquefaction device 313 by extruding or thermal / chemical action in a viscous injection mass 313.1 is transformed.

In the event that no or too little plastic material 72 is available, can also be supplied with binder 316 such as lime milk or starch via the treatment and metering device 314 as an organic or inorganic binder 314.1 the compacting system 312 be mixed. In this case, of course, the organic starch such as potato starch given priority, because this is burned without residue in contrast to the cheaper milk of lime and electrical and / or thermal energy 317.1 is released. The lime milk can be used as slag or minerals 317.2 be disposed of.

Depending on the quality requirements of the fuel to be supplied to the gasification or incineration plant 317 can be completely or partially the Kompaktieranlage 312 be bypassed and the material flows 72 and 311.1 directly to the thermal utilization 317 be supplied.

Disclosed are a method of treating waste with organic matter, in the case of uniform method steps depending on the grain size of the waste mixture different pulpers to release the organic components in a dilution liquid and different reactors to carry out a hydrolysis and / or a wet rot and suitable pulper and reactors. Furthermore, a suitable waste treatment plant disclosed.

1

pulper

1.1

pulper

2

input material

4

dilution water

6

Material solubilizing tank

8th

mixture

10

inlet lock

12

ground

14

Ausschleuseöffnung

16

outlet lock

18

Error / heavies

20

open minded suspension

21

edited Suspension (hydrolysis)

21a

edited Suspension (hydrolysis)

21b

edited Suspension (hydrolysis)

22

head

23

oxidized Mixture of substances (wet rot)

23a

oxidized Mixture (wet fermentation)

23b

oxidized Mixture of substances (wet rot)

24

Gas flow pump

26

inner tube

27

nozzle plate

28

Gaseinpressdüse

30

Compressed air line

32

control valve

34

Air collectors

36

Pneumatic compressor

38

suction

40

transport air

42

Gas discharge chamber

44

flapper

46

jacketed

47

isolation

48

to above directed suspension flow

50

Pressure bubble

52

compressed air

54

level

56

annulus

58

baffle

60

waste

62

Screening Plant

64

screen oversize

66

Umschalteinrichtung- and / or metering device

68

Sichtungsanlage

70

Heavy / contaminants

72

light materials

74

batching plant

76

suspension

78

flow-through

80

wash

82

Process water

84

cleaned heavies

86

ferrous metal separator

88

Nichteisenmetallabscheider

90

Ferrous metals

92

Non-ferrous metal content

94

other matter

96

polluted Process water

98

fibrous material separator

100

Fiber / floating matter

102

organikhaltiges water

104

solids screening and car wash

106

cleaning zone

108

circulating water

110

Solids discharge

112

abgereinigter Solid / pulp

114

dewatering press

116

dehydrated solids

118

water with dissolved Organik

120

wash water

121

mixed water

122

sand washer

123

sand discharge

124

prepurified fine sand

126

agitator

128

Fine sand washing means

130

purified fine sand

132

organic heavily loaded circulating water

133

suspension mixture

134

cache

136

pump

138

fermenter

140

heat exchangers

142

heating medium

144

biogas

146

entfrachtetes sewage

147

Excess water

148

wastewater treatment plant

150

purified sewage

152

pusher

154

bypass line

156

injecting line

158

mixed water

159

Faulwasser

160

impurities

162

hydrolysis or acidification stage

162a

hydrolysis or acidification stage

162b

hydrolysis or acidification stage

164

wet fermentation

164a

wet fermentation

164b

wet fermentation

166

annulus

168

separation plant

170

solid-free sewage

172

sour Luftwäscher

174

reactor

176

stirrer

178

insufflation

180

oxygenation

182

refrigeration unit

184

leader

186

Material mixture level

188

exhaust

190

exhaust gas chamber

192

reactor

194

stirrer

196

insufflation

198

Material mixture level

200

exhaust

202

exhaust gas chamber

204

returns

206

filtering device

208

dewatering press

210

press juice

212

raw compost

214

post treatment

216

dry product

218

separator

220

Firmly- and fibrous materials

222

inert materials

224

materials

226

mixing tank

228

Salt- or sulfuric acid

230

Ammonium Clorid or sulphate

232

Water-acid mixture

234

spraying

236

circulating pump

238

exhaust

240

cleaning stage

242

process air

244

guide tube

244a

guide tube

244b

guide tube

244c

guide tube

246

reactor bottom

248

reactor head

250

circulation flow

252

flow

254

poor

256

poor

258

poor

260

Valve

262

management

264

renewal

266

O ₂ probe

268

mixer

270

agitator

272

rotor

276a

rotor blade

276b

rotor blade

276c

rotor blade

278a

rotor blade

278b

rotor blade

278c

rotor blade

280a

Verwirbeluung

280b

Verwirbeluung

280c

Verwirbeluung

282a

Gegenverwirbelung

282b

Gegenverwirbelung

282c

Gegenverwirbelung

284

screw conveyor

286

mix mirror

288

fireplace

290

orbit

292

longitudinal wall

294

longitudinal wall

295

bottom wall

296

rotor

297

top wall

298

orbit

300

Material separation plant

302

overlapping area

304

promoter

306

poor

308

flow

310

total flow

311

drying

311.1

Dry mixture

312

compacting

312.1

Fitting (briquettes, pellets)

313

liquefier

313.1

Injection mass

314

reprocessing and metering device

314.1

binder

315

own zeugtes binder

316

been handed down binder

317

incineration gasification plant

317.1

electrical and thermal energy

317.2

Minerals / slag

Claims (62)

Process for the treatment of waste with organic components comprising the steps of: mechanical treatment of the waste into a waste mixture, dissolving organic constituents in a pulper 1 . 1.1 ), • hydrolysis ( 162 . 162.1 ) from the pulper ( 1 . 1.1 ) withdrawn with organik loaded suspension ( 20 ) in a reactor ( 174 ) and • fermentation of the hydrolyzed suspension ( 21 ) in a fermentation stage ( 138 ), where • the process water obtained in the hydrolysis or fermentation is circulated water ( 4 ) is guided in a circle and • selecting the pulper ( 1 . 1.1 ) and the reactor ( 174 ) for the hydrolysis ( 162 . 162.1 ) depending on the grain size of the mechanically treated waste mixture. Process according to claim 1, wherein with a grain size of about 80 mm the pulper ( 1 . 1.1 ) and the reactor ( 162 . 162.1 ) is changed. Process according to claim 1 or 2, wherein the hydrolysis ( 162 . 162.1 ) at least indirectly a wet rot or wet oxidation ( 164 . 164.1 ) is connected downstream. Method according to one of claims 1 to 3, wherein separating steps for separating impurities, heavy materials, fibrous materials, etc. from the fermentation stage ( 138 ) feeding biological suspension ( 132 ) are provided. A pulper for use in the method according to one of claims 1 to 4 for dissolving organic constituents of waste in a dilution liquid having a certain maximum grain size of, for example, 80 mm, with a pulper ( 6 ), in which a mixing device for mixing the waste and the dilution water is arranged, wherein via a suspension outlet ( 16 ) the organically loaded suspension ( 20 ), characterized in that the mixing device at least one gas injection nozzle ( 28 ), via which a gas, preferably air, the suspension ( 8th ) are pressurized such that organic components in the dilution liquid go into solution or are distributed by the shear forces applied via the gas. Pulper according to claim 5, wherein the gas injection nozzle ( 28 ) Part of a gas flow pump ( 24 ), over which the suspension ( 8th ) within the substance removal container ( 6 ) is pumped periodically or continuously. pulper according to claim 6, wherein the pulse spacing is more than 3 seconds, preferably between 5 and 10 seconds. Pulper according to claim 6 or 7, wherein the gas flow pump ( 24 ) an inner tube ( 26 ) has, at its lower inlet opening, one of the suspension ( 8th ) or flow-through nozzle plate ( 27 ) with a plurality of gas injection nozzles ( 28 ) is arranged and whose upper end portion has an outlet opening for in the inner tube ( 26 ) has transported suspension. Pulper according to claim 8, wherein at a distance from the outlet opening of the inner tube ( 26 ) a baffle plate ( 44 ) is arranged. Pulper according to claim 9, wherein the baffle plate ( 44 ) at least in sections a gas exhaust space ( 42 ) limited. Pulper according to one of the claims 6 to 10, wherein several gas flow pumps ( 24a . 24b . 24c ) in the substance dissolving container ( 6 ) are arranged. Pulper according to one of the claims 8 to 11, with the inner tube ( 26 ) is double-walled and the gas injection nozzles ( 28 ) are arranged in the inner cylinder space or in the annular space and the respective other space of a heating medium ( 142 ) is flowed through. Pulper according to one of the claims 5 to 12, wherein the gas is circulated and from a pump ( 36 ) from the substance dissolving container ( 6 sucked and / or pressurized from a memory ( 34 ) to the gas injection nozzles ( 28 ) is returned. Pulper according to one of claims 8 to 13, wherein in the inner tube ( 26 ) and from the outer peripheral wall of the substance removal container ( 6 ) limited annulus ( 56 ) Baffles ( 58 ) are arranged for flow guidance. Pulper according to one of the claims 5 to 14, wherein a plurality of pulp containers ( 6a . 6b , ... 6n ) are connected in series and the suspension from the first pulp container ( 6a ) into the downstream substance solution containers ( 6b , ... 6n ) flows. Pulper according to one of the claims 5 to 15, with a discharge opening ( 14 ) for interfering / heavy materials ( 18 ). Pulper according to one of the claims 5 to 16, wherein in the discharge opening ( 14 ) a connection for gas injection and mixing of the settled Stör- / Schwerstoffe ( 18 ) is provided. Pulper according to one of the claims 5 to 17, wherein the diluting liquid ( 4 ) has cycled. A pulper for use in the process according to one of claims 1 to 4 for dissolving organic constituents and waste in a dilution liquid having a certain minimum particle size of, for example, 80 mm, with a pulper ( 6 ), in which at least one agitator ( 270 ) is arranged for mixing the waste and the dilution water to a suspension, wherein via an outlet lock ( 16 ) the organically loaded suspension ( 20 ), characterized in that the agitator ( 270 ) a plurality of adjacent stirring elements ( 276 . 278 ), each having an opposite conveying direction. Pulper according to claim 19, wherein the stirring elements are used as rotor blades ( 276 . 278 ) are formed on a common rotor ( 272 ) are arranged and adjacent rotor blades ( 276 . 278 ) have an offset by about 180 ° blade pitch angle. Pulper according to claim 20, wherein the rotor blades ( 276 . 278 ) from an entrance opening ( 10 ) to an outlet lock ( 16 ) for interfering / heavy materials ( 18 ) evenly on the rotor ( 272 ) are arranged. A pulper according to claim 20 or 21, wherein an even number of rotor blades ( 276 . 278 ) is selected. Pulper according to one of the claims 20 to 22, wherein two rotors ( 274 . 296 ) provided with their rotor blades ( 276 . 278 ) an overlap area ( 302 ) form. Pulper according to one of the claims 19 to 23, wherein in the region of a discharge opening ( 14 ) for the interfering / heavy materials ( 18 ) a gas, preferably compressed air, is inflatable. A pulper according to claim 24, wherein the gas is circulated and pumped by a pump ( 36 ) from the substance dissolving container ( 6 ) is sucked in and returned to this. Pulper according to one of the claims 19 to 25, wherein a plurality of pulp containers ( 6a , ... 6n ) are connected in series and the suspension ( 20 ) from the first pulper ( 6a ) into the downstream substance solution containers ( 6n ) flows. Pulper according to one of the claims 19 to 26, wherein the pulper ( 6 ) in longitudinal section has a substantially rectangular shape whose height-length ratio of the equation h1: L1 ≥ 1: 4 corresponds. Reactor for use in the method according to one of claims 1 to 4 for processing a feed mixture having a certain maximum grain size of, for example, 80 mm, with an inlet and outlet and with a mechanical mixer ( 176 ) for mixing the substance mixture, characterized in that the mixing plant ( 176 ) from a guide tube ( 244 ) is encompassed, wherein when controlling the mixer ( 176 ) the mixture of substances from a reactor head side to a reactor bottom side through the guide tube ( 244 ) is sucked and outside the guide tube ( 244 ) an ascending loop-like flow ( 252 ) trains. Reactor according to claim 28, wherein the guide tube ( 244 ) an axial extension ( 264 ) to change its length or height. A reactor according to claim 28 or 29, wherein an oxygen supply ( 180 ) is provided for blowing oxygen into the mixture of substances, wherein the injection either near the bottom and / or in the height range of the mixing plant ( 176 ) he follows. Reactor according to claim 30, wherein an O ₂ -probe is provided for regulating the amount of oxygen to be injected, via which the axial extension ( 264 ), the axial position of the guide tube ( 244 ) and / or a mixture of substances ( 186 ) is adjustable so that preferably an optimal, ie almost 100%, oxygen utilization takes place. Reactor according to one of the claims 28 to 31, wherein the inner tube ( 244 ) is provided double-walled for performing a cooling medium for cooling the mixture. Reactor according to one of the claims 28 to 32, wherein three guide tubes ( 244a . 244b . 244c ) in the reactor ( 174 ) are arranged. A reactor according to any one of claims 28 to 33, wherein the reactor is hydrolysed ( 162 ) and / or in a wet rot ( 164 ) can be used. Reactor according to one of the claims 28 to 34, wherein the reactor preferably has the following geometries individually or in combination, - the guide tube height H1 corresponds to 8 to 10 times the guide tube diameter d1, - the effective diameter d2, ie the inner diameter of the reactor 174 , corresponds to 4 to 6 times the guide tube diameter d1, - the ground clearance H2 from the reactor bottom 246 to the guide tube 244 corresponds to 1 to 2 times the guide tube diameter d1, - the distance between the mixture mixture level 186 and the draft tube 244 corresponds to 2 to 3 times the guide tube diameter d1, - the variable height adjustment H4 between the mixture mixture level 186 and the draft tube 244 is 0.5 to 2 times the guide tube diameter d1, - the Aufströmgeschwindigkeit v1 of the circulating flow 250 ranges between 0.1 m / s and 0.8 m / s, - the guide tube diameter d1 is between 0.5 m and 1.5 m, depending on the substance mixture composition and the dry substance content. Reactor for use in the method according to one of claims 1 to 4 for processing a supplied mixture with a certain minimum grain size of for example 80 mm, with an inlet and outlet and with a mixing device for mixing the mixture, characterized in that the mixing device of a blowing device ( 178 ) is formed for the injection of gas, preferably oxygen. A reactor according to claim 36, wherein a plurality of gas injection nozzles near the bottom of the reactor ( 174 . 192 ) is arranged. A reactor according to claim 36 or 37, wherein the gas is recirculated and from a pump ( 36 ) from the substance dissolving container ( 6 ) is sucked in and returned to this. Reactor according to one of the claims 36, 37 or 38, wherein a gas measuring probe ( 266 ) are provided for regulating the amount of oxygen to be injected. Reactor according to one of claims 36 to 39, wherein in the reactor ( 174 . 192 ) exhaust gases ( 188 . 200 ) via a blower ( 36 ) can be pressed into the substance mixture, preferably near the bottom. Waste treatment plant for use in the process according to one of claims 1 to 4 with a pulper according to one of the preceding claims, in which organic components of the waste pass into solution, with a separation stage for separating pulps from that from the pulper ( 1 ) withdrawn organically-containing digested suspension ( 20 ). Waste treatment plant according to claim 41 with a solids preparation ( 80 . 86 . 88 ) for separating and washing the from the pulper ( 6 ) withdrawn solids ( 18 ). Waste treatment plant according to claim 41 or 42, wherein the separation stage comprises a pulp separator ( 98 ) for the separation of fibrous materials, floating matter or the like and a washing plant ( 104 ) for these substances ( 100 ) and a dewatering press ( 114 ) Has. Waste treatment plant according to claim 41, 42 or 43, with a sand scrubber ( 142 ) for separating and washing fine sand containing in the loaded wastewater ( 130 ). Waste treatment plant according to one of the claims 41 to 44 with a fermenter ( 138 ) for reacting the organic constituents of the organically highly loaded water ( 132 ) in biogas. Waste treatment plant according to claim 45, having a wastewater treatment plant ( 148 ) for the purification of excess water obtained after the fermentation. Waste treatment plant according to one of the claims 41 to 46, wherein the material in the pulper ( 1 ) disrupted suspension ( 20 ) at least as part of a hydrolysis ( 162 . 162.1 ) goes through. Waste treatment plant according to claim 47, wherein in the hydrolysis ( 162 ) suspension ( 21 ) the pulp separator ( 98 ) goes through. Processing plant according to claim 47, wherein in the hydrolysis ( 162 . 162.1 ) prepared suspension ( 21 ) directly to the fermenter ( 138 ) is supplied. Waste treatment plant according to claim 49, wherein the fermenter ( 138 ) wastewater ( 146 ) a separation plant ( 98 . 104 . 114 ) and thereby separated solids-free digested ( 171 ) with the dilution water ( 4 ) is mixed. Waste treatment plant according to claim 50, wherein a partial flow of the solids-free pumice ( 171 ) with the dewatered solids ( 116 ) from the separation plant ( 98 . 104 . 114 ) and a wet rot ( 164 . 164.1 ) is supplied. Waste treatment plant according to claim 48, wherein at least a partial stream of the after the separation plant ( 98 . 104 . 114 ) obtained dehydrated solids ( 116 ) and admixed with a binder ( 315 . 316 ) in a preferably under low pressure operated Kompaktieranlage ( 312 ) to form pieces for a gasification or incineration plant ( 317 ) are compacted. A waste treatment plant according to claim 52, wherein the binder seals the fittings until annealed in the gasification or incineration plant ( 317 ) holds together gas stable and in the waste treatment own produced binder 315 made of separated plastics and / or supplied binders ( 316 ) be used. Waste treatment plant according to claim 48, wherein in the dewatering press ( 114 ) solids ( 116 ) at least as a partial flow a wet rot ( 164 . 164.1 ) for obtaining an oxidized substance mixture ( 23 ) run through. Waste treatment plant according to claim 54, wherein the wet rot ( 164 . 164.1 ) Mixed water ( 158 ), which, when mixing the circulating water ( 132 ) with the wastewater ( 146 ) of the fermenter ( 138 ) is created, can be fed. Waste treatment plant according to claim 55, wherein the oxidized substance mixture ( 23 ) of the wet rot ( 164 . 164.1 ) a separation plant ( 168 ) and that in the separation plant ( 168 ) produced wastewater the dilution water ( 4 ) and / or the wastewater treatment plant ( 148 ) can be fed. Waste treatment plant according to claim 56, wherein the separation plant ( 168 ) a solids separator ( 98 ), a Feststoffsieb- and washer ( 104 ) and a dewatering press ( 114 ) having. Waste treatment plant according to claim 57, wherein the in the separation plant ( 168 ) resulting raw compost ( 212 ) a rotting ( 212 ) passes through for drying and / or directly disposable. Waste treatment plant according to one of the claims 41 to 58, wherein in the hydrolysis ( 162 . 162.1 ) and / or the wet rot ( 164 . 164.1 ) a reactor ( 174 ) is used according to claims 1 to 40. Waste treatment plant according to claim 59, wherein several reactors ( 174 ) are connected in series and / or parallel to each other, so that a multi-part hydrolysis ( 162 . 162a . 162b ) and / or wet rot ( 164 . 164a . 164b ) he follows. Waste treatment plant according to claim 59 or 60, wherein the in the reactor ( 174 . 192 ) exhaust gases ( 188 . 200 ) an air scrubber ( 172 ) can be supplied for the liberation of ammonia. Waste treatment plant according to one of the claims 54 to 61, wherein at least the reactor ( 192 ) for the wet rot ( 164.1 ) is operable so that a sanitation as a mixture of substances takes place.