DE2506795A1 - METHOD AND DEVICE FOR CONVERTING ORGANIC WASTE INTO GRANULATE - Google Patents

Description

S, A. F. Societe Agricole et Fonciere S.A., Luxembourg-Ville

Process and device for converting organic waste into granules.

The invention relates to a method and a device for conversion of organic waste in granules, the organic waste initially to a moisture content of 45 - 60%, preferably from 50 - 55%.

The role of humus in soil fertility is important as well It is imperative to have a sufficient content in the cultivable of it To maintain earth. For various reasons and as a result of economic conditions that lead to specialization Finding organic fertilizers near a certain growing area has become quite difficult and is becoming more and more difficult. In it is close to vegetable-growing areas or wine-growing areas sometimes possible to use a practically evaluable source of animal education

9000, S59.12D.2 / 2a - BIl / KW / dw

509883/0611

Finding divorces, such as dung heaps from cattle, horses, etc. However, the problems of an expensive transport for a very moist mass and the difficulties of Handling, storage, workers, smells and sight, and neighborhood prejudices are resolved. the Usable organic waste can be of vegetable origin, such as vegetable remains, distillation residues, peel of citrus fruits, etc., or of animal origin such as excretions from cattle, horses, sheep, poultry, etc. mixed with Plant parts, such as straw, hay, etc. These organic masses have a heterogeneous structure and contain, depending on the duration of the Storage a considerable amount of moisture, which can reach up to 85 - 90% water. Storage and handling also causes interference of foreign bodies such as wood, stones, pieces of metal, etc. Their use for organic soil improvement can therefore depend on the economic Position from outside the areas where these masses occur. Thereby exist for their application not insignificant restrictions because of the odors that occur and pollution.

Attempts have already been made to subject this organic waste to physical, mechanical or thermal treatments in order to achieve a or several organic materials, which arise in a certain region, from their damp, dirty and often bad smell Raw state in a water-free, dried, odorless, easy to handle, storable, economically transportable and easily applicable state of use.

According to a known procedure, the organic ones are dewatered Mass by heating this mass as such to cause evaporation

B098S3 / 0611

effect of water. This mass, which is initially moist with a water content of 65 - 85%, goes after evaporation into a mass with a moisture content between 8 and 15%. To ensure such a drying process, it is necessary to to overheat compact blocks of this mass. After this process, the mass is ground to turn it into a powder. This Powder is then pressed together in extrusion presses by means of mechanical devices to form small cylinders, the diameter of which in the order of magnitude of 5-10 mm and their lengths between 10 and About 30 mm. The mechanical pressures that are necessary to achieve such a product are very high and range not always enough to compress a dried powder back into pieces. It is therefore often unavoidable to moisten the mass obtained again with steam or atomized liquid manure. The granulated product is very compact, very little porous and has a smooth and impermeable surface, so that the absorption takes a long time through the soil because the product is practically impermeable to water. Although the product obtained despite these imperfections represents a good quality organic soil improvement, however, the disadvantages must be pointed out which occur in its manufacture and application. These disadvantages are, above all, a considerable amount of dust and the appearance of odors during dehydration at high temperatures, which favor the formation of mercaptans, the uneven heating of the Product in its mass, the formation of compact granules with a waterproof outer surface, which only after a long period of time be picked up from the ground, and the use of high pressure extrusion presses to process a dry and rough mass,

509883/061 1

Another known method uses a similar technique but is limited to the manufacture of the dried powder. If, in contrast to the granules, the powder is absorbed very easily and very quickly by the ground, its practical application offers however, several disadvantages, such as the formation of considerable amounts of dust, the blowing away of these dusts by the wind and the danger inhalation by workers.

Affected by the technology used in the manufacture of chemical fertilizers Another known procedure (FR-PS 2 192 081) provides for the wet grinding of manure in order to produce a homogeneous pulp with a Moisture content between 60 and 70% using a roll crusher with grooved rolls. The formation of cylindrical Sticks from the moist pulp are made by means of an extruder with a cutting device and the subsequent granulation these sticks in a granulating machine to obtain roughly spherical granules. These granules are then dried in common devices with a fluid bed,

In another known procedure (GB-PS 835 216) brings the organic waste to a moisture content of 45 - 55%,

and
by mixing the moist mass / relatively dry mass and then granulating this mixture in a granulating machine, whereupon these granules are dried in a fluidized bed. This procedure offers the advantage of a practical implementation in two separate phases, namely a phase of transferring the raw material into a preliminary stage with a moisture content within a certain range, and a phase of granulation using a granulating machine which exerts pressure on the granules and therefore makes homogeneous drying extremely difficult. The final structure of the granules is relatively little porous,

509883/0611

so that their uptake by the soil is also difficult and long-lasting,

The purpose of the invention is therefore essentially to avoid this Disadvantage.

To this end, the method according to the invention is characterized in that that the waste previously brought to a moisture content of 45 to 60%, preferably 50 to 55%, is homogenized and subjected to a comminution, then pressed into thin strands and the strands obtained finally physical effects and exposed to drying, granules by breaking the strands without cutting, without pressure and without the use of a granulating machine can be obtained.

In this way, there is no need for a cutting device in the second phase and not a granulating machine, but the granules form themselves by breaking the strands coming out of the extruder escape, especially under the influence of their own weight and free fall and, if necessary, by vibrations and Impact effects. Form under the action of their weight already traces of cracks in the strands at the exit of the extruder, the granules are formed in this way by themselves without pressure, and thanks to a moisture content that has been carefully selected for the raw mass. The moist granules are only slightly compressed and their natural or artificial drying to achieve a moisture level of 10-14% is carried out regularly on the small ones Pieces of mass and under good conditions, the final structure of the granules is also porous and absorbent for water, whatever their absorption relieved by the bottom.

509883/061 1

2506798

The invention also relates to an implementation device of the process, which is characterized by storage and mixing areas for the organic waste, at least one degassing chamber to absorb the calories of the exhaust gases for the purpose of pre-drying the moist, organic waste and to separate the dry from them Dust particles carried along by gases, furthermore through at least one pre-drying furnace and crushing and rolling devices, furthermore through a Feed device with a regulator and through a comminution device fed by this, an extruder and at least an evaporation bed with a vibrating, perforated bottom as well by a hot gas source, which hot gases in the evaporation bed passes through the bottom holes, and through at least one resting tank.

An embodiment for carrying out the method according to the invention is described below, for example, in connection with the accompanying drawings, in which:

Fig. 1 schematically shows the plant for preprocessing the mixture

organic waste up to a moisture content of 50 - 55%,

Fig, 2 schematically in side view the comminution and the

Rolling in the device according to FIG. 1,

Fig. 3 schematically the essential parts of the device for

Achievement of the end product and

4 shows schematically additional equipment parts for a device according to Fig. 3.

The device shown in Fig. 1 has a bearing surface 1 for Storage of manure and moist, organic matter, a drainage ditch for manure and other liquids from the storage of the product

509883/0611

on the surface 1, furthermore a storage surface 3 for dry organic Masses and a mixing surface 4 for mixing moist organic and dry organic matter. Another mixing surface 5 is used to mix dry organic matter and liquid manure by moistening to cause fermentation. Furthermore, a pre-drying oven 6 and a degassing chamber 7 are provided for removing all of them Exhaust gases from the production equipment as well as those from the pre-drying oven 6 and the evaporation device as shown schematically in FIG. 3. The system also has a trigger 8 to exit of water vapor and cooled gases into the atmosphere. Furthermore is provided a. Detector 9 for metal pieces, a lump breaker 10, a roll crusher 12 to the hard materials to a size below 3 mm to bring a conveyor belt 11 between the lump breaker 10 and the roll breaker 12 and a removal belt 13 for removal of the masses from the roll crusher and a storage surface 14 for the intermediate product obtained in this way with a water content from 50 - 55%.

A bucket chain device is preferably used on the mixing surface 4, which is a good efficacy for dosing the

-active masses and generally a good mixture and the vegetable Pre-shredded fibers. This surface 4 allows a first sorting out of visible foreign bodies,

The pre-drying in the furnace 6 is carried out by hot gas at a Temperature of 120 to 150 ° C approximately, around that coming from surface 4 Bring mixture with a water content of 70% to a water content below 60%, preferably close to 50%. In the degassing chamber 7 you bring certain amounts of moist, organic matter, to deposit them there. They absorb the calories of the hot gases and the dry dust particles that are carried away and carried in to the vent

5 0 9-883 / 061 1

be deposited in the degassing chamber. This storage of moist organic matter can either be static in this degassing chamber be made or dynamically by means of a belt with a continuously functioning drive.

The origin of the raw materials for the storage area 1 can be manure his and organic waste, the humidity of which is between 60 and 85%. For storage area 3, dried manure can be used, as it occurs in certain poultry holdings, as well as dry organic masses, for example distillation residues, as well sifted manufactured products outside the specified grain size and dust after evaporation and prior to storage of the final granulated products during bagging. These materials have a moisture content between 10 and 30% water each according to origin. Manure and sewage from the storage area 1 and from the trench 2 are added to this dry starting material.

The various possible circuits between positions 1 to 7 are indicated by arrows. Several circuits of the moist mass are provided in order to lower the percentage of moisture and to a value below 60%, preferably close to 50-55% water to reduce so that the mass meets the requirements for the formation of granules from continuous strands without cutting devices.

A certain amount of organic, moist matter is stored in the degassing chamber 7, where it is partially evaporated by absorption learns about calories given off by the exhaust gases and where they accumulate in dry dust particles, those of them Gases are carried. The heterogeneous mass from the degassing

509883/061 1

chamber 7 is conveyed onto the mixing surface 4. After a first This mass is homogenized, for example by means of a caterpillar tractor, with moist organic masses from the storage area mixed in if it is too dry, or dry organic masses from the storage area 3 if it is too moist. This one got first Intermediate product is then conveyed to the detector 9 for mechanical foreign bodies, as indicated by the arrow II.

Certain amounts of moist organic matter from storage area 1 are mixed with dry organic matter from area 3 and promoted to the mixtures whose moisture is in a ■ value range is between 45 and 60%. This intermediate product obtained is also conveyed to the detector 9 like the one mentioned above.

The liquid manure from the ditch 2 is used to form artificial dung on the area 5, in which the dry organic matter of the area is sprinkled with it and allowed to ferment. The intermediate product obtained in this way is also passed to the detector 9 _s as indicated by the arrow III.

Certain amounts of the moist organic masses of surface 1, homogenized on surface 4 and optionally mixed with dry ones organic matter from surface 3, reach a degree of moisture of 70% and are after entering the pre-drying oven led, which they leave with a humidity level of 5Θ - 55%. The intermediate product obtained in this way is also conveyed back to the detector 9, as indicated by the arrow I.

509883/061 1

Visible foreign bodies such as stones, pieces of metal, wood, fabric, plastic, etc. can be removed from the mixing surfaces 4 and 5. The metals that have escaped visual inspection will be then from that. Detector 9 detected. The intermediate product is then crushed and mixed in a lump breaker 10 and rolled onto it between two rollers 12 to be deposited at 14. The lump breaker 10 is of known type, it contains two counter-rotating rollers with helical blades.

So that it is possible to achieve the formation of granules in the subsequent phase without the use of cutting devices, the mixture must have a water content between 45 and 60%. If the moisture content exceeds 60%, the strands of the mass can stick together and clump together. Is the Moisture content, however, below 60%, the mass strands are brittle and break into pieces, the length of which is between once or twice the Dimension corresponds to their diameter. In the case of strands with a cylindrical shape, therefore, their length is one or twice that of that the diameter. The breaks of the strands occur as the strands fall onto the conveyor belts due to the vibrations the evaporation devices, etc. If the moisture content is below 45%, there is a possibility that the strands of material will not develop well, especially if the pressures exerted on the material are not very high. On the other hand, the coefficients of friction are the Increased mass at the openings of the strand formation lattice and the Wear becomes considerable.

The pre-drying oven 6 can, for example, be filled with heavy oil no. 2 operated and generates combustion gases mixed with air.

509883/0611

This gaseous mixture has a temperature of the order of magnitude from 120 - 150 C. A pre-drying oven with a capacity of, for example, 9 tons / hour of starting material with a Moisture content of 70% can produce 6 tons / hour intermediate product with 55% water. That means a possibility of evaporation of 3 tons / hour of water.

The degassing chamber 7 can be equipped with a conveyor belt, which runs at a low speed of movement, so that the moist organic substances are within this chamber for a sufficiently long time. This is intended to absorb the dry dust from the exhaust gases and the remaining calories. In case of a final production of for example 4 ton / hour granules having 10-14% water can 100-150 receive kg / hour dust and absorb part of the calories of 300. 000 MSS / hour gas whose temperature is at 60 ⁰ C. In this way it is possible to obtain 20 tons / day of material with 55% water, which was processed with 75 - 80% water.

The dimensions of the individual machines in the plant depend on the desired hourly production of the manufacturing unit. For a production unit for the production of 4 tons / hour of a granulate with 12% residual water and the production of an intermediate product With a moisture content of 50 - 55%, for example, devices with the following hourly outputs can be used:

Pre-drying oven: 6 tons / hour
Degassing chamber: 1 ton / hour

Mixer for moist organic and dry organic masses:

1 ton / hour

50.9883 / 061 1

Mixer for dry organic and liquid masses: 0.5 ton / hour.

In summary, the first phase of the process, as described above, forms the following advantages: the phase of Production of the intermediate product is independent of the actual production phase, which gives the whole thing great flexibility gives. This phase is carried out until an intermediate product is obtained, which does not contain any hard foreign bodies with vegetable, partially contains shredded fibers and has a humidity of the order of 50 - 55% water. This moisture allows the manufacture of the end product by continuous extrusion without a cutter and without a granulating machine. This can be reduced by using suitable mixing ratios Percentage of moisture, which in turn avoids adding extra calories. The rest of the recording is used Calories and dust carried along in the exhaust. In this way one achieves a profitability under at the same time solving a major problem of atmospheric pollution. This distributes the application of the for the end product necessary calories, one undoubtedly saves on the total sum of the necessary calories for a certain production, but one also uses a part of it for this preparatory phase and thereby solves the problem of granulation, which the Saving corresponding machines allowed. By sticking to the use of an intermediate with a certain moisture content lasts, you can finally see the yields, the modes of operation, the outputs, the working methods and the settings of the various Mastering final production machines.

509883/061 1

At the end of the first phase there is an intermediate product which, in the loose state, has a paste-like, but not compact appearance and contains organic masses with a grain size of less than 0.5 mm as well as hard, rolled solids, the grain size of which corresponds to the

The distance between the rolling cylinders 12 corresponds to and is approximately 4 mm, also soft or fibrous elements, which are partially crushed by the chains of the crawler tractor and by the lump breaker and which consist of elements of low thickness, but whose length can reach several centimeters. The middle humidity this mass is between 50 and 55% water.

Ih the system shown in Fig. 3, which quite generally a Can be a production factory, this intermediate product is first homogenized by chopping, whereupon continuous strands are made forms by extrusion. The granules are then allowed to form by breaking the strands before and during the evaporation the granules and the strands, what with hot gases on a vibrating floor or by fluidization or by both Measures taken. The granules are then sieved to remove the particles from within the selected grain size and the dust, whereupon the sagging of the granules is carried out.

The system shown schematically in Fig. 3 has a feed funnel 15, through which the intermediate product arrives on a conveyor belt 17, above which a feed regulator 16 is arranged. This feed regulator 16 is known per se and has blades, which are set in rotation against the running direction of the conveyor belt 17. The delivery rate of the intermediate product can thereby can be set to match the running speed of the

509883/061 1

Acts conveyor belt or changes the distance between the controller 16 and the conveyor belt 17.

The system also has at least one, generally two chopping devices 18, one of which for preparation and the other is used for finishing, furthermore an extruder 20, a conveyor belt 21 between the extruder and an evaporation bed 22 with a vibrating bottom 23, which is inclined and perforated for the passage of hot gases 24, which from

a hot gas source, not shown, come. The plant contains also an elevator, which conveys the granules coming from the bed 22 into a resting container, as well as a sieve and a Dust sieve, an evaporation bed to end the evaporation if necessary, a cooling device using cold air for the granulates, a storage silo, a device for the recovery of the dust, which is caused by the handling and the vibrations in the storage accrues, and a bagging device with dedusting system, All these devices are known per se and are not shown. The processed Mass goes from one machine to the other, as indicated by the arrows in the schematic drawing.

As soon as the intermediate product is consistently very fibrous, as is the case with manure is the case with an extraordinarily large amount of straw, it can be expedient be to provide two chopping devices, the first of which is used for preparation and the second for finishing. The first facility is therefore designed so that it cuts the fibers in lengths of a few centimeters, while the second device cuts these fibers cuts in lengths of a few millimeters. In general, however, one is content with the use of only a single chopping device.

509883/0611

This chopping device 18 has a worm screw 25, which is rotatably mounted within a cylinder 26 with a horizontal axis. The product is through this worm screw through the cylinder promoted and arrives at a grid 27 which is provided with holes. The end of the worm screw 25 is in contact with the grid 27, in such a way that the angle, which form the thread of the worm screw and the grid, decreasing to zero to achieve a shear effect. There are also Not shown knife provided, which by the screw rotation are driven and are also in contact with the grid in order to separate the fibers that are inevitably in Accumulate the height of the inlet openings of the grid 27. This measure prevents clogging in front of the grid, as is the case with chopping devices that use simple axial pressure of the Work ground against the grid.

A rotating, outer cutter 28 is driven coaxially with a speed different from that of the worm screw 25. It has the task of keeping the mass at the exit the openings of the grid 27 to be separated.

One for an output of around 9 tons / hour Mass with 50-55% water can be used, for example, a chopping device whose worm screw has a diameter of 600 mm and a slope of 250 - 300 mm and the with rotates at a speed of 20 revolutions / minute and with two inner knives, which sit firmly on the screw and brush over the grille. One uses a grid with a thickness of 20 mm, drilled with holes 30 mm in diameter evenly spaced 40 mm apart. The axis of the worm

509883/0611

The screw is preferably mounted in a ball bearing on the grid.

The outer knives 28, which brush over the grid, are preferably driven at a speed of 100-200 Revolutions per minute. It is important that the mass is never compressed, but continuously conveyed mechanically until it has passed through the holes in the grille.

The extruder 20 is the same machine as the chopping device with the difference that this machine has a grille 29, the outlet openings of which have a smaller dimension, and that no cutting device is provided for the strands 30 formed. Deposits of small fiber particles can occur on the inlet openings of the grid 29 occur, which could clog it quickly. To avoid this disadvantage, doctor blades can be provided, the rotation of which is coupled to that of the screw, as described for the chopping device.

For a strand output of 9 tons / hour, what a volume corresponds to the order of magnitude of 8 m ^ / hour, one uses for example also a screw with a diameter of 600 mm and a pitch of 250 to 300 mm, which with a speed of rotation is driven by 20 revolutions / minute, as well as a grid with a thickness of 15 mm, pierced with holes with a diameter of 10 mm evenly spaced from 13 mm. After evaporation, the granules obtained have a Diameter whose value is about 10% below that of the moist strand with 50-55% water. The lengths of the granules are approximately equal to single or double the diameter.

509883/0611

In the vaporization bed 22, the moist granules to form with a "water content of 50 - 55% on the perforated floor 23 is a layer, ■ which a mixture of gas and hot air 24 having a temperature of 120 - through which flows 150 ⁰ C. These gases. arise from the combustion of heavy oil in a combustion chamber, which is designed so that air can be added to the final mixture and is heated, whereupon the temperature equilibrium is established. The layer is in motion due to the fluidization that usually occurs, whereby the individual particles are mutually exclusive In addition, the bottom 23 is inclined by a few degrees to the horizontal and can be excited to vertical vibrations, so that the entire layer gradually moves from the inlet 31 to the outlet 32. The exhaust gases are collected in a flue 33 to to be passed into the degassing chamber 7 (Fig. 1).

The strands 30 with a corresponding moisture content have fracture cracks at the exit of the extruder 20. At the horizontal exit of the grid 29 they are exposed to gravity, which favors their breakage. The strands then fall onto the belt 21, where they break, and then again into bed 22, which causes more new breaks. The hot gases, the movements of the granules against each other and the vibrations cause further breaks in the strands in their length, which are then about one to two times the diameter is equivalent to. The granulation is obtained in this way solely by physical action, without cutting, without pressure and without a granulating machine.

In general, superficial evaporation of the granulate is obtained, while the middle core is still moist. The Kalo-

509883/0611

2506791

rien, which are transmitted through the hot gases, cause an increase in the temperature of the granulated mass, but the water remains trapped in the central core. It is therefore expedient to provide a period of rest in a cylindrical silo with a vertical axis, so that the water that is in the middle Core is contained, migrates outwards against the circumference of the granulate. The resting silo or container is opened via an upper opening loaded by means of an elevator, for example a bucket elevator. The container is therefore chosen to stand upright in order to accommodate its To be able to discharge by gravity. It is cylindrical in shape to prevent particles from adhering along angled walls avoid what can lead to the formation of bridges.

Small, vibrating apparatuses are expediently arranged on the inner surfaces of the container along one or more surface lines. The granules remain in the container for a sufficient time, about an hour, so that they are evenly distributed the moisture can take place.

The particles outside the desired grain size and the dust, which are removed by sieving, are deposited on the storage surface 3 funded back.

The evaporation in the bed 22 brings the moisture content with a value of 50-55% to a value of 10-14% and can in be carried out in a single step when the hot gases 24 have low temperatures of the order of about 60.degree and when the vibrating floor 23 is of sufficient size and slight inclination to allow the contact time between the hot gases and the granules is long enough to

509883/0611

to bring about gradually ^ continuous and regular evaporation. In order to handle larger quantities of material on a modern, industrial scale, the necessary dimensions are chosen in such a way that the bed with a vibrating base takes up a lot of space and its construction becomes very costly the longer the vibrating one Floor is, to which there is also the increased driving force for its vibration.

However, it is possible to increase the size and the cost of the installation lower and increase the yield, in particular the thermal yield, with the following measures: In the bed with vibrating soil, the mass in the form of granules is subjected to an initial dewatering phase, which it simply transforms into a no longer sticky state, whereupon they are placed in a resting container is promoted. It is then subjected to a fluidization and dehydration treatment in at least one evaporation bed with a solid, perforated base through which hot gases are passed.

The only condition that one demands of the crowd, which is the bed with vibrating ground, the one is that it is no longer sticky. This is enough to ensure the formation of granules, which do not have the tendency to clump back together, so that the dimensions of this bed and the rest time of the crowd are acceptable and economically reasonable limits can be kept.

The hot gases that vibrate the granulate layer in the bed Soil scoured are low in calories and high in moisture. They are preferably no longer passed into the degassing chamber, since their heat exchange is weak, but to the

509883/0611

Pile of raw material on the storage areas, leaving the dust and the fine particles, which are carried away by the gases, can be recovered by simple deposition. The hot gases which have flowed through the bed with solid bottom are much richer in calories and drier and are directed into the degassing chamber. The flow rate of the gases at the entry of the bed with solid bottom is preferably relatively high in one Of the order of 4 m / sec.

The additional device is shown in FIG. It has a conveyor belt 34 at the exit of the bed with a vibrating floor 22, a resting container 35, a first evaporation bed 36 with a solid, perforated floor 37, through which a stream of hot gas 38 flows at a temperature of about 100 ° C and a relatively moderately high temperature Flow rate of 4 m / sec, a conveyor belt 39, a second resting container 40 and a second evaporation bed 41 with a solid, perforated floor 42, divided into two sections, of which the first section 42a extends over the first two thirds of the length of the floor 42 extends and the second section 42b over the third third of the inclined floor. The section 42a is traversed from bottom to top by a stream of hot gas 43 at a temperature of approximately 100 ^° C. and an increased flow rate of the order of magnitude of 4 m / sec. These gases are collected above the bed by means of a vent 44. A stream of ambient air 45 flows through the second section 42b, which is discharged through a line 46 at the outlet. The degassing chamber 7 in the form of a tunnel is traversed by a conveyor belt made of slatted frame 48, which conveys the moist mass in the direction of the arrow F1. The hot and dust-laden gases, which are discharged via the evaporation beds 36 and 41, are introduced into the lower part of the degassing chamber 7 at 49 in countercurrent. 509883/0611

The pre-broken strands leaving the extruder 20 and their granulation in the bed 22 with a vibrating bottom 23 is completed, stay in this bed only as long as it is necessary to ensure a non-sticky state. The granules are then placed in the resting container 35 by means of the conveyor belt promoted and remain in this resting container for a period of time that is necessary to ensure an even distribution of the moisture content in the granules. This rest period allows the moisture to be distributed evenly through the granules a self-rewetting, which goes from the center to the outer circumference. A second contact with hot gases is permitted a rapid evaporation of water on the outer periphery and in lower layers, while the evaporation of water in the In the middle of a granulate that has already been dehydrated on the outer circumference and in the lower layers, an additional calorie expenditure and heating of the product, which can adversely affect its quality.

The granules are then in the dewatering bed 36 with solid Conventional floor construction where the drainage takes place under the action of hot gases 38. The granules, which in the Arriving at bed 36, you are already relatively dehydrated and warm. In addition, the hot gases flow into this bed with solid Soil with an increased flow velocity in the order of magnitude of 4 m / sec and do not cause a very substantial heat exchange, so that the 7 conducted gases are relatively dry and hot, so that an increased heat exchange takes place in the degassing chamber.

509883/0611

The granules are then transferred to the second resting container 40 by means of the conveyor belt 39, where a new, even distribution their moisture content takes place, after which they then get into the second bed 41. In the first section 42a this The dewatering is ended and the gases drawn off at the vent 44 are relatively very hot and dry. By doing In the second section 42b, the granules are cooled by a stream of air at ambient temperature. The one pulled off the trigger 46 Air has a temperature that is only a few degrees higher than the ambient temperature and becomes a heap of moist mass guided on a storage surface, whereby the dust and fine particles are recovered by simple deposition. The granules, which leave the bed 41 can be used immediately or stored in silos.

In the degassing chamber 7 flow through the hot, returned Gases 49 a layer 51 of moist raw material, which in a layer thickness of about 250-300 mm with reduced speed is moved, with a flow velocity in the order of magnitude of 0.4 m / sec. The heat exchange when flowing through the layer of moist raw material / acts as an evaporation of water, which is about eight times larger than what one gets through a superficial one Heat exchange receives. In addition, all dust and other particles that are carried away by the gases are recovered. The mass leaves the degassing chamber 7 with the desired moisture content between 50 and 55%. In a modified embodiment the relaxation chamber can also be equipped with a fixed slatted frame.

509883/061 1

Claims (25)

PATENTANS PR UEC HE , Then too thin are brought 55% _s characterized in that it is homogenized waste and a crushing subjecting - Iy process for the conversion of organic waste into granules, wherein the organic wastes initially to a moisture content of 45 - 60%, preferably from 50 Extruding strands and finally exposing the strands obtained to physical influences and drying, granules being obtained by breaking the strands without cutting, without pressure and without using a granulating machine, 2. The method according to claim 1 for converting a mixture of dry and moist organic waste, characterized in that that part of the wet waste is treated in a degassing chamber, where it is partially evaporated by adding calories occurs, which are contained in the exhaust gases, as well as an accumulation of dust particles that are carried along by these gases. 3. The method according to claim 2, characterized in that the mixes the mass coming from the degassing chamber with the dry mass. 4. The method according to claim 3, characterized in that one of the Mixture adds untreated wet mass if the mixture is too dry, or dry mass if the mixture is too moist. 5. The method according to any one of claims 2-4, characterized in that that you immediately and separately moist untreated masses and dry masses to achieve a mixture with the desired Moisture content mixes. 50988 3/0611 6. The method according to any one of claims 2-5, characterized in that a part of the moist, optionally mixed with dry masses is subjected to a pre-drying in a pre-drying oven which ^{is heated to a temperature of about 120 to 150 0} C until the desired moisture content is reached. 7. The method according to any one of claims 1-6, characterized in that that one mixes liquid organic waste of moist organic masses and dry masses by moistening and until it is achieved ferment with the desired moisture content. 8. The method according to any one of claims 2-7, characterized man
net that / subjects the mixtures to a crushing and rolling process. 9. The method according to any one of claims 1-8, characterized in that that one lets the thin strands emerge horizontally and without support from the extruder and thereby break them due to their weight as well as causing cracks, 10. The method according to claim 9, characterized in that there is at least one free fall coming from the extruder Provides strand sections. 11. The method according to claim 10, characterized in that the strand sections in an evaporation bed with a vibrating, perforated and sloping floor, through which hot gases are passed. 12. The method according to claim 11, characterized in that in the bed with vibrating bottom, the mass in the form of granules is subjected to a first dehydration phase, which it in 509883/0611 a non-adherent state, whereupon it becomes a Funded resting tank and then a fluidization and dewatering treatment is subjected in at least one evaporation bed with a solid, perforated bottom through which one conducts hot gases. 13, the method according to claim 12, characterized in that the hot gases passed through the evaporation beds create a flow velocity more than 3 m / sec. 14, the method according to any one of claims 12 or 13, characterized in that that the gases leaving the bed with solid bottom are collected and directed into a degassing chamber, where they are a Flow through a static or moving layer of moist waste. 15, the method according to claim 14, characterized in that the hot gases are introduced into the degassing chamber in countercurrent to the direction of movement of the layer of moist waste. 16, the method according to any one of claims 12-15, characterized in that that the dewatering of the granules leaving the evaporation bed with solid soil by transferring them to a resting container and then terminated in a second solid bottom evaporation bed which is perforated and divided into two sections, of which the first section, like the previous bed, is traversed by hot gases and the second section by cooled gases. 17, the method according to claim 16, characterized in that the hot, the second bed with solid bottom can also be collected by flowing gases and fed into the degassing chamber, 509883/061 1 18, the method according to any one of claims 11-17, characterized bed draws that the hot, the / flowed through with a vibrating floor Gases are directed to piles of wet waste on the storage areas. 19. The method according to claim 16 _S, characterized in that the cooling gases are directed to heaps of moist waste on the storage areas, 20. Device for performing the method according to claim 1, characterized by storage and mixing surfaces (L - 5) for the organic Waste, through at least one degassing chamber (7) to absorb calories from the exhaust gases for the purpose of pre-drying the moist, organic waste and for the separation of the dry dust particles carried along by these gases, furthermore by at least one pre-drying oven (6) and crushing and rolling devices (10, 12), furthermore by a feed device (15, 17) with a controller (16) and by a comminution device (18) fed by this, an extruder (20) and at least one evaporation bed (22) with a vibrating, perforated bottom (23) and by a hot gas source, which hot gases (24) into the evaporation bed through the bottom holes (23) conducts, and through at least one resting tank (35). 21. The device according to claim 20, characterized by degassing skammer (7) with a vent for steam and cold gas. 22. The device according to claim 20, characterized by a comminuting device with a horizontal worm screw (25) in a cylindrical housing (26) with a grid (27) on one Front side, on the inside of which the screw end with a, up to 0 ° 509883/061 1 decreasing angle is applied, furthermore with driven by the screw rotation and also resting on the inside of the grid Knives as well as with an external, rotatable cutting device (28), which have a different speed of rotation compared to the screw is driven and rests against the grille on the outside. 23. The device according to claim 20, characterized by a Extrusion press with a horizontal screw in a cylindrical Housing with a grille (29) on one end face, on the inside of which the screw end decreases with a rate of 0 ° Angle. 24. The device according to claim 23, characterized by a Extrusion press with knives driven by the screw rotation and resting against the inside of the grid to prevent deposits of fibrous particles at the inlet openings of the grid (29). 25. Device according to one of claims 20-24, characterized by at least one resting container (35) arranged after the bed (22) with a vibrating bottom (23) and at least one further evaporation bed (36, 41) with a solid, perforated base (37, 42) through which hot gases (38, 43) flow. 509883/061 1 Blank page