DE19909353A1 - Method and device for the preparation of a mixture of substances containing organic matter - Google Patents

Abstract

What is disclosed is a method for the preparation of a substance mixture containing structural components and organic matter and a device for carrying out this method. According to the invention, the mixture of substances is subjected to a pulse or periodically with a force, so that the formation of flow channels for a washout liquid or process air in a pile can be prevented.

Description

The invention relates to a method for processing of a material mixture containing structural components and organic matter cal according to the preamble of claim 1 and Device especially for performing this procedure rens.

Such a method is used for example treatment of residual waste. In DE 196 48 731 A1 describes a waste treatment process in which the remaining waste is processed in a percolator. By such percolation or extraction are indicated by a Extraction or detergent organic components organic substances and possibly water-soluble fatty acids washed out of the garbage. The backlog becomes from the Percolator removed and after a subsequent Drying supplied to a combustion or deposited.

It was shown that the organization African substances not to the extent necessary have the remaining waste removed.

The disadvantages of this known waste processing driving can be opened by the in WO 97/27158 A1 barte processes for the treatment of biological waste clear out. In this process, a new type of Perko used the waste in the reactor in Hori passes through the zonal direction (longitudinal direction) and the percola tion process a biogenic reaction by adding air oxygen (process air) is superimposed.  

By supplying process air, the cells of the Organic broken down and the released organic sub punched away by the washing liquid. For Avoiding channel formation within the waste and to The introduction of shear forces in the reactor is a stirring or Circulation unit provided by which the waste in vertical direction (parallel to the flow direction of the washout liquid and the process air) mixed and also in Transport direction is moved.

The disadvantage of this method is that for guidance and mixing the waste within the reactor considerable effort must be made by the Investi tion costs significantly affected. Such a complex one mechanical construction also harbors the risk of system outage if due to a fault in the transport system of the Reak tors in itself, so that a comparatively high effort for Maintenance of the reactor must be operated. Such out cases of the reactor due to the required maintenance or a disturbance in the reactor periphery can only by providing appropriate buffer spaces be caught in the waste during the stoppages time of the reactor can be temporarily stored.

In contrast, the invention is based on the object a process for the preparation of a structural part and Mixture of organic matter and a device to create, where with minimal device technology a sufficient breakdown of organic matter partly done.

This task is accomplished with regard to the procedure the features of claim 1 and in terms of Device by the features of claim 12 ge solves.  

By the measure, the structural parts and organic containing mixture of substances (e.g. residual waste) Reactor without substantial longitudinal and transverse mixing to let run and the channel formation through the Beaufschla gene of the mixture with approximately parallel or transverse to Directional forces can prevent the reactor much easier than the one described above State of the art are applied, since no agitator for Cross-mixing must be provided. The powers will preferably from the edge region of the reactor, for example via a suitably designed discharge device tion or by blown gas, preferably compressed air initiated. Especially when using compressed air the pile is also subjected to shear forces which reshaped the surface of the fill and material mixed particles are unraveled.

The reactor can act as a percolator and as a dryer be used without any modifications or Conversions are required.

When introducing the channel formation preventing The mixture of substances becomes forces via the discharge device preferably at least partially circulated so that due to the conveying elements causing shear forces be initiated.

The flow guide according to the invention allows the To design the reactor very compact, with all feed and discharge devices on the top and bottom of the reak tors can be arranged.

In a particularly preferred embodiment are the forces for changing channel formation and those for new surface formation and for tearing open the parts kel required shear forces on a compressed gas, preferred wise compressed air applied from the edge of the Reak  is blown into the pile (bed). The bed is partially expanded by the compressed air, so that a new surface is formed in the pile and the particles due to the entered shear forces be torn - the mass transfer area for the digestion of the mixture of substances through the atmospheric oxygen and through the Wash-out liquid is increased.

In a particularly preferred embodiment the compressed air and process air are drawn in through nozzles leads in the foot part and / or in the bottom part of the reactor are arranged.

According to the invention it is preferred if the substance mix the reactor substantially vertically (parallel to the Direction of gravity) or horizontally, so that the Mixture of substances approximately parallel or in cross flow to the process air is led.

In the case where the reactor is used as a percolator det, the washout liquid is preferably over a distributor in the top of the reactor.

The compressed air is at a pressure of more than 2 bar, preferably fed more than 4 bar during the process air is usually pressurized to 0.5 bar is.

The nozzles for introducing the process and / or pressure air can advantageously be controlled individually, so that a certain compressed air profile across the reactor cross cut is adjustable.

The use of compressed air to introduce shear forces and to prevent channel formation has the advantage that at the same time the atmospheric oxygen required for the aerobic process in the pile is supplied, so that the compressed air practically fulfills a dual function:

• 1. Supply of atmospheric oxygen for aerobic degradation and
• 2. Entering shear forces.

In a simpler embodiment, the Forces to prevent channel formation in the pile for example supplied by a discharge device which is arranged on the bottom part of the reactor. This discharge direction can be, for example, a scraper floor system a similar one that removes the mixture of layers in layers Be a conveyor. This variant has the other Advantage that by the feed movement of the discharge device tion supply and discharge openings in the bottom part of the reactor be kept clear so that the washing liquid escapes and compressed or process air enter the pile can. A can also be used as the discharge device Screw conveyor carpet, a walking floor, silo milling directions etc. are used. This discharge device gene can of course also in the above described embodiment used with compressed air become.

Since the mixture of substances preferably layers the reactor runs through formally, the residence time of the mixture of substances inside the reactor in a continuous process leadership can be determined very precisely, so that the pass times can be optimized with regard to biodegradation are. In the case of the solutions mentioned at the beginning, the longitudinal and transverse mixing by means of the agitator only an average dwell time value can be set.

The loaded process air or the loaded compressed air are fed to an exhaust gas purification system, in which organic Components separated and the purified air in the Process is returned.  

The energy balance of the plant can be further improved if the loaded detergent of a wastewater treatment plant supply is supplied. This can include a biogas plant in which the organic is converted into biogas. By coupling the energy of the released biogas the process according to the invention is largely self-sufficient in terms of energy shape.

In the prescribed procedure, the Or ganic-containing mixture of substances known as hydrolysis subjected to, by the interaction of the air and the Wash out the organic material through the aero be, thermophilic heating through the air loosened and turned on acidifies and transported away by the washing liquid becomes. That is, the organic components are broken down by setting a certain humidity and by closing guidance of clean air.

The processing of the mixture of substances is invented according to a drying of the residue before. This Drying can be done with minimal energy an aerobic, thermophilic heating of the residue in the reak goal. To do this, the mixture of substances can either be in the reac clean air to be applied, so that by the right resulting aerobic warming water vapor over the led air discharged and the residue is dried. The drying and hydrolysis in a single reactor sets however, a batch operation ahead, so this should only be considered for smaller systems. With large Outer plants have their own reactor (dryer) for aero ben, thermophilic heating of the residue from the Hy drolysis provided. Of course, these two can Reactors in a single container in n-fold order can be switched in sequence, so that several Hy can connect drolysis / drying processes one after the other nen.  

The energy balance of the plant can be further improved if the loaded detergent of a wastewater treatment plant supply is supplied. This can include a biogas plant in which the organic is converted into biogas. By coupling the energy of the released biogas make the process of the invention self-sufficient in terms of energy.

It is particularly advantageous if it is based on this prepared solid action after hydrolysis and / or aerobic drying a compacting is supplied. Here becomes the one with a certain particle diameter Solid in a predetermined geometric shape, at for example pellets or briquettes pressed. Through this com a further drainage of the processing takes place tendency mixture of substances, so that after the compaction body that is dry and no longer elutable is stable.

This body can be used as a substitute fuel, for example as an alternative to fossil fuels or in one Landfill to be deposited.

The main application of the method according to the invention should be in the treatment of waste; in principle However, the method can also be used with other materials Use organic ingredients.

Water is usually used as the detergent, that cycled in the method according to the invention becomes. The air for hydrolysis and thermophilic drying of the mixture of substances can be countercurrent to the mixture of substances or but can also be carried out in direct current.

Other advantageous developments of the invention are the subject of further subclaims. Hereinafter are preferred embodiments of the invention based on schematic calculations explained in more detail. Show it:  

Fig. 1 shows a section through a reactor in which a hydrolysis of an organic matter-containing substance mixture is carried out;

Figure 2 shows a reactor for carrying out an aerobic thermophilic drying.

Fig. 3 shows a plant in which several hydrolysis and drying reactors according to Figures 1 and 2 are connected one behind the other;

Fig. 4 shows a device, in a common receptacle a plurality of reactors for hydrolysis and / or drying are connected in series in the;

Fig. 5 is a plan view of the device of Fig. 4 and

FIGS. 6 and 7 show alternative embodiments of a reac tors.

Fig. 1 shows a process diagram for explaining the method according to the invention and the device for carrying out the method. Accordingly, the aerobic hydrolysis (aerobic biogenic reaction and percolation) takes place in a reactor 1 , to which the mixture of substances 2 to be processed is fed via a material input device 4 . The mixture of substances to be treated contains a high proportion of structural material and organic matter. Such mixtures of substances occur, for example, with household waste, organic waste, commercial waste, etc.

The reactor 1 is out as a closed container, so that the material flows described in more detail below via locks, valve devices etc. are supplied.

The actual reactor 1 is preferably a steel or concrete container, which is loaded with the mixture of materials (residual waste) from above in the exemplary embodiment shown.

A substantial proportion of the organic fraction of the mixture consists of short-chain compounds, which are mostly absorbed on a surface. If warm water flows around this surface, primarily insoluble compounds are hydrolyzed and washed out. The degree of hydrolysis depends on the time spent in reactor 1 . The odor-intensive components of the mixture of substances and the hydrolysis products are readily water-soluble and can be washed out. Percolation therefore leads to a reduction in organic matter and deodorization of the mixture of substances. Fine sand particles are also discharged with the wash-out liquid (process water). The reactor 1 is odor-tight and the exhaust air is deodorized in the fol lowing manner described in more detail below.

Process air is also used in percolation supplied by which the physico-chemical effect of Water extraction by increasing bacterial degradation is reinforced. The microorganisms start in the aerobic To excrete exoenzymes which are particulate poly Split other components into monomers and brine in solution gene.

During the percolation, about 10% of the inert fen (glass, ceramic, sand) released, which with the Wash liquid are discharged. The deposition takes place in a sand classifier, which is also a Rinsing allowed for sand washing.

In the embodiment shown in FIG. 1, the carrying device 4 is arranged on the upper end section of the reactor 1 as seen in the direction of gravity.

At least one discharge device 6 is formed in the lower region of the reactor 1 , via which the processed and biologically digested mixture of substances can be removed from the reactor 1 .

The reactor 1 also has below (representation according to FIG. 1) the discharge device 6 a collector 10 which is separated from a reaction chamber 12 via a sieve plate 8 . For the described in more detail below supporting device 6 is formed such that the mixture of materials lying on the perforated base 8 in layers discharged from the actuator Re and the openings of the sieve tray 8 are held throughout.

An air connection 14 and a washout liquid outlet 16 open into the collector 10 . In the head region of the reactor 1 , a further air connection 18 and a washout distributor 20 are arranged.

The washout liquid used for percolation or extraction of the organic constituents of the substance mixture (water) is fed into the reactor via the distributor 20 and drawn off via the outlet 16 . To simplify the flow guidance, the bottom 22 of the reac tor 1 drops towards the outlet 16 , so that the washout liquid collects in the region of the outlet 16 .

The lower air connection 14 in FIG. 1 is connected to an air delivery device 24 . Depending on the design of the air conveying device (fan, compressor) can be adjusted of the reactor 1, a flow 25 from the lower Luftan circuit 14 to the upper air outlet 18, or a flow 27 in the reverse direction from the upper air connection 18 for un direct air connection 14 in nerhalb. That is, according to the design of the air conveying device 24 , the mixture of substances taken up in the reactor 1 is flowed through with air in the illustration according to FIG. 1 from bottom to top or from top to bottom.

The wash-out liquid flow takes place in the direction of the force of gravity, ie from the distributor 20 arranged at the top in the reactor 1 to the outlet 16 .

The leaching liquid emerging from the reactor 1 is processed via a waste water treatment device 26 (anaerobic filter), which will be described in more detail below, and then recycled back to the distributor 20 .

The residue lying on the sieve tray 8 is drawn off as material discharge 28 via the discharge device 6 and either passed on for further processing as product 30 or returned to the entry device 4 as circulating material 32 . The distribution of the material discharge 28 into product 30 and / or circulating material 32 takes place via a suitable metering device 34 , which can be designed, for example, as a slide, flap, switch, etc.

That is, by suitably adjusting the dosing device 34 , part of the material discharge 28 can be returned as circulating material 32 to the reactor 1 , and used there for inoculating the mixture of substances and thus for accelerating the biological degradation.

Furthermore, by circulating the whole or part of the mixture of substances via the funding Shear forces introduced into the circulating material, so that surfaces of the mixture of substances newly formed and particles frayed become.

For a better understanding, the individual is now available described components of the device according to the invention explained in more detail.  

The incoming mixture of substances 2 was previously mechanically processed in a known manner so that it has a predetermined maximum particle size. This processed substance mixture 2 is fed via suitable conveying devices, for example conveyor belts 36, to the entry device 4 , via which the mixture of substances 2 is distributed over the reactor cross section. In the embodiment shown, the input device 4 has a cross conveyor 8 , via which the mixture of substances is distributed in the plane of the drawing and transversely to the plane of the drawing and the material discharge funnels 40 distributed over the cross section are fed to the reactor 1 .

By controlling the material discharge hopper 40 or the cross conveyor 38 , the mixture of substances 2 is introduced in layers into the reactor 1 , so that the 8 n layers 42 are arranged one above the other practically on the Siebbo.

The fill level H of the reactor 1 is selected so that the distributor 20 for the washout liquid is above the pile. The distributor 20 can, for example, have a multiplicity of spray heads 44 distributed over the reactor cross section, via which the washout liquid can be distributed uniformly over the top layer 42 .

The discharge device 6 is formed in the embodiment shown in FIG. 1 Darge as a horizontal conveyor, which is designed such that the respective lower, resting on the sieve bottom 8 mixture layer in Ho rizontalrichtung can be removed. In the reactor 1 shown , the discharge device 6 is designed as a push or scratch floor, as described, for example, in WO 95/20554 A1. Such moving floors are used for example in sewage sludge silos, composting plants etc. and are known from the prior art, so that only the essential components are described in the fol lowing.

Referring to FIG. 1 has the pusher plate in a plurality of horizontal (view according to Fig. 1) spaced conveyor wedges 46, which is arranged on a push rod 48. The push rod 48 can be moved back and forth parallel to the arrows 52 , 54 in FIG. 1 via a hydraulic cylinder 50 or via another drive device.

The front surface of the discharge wedge 46 facing the discharge opening is designed as a vertical surface 56 , while the rear surface is an inclined surface 58 . By corresponding control of the hydraulic cylinder 50 , the push rod 48 is periodically moved back and forth, with the movement of the push rod 48 in the direction of arrow 52 (to the left in FIG. 1) the substance mixture of the bottom layer slides along the inclined surface 58 and behind in the room the relevant wedge 46 comes to rest. In the subsequent return movement of the push rod 48 in the direction of arrow 54 , this material is carried along by the vertical surface 56 and conveyed to the right to the adjacent conveyor wedge 46 or to the discharge opening. That is, the height of the conveyor wedges 46 determines the layer height of the discharged mixture. In order to keep the extraction conditions in the reactor 1 constant, the layer thickness of the material discharge corresponds approximately to the layer thickness of the material feed, so that the filling height H remains essentially constant.

As already mentioned at the beginning, part of the material discharge 28 can be returned as a vaccine (circulating material 32 ) to the conveying device 36 or directly to the entry device 4 . In principle, it is also possible to run the entire material discharge 28 as circulating material 32 , so that the substance mixture passes through the reactor 1 several times and is only discharged as product 30 after, for example, 4 passes.

The sieve tray 8 arranged below the discharge device 6 has a mesh size Z which is selected as a function of the composition and particle size of the mixture of substances to be processed. The construction of the push rod 48 and the conveyor wedges 46 is chosen so that the sieve plate 8 is cleaned by the reciprocating movement of the Kratzbo dens, so that clogging of the meshes can be prevented.

The layered material discharge causes the mixture of substances to move in layers in the vertical direction from top to bottom ( FIG. 1) through the reactor 1 .

As already mentioned above, the Luftförderein device 24 can be designed as a blower or compressor, so that different air flow directions in the actuator 1 can be set. In both cases, the entry and exit areas of the reactor 1 are chosen so that the air flows through the layered mixture distributed over the entire reactor cross section. This air flow is indicated in the illustration in FIG. 1 with dashed lines.

The wash-out liquid flows through the layered substance mixture along the solid arrows from top to bottom and enters through the sieve bottom 8 with organic loading in the collector 10 . The loaded wash liquid speed 60 is withdrawn via the outlet 16 and the waste water treatment device 26 supplied. This has an impurity separator 62 in which impurities 64 , such as sand, stones, floating materials, suspended matter, etc., are separated. Such contaminant separators can have, for example, a settling tank and a skimmer for separating the said contaminants 64 .

The washout liquid which is freed from the contaminants and contains colloidal organic compounds in the aqueous phase is then fed to an anaerobic fermenter 66 , for example a biogas or digestion plant. In this anaerobic wastewater treatment methane and carbon dioxide and possibly small amounts of hydrogen sulfide are formed as metabolic end products. This biogas obtained as a degradation product can be converted into electricity and heat in suitable CHP plants. Part of the energy obtained from the biogas is returned to the process according to the invention, so that it is largely energy self-sufficient.

Preliminary tests have shown that approximately 80 Nm ^{3 of} biogas with an energy content of 6.5 kWh can be obtained from the treatment of one ton of household waste.

In the above-described embodiment, that is Reactor assigned to a wastewater treatment plant. Alterna The wash-out liquid could also be used in an existing one Wastewater treatment plant can be integrated or directly into the Kanalisa tion initiated or another treatment step be performed. Fresh or be driving water or a slightly contaminated wastewater used.

Following the anaerobic fermenter 66 is followed by a two-stage aerobic aftertreatment 70 , whereby foul water from the biogas plant is aftertreated to minimize the residual load and nitrogen is eliminated.

The resulting wastewater 72 is fed to a further treatment stage or discharged directly into the sewage system, depending on the load and applicable legal regulations. The scrubbing liquid cleaned in aerobic biology 70 is then fed via the distributor 20 to the reactor 1 . As indicated in FIG. 1, a partial flow of the digestion water from the anaerobic fermenter 66 can be fed directly to the distributor, bypassing the 2-stage aerobic biology 70 , in order to have a catalytic effect on the biological digestion in the reactor 1 .

Due to the flow guidance according to the invention within the reactor 1 , an aerobic hydrolysis occurs, whereby through the air flowing through the substance mixture 2 and the moisture of the substance mixture set via the wash-out liquid, an aerobic, thermophilic heating takes place, through which the cells of the organic matter are broken open and the released organic substances are discharged through the washout liquid.

The decomposition of the organic material is due, on the one hand, to the aerobic decomposition of the available carbon C to CO ₂ (carbonic acid) and, on the other hand, the washing out of the dissolved and acidified organic matter and the removal via the washing liquid. Due to the aerobic, thermophilic reaction and the simultaneous degradation of the organic compounds, the temperature in the substance mixture increases during the extraction process (for example to approximately 40 to 50 ° C.). This increase in temperature releases water vapor which is carried out via the supplied air. This water vapor discharged with the air can be fed as condensate to the wastewater treatment system described above.

The air flowing out of the reactor 1 is loaded with carbon dioxide as a decomposition product and the water vapor produced by the heating. The exhaust air loaded with organic components can be fed to a biofilter, in which biological cleaning takes place using aerobic microorganisms.

Pure water is initially used as the wash-out liquid used that after starting up the plant and Errei Chen almost stationary process parameters through during the aerobic treatment dissolved salts in an acidic state is transferred. The slight acidification of the water below supports the washout of soluble organic, inorganic substances and water-soluble fatty acids.  

As further shown in Fig. 1, the mixture of substances 2 located inside the reactor 1 is subjected to shock-shaped impulses by the reciprocating movement of the conveyor wedges 46 , so that shear, transverse and longitudinal forces are introduced into the mixture of substances the flow channels of the evasive fluid and the air are destroyed. The magnitude of these forces is designed so that on the one hand they are large enough to destroy these channels and chimneys, but on the other hand they do not lead to any destruction of the layer structure.

In the embodiment shown in FIG. 1, these impulses are brought about by the movement of the scraper floor. Alternatively, however, as shown in FIGS. 6 and 7, other exciters could also be used to apply shear forces to the mixture of substances 2 and to destroy the channels, as shown in FIGS. 6 and 7.

After the above-described hydrolysis, ie the digestion of the organic constituents and the extraction of these constituents by means of the wash-out liquid, the material discharge 28 is fed to drying. It has proven to be particularly advantageous if this drying is carried out as aerobic drying, since the residual moisture can then be reduced with a minimal expenditure of energy. Such aerobic drying can be effected, for example, by interrupting the supply of the washout liquid via the distributor 20 , so that the mixture of substances 2 after the hydrolysis is only flowed through by the air. The aerodynamic degradation of the still available carbon C to carbon dioxide takes place due to the flow through the moist substance mixture 2 . Furthermore, similar to hydrolysis, the mixture of substances is warmed due to the microbial conversion and water vapor is thereby discharged through the air flowing through. Due to the aerobic decomposition of the carbon and the removal of the water vapor, the residual moisture of the mixture of substances is reduced, and the desired proportion of dry substrate can be easily adjusted by the duration of the aerobic drying.

In the exemplary embodiment described above, the hydrolysis and the aerobic drying are thus carried out in a single reactor 1 . In other words, the reactor 1 can be used for drying as well as for percolation without modification, so that a simple system construction is ensured.

Alternatively, the reactor 1 from FIG. 1 could be followed by a dryer according to FIG. 2, to which the material discharge 28 of the reactor 1 is fed. This aerobic dryer 74 has essentially the same structure as the reactor 1 of Fig. 1, ie the mixture of substances, in this case the material discharge 28 is via a device 4 device in a lock provided and after aerobic drying via a Discharged from support device 6 . The dryer 74 has in the difference to the above-described reactor 1 several Luftanschlüs se 14 perpendicular to the plane one above the other, so that the air can be blown flat. The drying air can in turn be conducted in countercurrent or in cocurrent to the mixture flow and is accordingly supplied or discharged via air connections 14 , 16 .

In contrast to the reactor from FIG. 1, the dryer 74 from FIG. 2 has no distributor 20 for applying washing liquid.

During aerobic dryer 74, in turn, is a Teilrückfüh tion of the signal at the output of the dryer 74 Trockengu tes 76 as circulation 78 and / or the discharge of a ge dried product 80 is provided. The mixture of substances to be dried passes through the dryer 74 preferably again layered, the channel formation being prevented by impulsive shear, transverse and longitudinal forces. Of course, this two-stage process could also be carried out by two reactors connected in series according to FIG. 1, the hydrolysis in the first reactor being carried out by supplying air and washing liquid, while in the second downstream reactor 1 it is only aerobic drying by supplying air .

Fig. 3 shows an embodiment in which three actuators 1 a, 1 b, 1 c according to FIG. 1 are connected together with three dryers 74 a, 74 b, 74 c according to FIG. 2. Accordingly, the three reactors 1 a, 1 b, 1 c are assigned a common conveying device 36 via which the mixture of substances 2 can be fed to the individual reactors 1 a, 1 b, 1 c. Appropriate metering devices 34 can in turn be used to adjust the flow of material to the individual reactors 1 a, 1 b, 1 c.

The material 28 a, b 28, 28 c from the individual Re actuators 1 a, 1 b, 1 c can again be fed back via the metering device 34 as circulation 34 or supplied as a product 30 for further processing or as material 28 of the aerobic drying become. The material discharge 28 from the reactors 1 a, 1 b, 1 c is fed via a conveyor 84 and suitable dosers 34 to the dryers 74 a, 74 b, 74 c.

In the system diagram acc. Fig. 3 is also vorgese hen that the mixture 2 is also supplied directly, ie bypassing the reactors 1 of drying. This is the case, for example, if the present mixture of substances already has a considerable proportion of dry substance, so that wet washing is no longer carried out.

The material discharge from the dryers 74 , ie the dry material 76 a, 76 b, 76 c, is then either further processed as a dry product 86 , fed as drying material 78 again, or supplied as an intermediate product 88 to a device 90 for dewatering and / or compacting .

The device 90 is also used for the further processing of the material discharge from the reactors / dryers shown in FIGS. 1, 2. The device 90 can, for example, be formed as an extruder or drying / extrusion press, so that the mechanical action and the heat generated by the build-up of pressure result in a further drainage or drying of the intermediate product 88 .

In the device 90 , the extracted residual waste is adjusted to a dry matter content of <60%. In a preferred embodiment, the device 90 further contains a high-pressure press, via which the extracted, dewatered material can be pelletized. Densities of 1.7 t / m ^{3 are} achieved. The energy expenditure for the production of the pellet is approx. 1% of the energy content of the pellets if one assumes an average energy content of 14 MJ / kg.

Depending on the configuration of the device 90 , the dewatered end product 92 can be present as a pellet, briquette or other compact form. Through the above-described process steps, a non-elutable and non-breathable product can be produced, which is characterized by a high proportion of dry matter, and in contrast to the known processes, no external thermal energy has to be used for drying.

The material dewatered via the device 90 can be subjected to post-drying by means of composting or belt drying. Up to now, post-rotting has usually been carried out after mechanical-biological treatment of garbage in order to achieve additional degradation of organic material and drying of the leached-out rest. Subsequent rotting can easily be done on open rent. The proportion of biogenic material is sufficiently high even after percolation so that the rotting temperature rises to 70 ° C. within 4 to 6 days. The residue treated in this way reaches a dry matter content of up to 80% within 10 to 16 days. Since waste heat would be available for drying the percolation residue in the process described above due to the biogas production and the electricity generation in a gas engine, a space-saving drying process can also be used as a post-rotting.

The arrangement shown in Fig. 3 is chosen when continuous continuous operation is desired. With high throughput rates, the system can be expanded by adding further modules (reactors 1 , dryer 74 ).

The conveyors 36 and 84 and the dosing device 34 (material deflection) can be controlled such that the sequence of filling, emptying or by mixing (circulating material) of the individual reactors, dryers can be changed in any order.

Fig. 4 shows an embodiment in which a container 96 Be divided by two partitions into three chambers or reactors 1 a, 1 b, 1 c. These chambers correspond to the facilities acc. Fig. 1 and gem. Fig. 2 in which the hydrolysis and / or aerobic drying can be carried out.

The dense container 96 is assigned a common Förderein direction 36 , via which the substance to be prepared mixture 2 is supplied to the container 96 . From the common men conveyor 36 , the mixture of substances on the Do sizer 34 is guided to a cross conveyor 38 , which is designed as a distribution crane in the embodiment shown. This has a material drop 40 , which is movable by means of the distribution crane (cross conveyor 38 ) over the entire cross-sectional area of the container 96 . This ensures that the subspaces 1 a, 1 b, 1 c of the container 96 can be loaded with the mixture of substances 2 in layers.

The preparation of the mixture of substances (material discharge 28 or dry material 76 ) is discharged via a discharge device 6 which, for example, can be the one in FIG. 1. According to the variants shown in FIG. 4, several discharge devices 6 a, 6 b, 6 c can also be formed side by side in the bottom region of the container 96 . In the game shown Ausführungsbei is the container 96 leads out as a multi-chamber dryer, so that this is carried out with air connections 14 , 18 , in Fig. 4 only the overhead Luftan circuit 18 is shown. Also in this variant it is easily seen that the air is guided in cocurrent or in countercurrent to the mixture of substances. The container 96 could of course also be carried out as a reactor with several subchambers. Of course, the reactors / dryers shown in FIGS. 1 to 3 can also be designed with a plurality of discharge devices 6 lying next to one another.

The material discharge 28 can be fed back to the conveying device 36 via the dosing device 34 as circulating material 32 or can be discharged as a product 30 .

Fig. 5 of the material mixture 2 is to illustrate the distribution is a plan view of the container 36 of Fig. 4. Accordingly, the mixture of substances 2 means to the conveyor 36, for example, given a conveyor belt and fed to a distributor crane 38 about this, the, in the direction of arrow 100 101 above the partitions 98 , 99 can be moved. The distribution crane 38 carries a movable or several stationary material dumps 40 , so that the entire width (vertical Fig. 5) of the subchambers 1 a, 1 b, 1 c can be covered.

The prepared mixture of substances is discharged from the container 96 in the direction of the arrow 102 and this material discharge 28 is transported away via a suitable conveying device either as a product 30 or as a circulating good 32 . The latter is transported back to the conveyor 36 via a conveyor belt and then introduced again into one of the compartments 1 a, 1 b, 1 c.

In the above-described embodiments, the chimney formation was prevented by the forces introduced into the heap via the discharge device 6 , which caused a wavy vertical movement in the bed and thus led to a new formation of the bulk material surfaces and destruction of the channels. Depending on the quality of the mixture of substances to be processed, the shear forces introduced in this way can sometimes be too low to effect the required mechanical disintegration of the pile. In the above-described reactors 1 , the proportion of the material to be circulated 32 is then increased so that the shear forces required for the material exclusion are introduced via the conveying elements for conveying the material to be circulated 32 .

This variant is regarding the energetic and Material costs are still much cheaper than that State of the art at the beginning, in which agitators in Inside the reactor used to introduce the shear forces become.  

The energy and equipment expenditure can be further reduced if the reactor / dryer according to the invention is executed in the manner described in FIGS . 6 or 7.

In the exemplary embodiments described in FIGS . 1 and 2, the process air was blown in through one or more air connections 14 into the bottom part of the reactor 1 or the dryer and then enters through the sieve plate 8 into the bed (heap). In contrast to this, in the exemplary embodiments shown in FIGS . 6 and 7, the process air is blown in via a plurality of lances 110 distributed over the cross section of the reactor 1 , the nozzles 112 of which are in the lower region (view according to FIGS . 6, 7) of the pile 114 flow out. The lances 110 pass through the sieve tray 8 and the discharge device 6 - in the present case the push tray.

The process air or compressed air lances 110 are each connected via a control valve 116 to a pressure line 118 which opens into a pressure accumulator 120 . This is connected to a compressor 122 , via which fresh air or air 124 returned from the exhaust air treatment (biofilter) is brought to the system pressure, ie the pressure in the pressure accumulator 120 . The control valves 116 are connected to a process controller 126 and thus can be individually activated or closed.

The opening cross section of the control valves 116 can be continuously adjustable as a function of the process control 126 , so that the pressure of the process gas can be changed.

The system pressure in the pressure accumulator 120 is preferably set to a pressure of more than 4 bar. When a control valve 116 of a lance 110 is completely open, compressed air 128 emerges from the nozzle mouth upward (view according to FIGS. 6, 7) and flows through the heap 114 in the vertical direction with the maximum pressure, the arrows in FIGS. 6, 7 indicating that the compressed air 128 is also deflected in the transverse direction. The pile 114 is partially or fluidized in the flow area of the compressed air 128 , so that the surfaces of the bed are newly formed and channels are destroyed. In other words, the compressed air that is injected produces a partial wave motion 130 in the heap 114 , which moves upward away from the nozzle 112 of the respective lance 110 through the heap 114 . By this wave movement, the mixture of substances is moved relative to one another, so that the surface of the particles is torn open and thus the mass transfer area is increased. Since the compressed air is pressed in only in pulses, the aggregate 114 sags again after the control valve 116 is closed, so that shear forces are again introduced into the aggregate 114 , which leads to a renewed reshaping of the surfaces and the destruction of channels. The laden air 123 emerging from the reactor 1 is fed to a biofilter.

In principle, two effects are achieved by the compressed air. On the one hand, shear forces are introduced into the pile 114 in the manner described above, and on the other hand the process air required for hydrolysis and / or drying is also supplied, so that practically shear force input and process air supply are combined. Model calculations showed that the supply of compressed air according to the invention allows the energy requirement to be reduced by up to more than 50% compared to a conventional reactor with an agitator.

The process control 126 and the control valves 116 are designed in such a way that the pressure of the process / compressed air can be changed over time, so that, for example, only process air with low pressure (0.5 bar) is supplied over a predetermined time interval, which is necessary for the Drying or hydrolysis is required, but does not lead to any noteworthy shear force input into the pile 114 . Depending on the dumping height and the quality of the mixture of substances to be processed, compressed air with a comparatively high pressure (<4 bar) is then intermittently supplied in order to introduce the shear forces described above and to avoid channel formation.

The valves 116 of the plurality of pressure lances 110 of the reactor 1 can also be controlled in succession, so that the pile is penetrated by an "expansion wave" which moves parallel to the drawing plane or perpendicular to the drawing plane in the illustration according to FIGS. 6 and 7 .

Otherwise, the exemplary embodiment shown in FIG. 6 corresponds to the exemplary embodiments described above. In other words, the mixture of substances 2 is introduced through the entry device 4 from above into the reactor 1 and migrates through it, the layer structure remaining essentially unchanged by the compressed air supply and the resulting partial fluidization of the pile. The processed mixture of substances is then discharged via the discharge device 6 , ie a moving floor, and fed to the further processing steps.

In the exemplary embodiment shown in FIG. 7, the mixture of substances 2 is fed in on the left end face of the reactor 1 in FIG. 7 and discharged downward on the opposite side of the reactor 1 . Accordingly, the mixture of substances travels through the reaction space 12 with a vertically arranged layer structure, as is identified by the reference numerals l ₁ to l _n . In other words, the mixture of substances moves through the reactor in the horizontal direction (1), while in the exemplary embodiment illustrated in FIG. 6 it is moved through the reactor in the vertical direction.

Otherwise, the exemplary embodiments shown in FIGS . 6 and 7 correspond to the previously described exemplary embodiments, so that reference is made to the previous statements with regard to the other components. For the sake of simplicity, the same reference characters as in FIGS. 1 to 5 have been used in FIGS. 6 and 7 for corresponding components.

Put simply, in the exemplary embodiments shown in FIGS. 6 and 7, the agitator used in the prior art is replaced by a “compressed air agitator”, the pressure of the compressed air being chosen such that the layer structure is essentially retained. By the individual controllability of the distributed over the cross section of the reactor 1 Steuerven tile 116 the aggregate 114 may be selectively pressurized bumps, so that the shear forces prozeßab dependent, ie, depending on the quality of the aufzuberei Tenden material mixture and on the residence time in the reactor 1 with Compressed air or process air can be supplied. The applicant reserves the right to direct independent claim sets to the variants shown in FIGS . 6 and 7 and 1 to 5.

A method for the preparation of a Structural components and organic matter contained mixture of substances and an apparatus for performing this method. Erfin accordingly, the mixture of substances becomes impulsive or peri odisch with a force so that the formation of Flow channels for a washout liquid or process air in a pile can be prevented.

Claims (20)

1. A process for the preparation of a structural mixture and organic matter-containing substance mixture ( 2 ) which is taken up as a heap and is subjected to an aerobic digestion or an aerobic drying in a reactor ( 1 ) by means of flow with process air and / or addition of a wash-out liquid, so that the soluble organic constituents are discharged, characterized in that the mixture of substances ( 2 ) is impulsed or periodically with forces approximately perpendicular and / or parallel to the direction of movement of the mixture. 2. The method according to claim 1, characterized in that the forces for unlocking the pile ( 114 ) are applied by compressed air. 3. The method according to claim 1 or 2, characterized in that the compressed air or the process air through nozzles ( 112 ) in the head part and / or in the bottom part of the reactor ( 1 ) is supplied. 4. The method according to claim 3, characterized in that the process air and the compressed air are supplied through the same nozzles ( 112 ). 5. The method according to any one of the preceding claims, characterized in that the reactor ( 1 ) is operated continuously and the mixture of substances is passed through the reactor ( 1 ) approximately in parallel or in crossflow to the process air. 6. The method according to any one of the preceding patent claims, characterized in that the wash-out liquid is supplied through a distributor ( 44 ) in the head part of the reactor ( 1 ). 7. The method according to any one of the preceding claims che, characterized in that the compressed air with egg nem pressure of more than 2 bar, preferably more than 4 bar is supplied. 8. The method according to any one of the preceding patent claims, characterized in that the treated substance mixture ( 2 ) is withdrawn via an arranged discharge device ( 6 ) on the bottom part of the reactor ( 1 ), via which the forces alone or additionally can be brought into the pile are. 9. The method according to any one of the preceding claims che, characterized in that the aerobic Digestion of aerobic drying of the mixture closes. 10. The method according to claim 4, characterized in that the mixture of substances ( 2 ) successively passes through several re-digestion and / or drying steps. 11. The method according to any one of the preceding claims che, characterized in that the digestion and / or the aerobic drying a compacting of the Mix of substances connects. 12. The device, in particular for carrying out the method according to one of the preceding claims, with a reactor ( 1 , 74 , 96 ), which is assigned an entry device ( 4 ) for introducing a mixture of substances, the bottom part and / or the head part the reactor ( 1 , 74 , 96 ) inlets ( 14 , 18 ) for introducing process air and / or in the head part of the reactor ( 1 , 74 , 96 ) a distributor ( 20 ) for washout liquid are arranged, characterized by an excitation device ( 6 , 112 ), by means of which pulses or periodic forces can be applied to the mixture of substances ( 2 ) contained in the reactor ( 1 , 74 , 96 ). 13. The device according to claim 12, wherein the excitation device is a compressed air system ( 22 , 120 , 116 , 110 , 112 ), via which compressed air can be supplied to act on the pile ( 114 ) with shear forces. 14. The apparatus according to claim 13, characterized in that the compressed air system in the bottom part of the re actuator ( 1 ) has outlet nozzles ( 112 ) which are connected to a pressure accumulator ( 120 ) fed by a compressor ( 122 ). 15. The device according to claim 13 or 14, characterized in that the compressed air system is assigned a controller ( 126 ), via which the pressure of the compressed air or process air can be varied. 16. Device according to one of the claims 13 to 15, characterized in that via the compressed air system Compressed air and process air can be supplied together. 17. Device according to one of the claims 13 to 16, characterized by a gas cleaning system for Rei Cleaning and return of the process and / or compressed air. 18. Device according to one of the claims 13 to 17, characterized in that the excitation device is at least partially formed by a discharge device ( 6 ) on the bottom part of the reactor ( 1 , 74 , 96 ). 19. Device according to one of the claims 13 to 18, characterized in that a plurality of reactors ( 1 , 74 , 96 ) are connected in series, with a plurality of reactors ( 1 , 74 , 96 ) being assigned a common entry device ( 4 ) via which the substance mixture ( 2 ) to be prepared can be supplied. 20. Device according to one of the claims 13 to 19, characterized by a compacting device ( 90 ) for compacting, dewatering and shaping the processing substance mixture.