WO1993017280A1

WO1993017280A1 - Process for melting down combustion residues in slag

Info

Publication number: WO1993017280A1
Application number: PCT/CH1993/000035
Authority: WO
Inventors: Hans Künstler
Original assignee: Kuenstler Hans
Priority date: 1992-02-26
Filing date: 1993-02-11
Publication date: 1993-09-02
Also published as: EP0581918B1; CA2108677A1; JPH06507232A; DE59309121D1; EP0581918A1; ATE173332T1

Abstract

Instead of burning rubbish completely up, which has long been the aim, the material to be processed is first merely carbonised in a low temperature unit (2) and then, with the addition of carbonising agents or gases, taken to a high temperature unit (7) to reach the temperature needed to melt the slag and achieve complete combustion. It is thus possible that foreign substances (heavy metals) are absorbed in the slag and bind permanently therein. Concerning the equipment, the original, conventional combustion region is replaced by a generator for combustible carbonising gases so that, instead of being burned, the material introduced is merely gasified. Gasification or carbonisation may be controlled in any manner. The residues from the carbonisation process contain more combustion energy than the ordinary burned residues and may be subjected to a slag liquefaction process in the high temperature unit; a rotary kiln is proposed there. The end product is a completely burned, liquefied slag which may be allowed to set in any shape.

Description

METHOD FOR MELTING COMBUSTION RESIDUES IN SLAG

The invention relates to a method and a device for degassing, gasifying, burning and melting down waste and melting down solid residues, for example from domestic waste incineration plants, using waste as an energy source.

The fly ash, filter cake and slag from conventional waste incineration plants today contain, in addition to unburned carbon, heavy metal compounds which can be washed out and organic hydrocarbons. Legislation is now increasingly used worldwide to prescribe striking reductions in the amount of such pollutants (in a relatively short time) in order to reduce the ecotoxic potential of the slags and to enable safe storage and / or recycling. At the same time, the requirements for other solid residues (dusts and RGR residues) are also being tightened; Residues that can no longer be used should be able to be processed into residues that are as inert as possible.

As a rule, today attempts are made to reduce the volume of at least the spatial dimensions of the unusable components, which is the rest of the whole effort to counter in order to keep unavoidable residues as small as possible. In the case of highly toxic residues, a space-intensive, environmentally safe landfill is very expensive, especially when legal requirements regarding long-term safety have to be met.

Up to now it has not been possible to carry out combustion at such a high temperature in conventional grate furnaces for household waste, apart from. unwanted local. Heating that during the incineration process-related melting of the incineration slag could also take place for the permanent incorporation of heavy metals and burning out of organic, partly highly toxic compounds. According to current experience, slag liquefaction would cause the grates to stick together during combustion, or the liquefied slag would flow through the grate gaps. In other words, neither the combustion process known today nor the plants in use are suitable for such a procedure. In the few plants which consist of a combination of a grate furnace and a rotary kiln, melting of the slags has not yet been possible either, since in the firing zone the most possible total combustion of the waste is sought and also takes place and is therefore no longer sufficient in the rotary kiln Combustion energy for melting the slag is available. Apart from this, these rotary tube furnaces do not have the required properties and facilities for removing the molten slag. According to the task, such rotary kilns only serve to completely burn out the slag. With hazardous waste disposal, the waste is burned in hazardous waste rotary kilns at very high temperatures with the help of external energy. The slag problem is very minor here. The aim of the invention is to contribute to the relief of the environment. Its task is to specify a process for the effective inerting of slag, fly dusts, kettle ash and similar toxic substances and to create a device with which this process can be carried out. The material which is condensed and binds environmentally harmful substances in accordance with the inventive process is said to have a landfill form which is harmless to the environment (for example as a TVA inert residue according to the Swiss requirements of the Technical Ordinance for Waste) or is to be used instead of being disposed of for a useful purpose can.

With the method according to the invention, slags, dusts and boiler ash can be melted down solely by the energy content of the waste. The heavy metal compounds are immobilized, the glow loss is reduced to a minimum, the organic hydrocarbon compounds are reduced below the current detection limit and the specific volumes are greatly reduced. The basic idea of the invention is that instead of a complete incineration of waste, as has been sought up to now, only a substoichiometric carbonization of the process material is carried out beforehand in a low-temperature unit and then using the sulfurized materials or gases obtained in a high-temperature unit, complete combustion (for example in a rotary kiln) is carried out with subsequent slag liquefaction. The material remaining from the charring (residues) contains more combustion energy than the usual, burned-out residues and can be fed to a slag liquefaction process in the high-temperature unit, for example a rotary kiln. Part or all of the energy obtained by the gasification can be supplied to the slag liquefaction in gas form, so that the process can be controlled or regulated in a relatively simple manner. The end product of the process is a completely burned-out, liquefied slag that can be solidified in any form. Figure 1 shows schematically an overall system according to the invention, the waste-operated reactor with boiler and flue gas cleaning. The inventive method and also the essential parts of a device according to the invention can be discussed in this reactor.

FIG. 2 shows the temperature profile in the reactor, measured in a test facility.

FIG. 3 shows a diagram of the course, for example, of an addition of foreign matter for melting into the slag, here it is recirculated filter dust from our own plant, but it can also be foreign matter from other plants.

FIG. 4 shows an example of the composition of the residual materials from a ton of waste (Vehlow literature).

On the basis of these four figures, the invention is presented in its idea and its execution down to the details.

The reactor according to FIG. 1 is constructed using tried and tested plant components available on the market. In terms of process engineering, the components are coupled and connected in series so that the desired process can be carried out. The reactor points in the process direction, that is from left to right, the essential parts of the device: a feed point 1, for receiving the process material with devices for placing it on the smoldering grate (for example a feed grate); a generator 2 in which, with a uπterstoichiometric air supply, garbage garbage as an energy source or is gassed; In this generator, the following essential equipment parts are present: a feed grate 3, nozzles 4 and addition devices 5 and 6; then follows a rotary kiln 7 with a gas / air hood 8, for the combustion of the generated generator gases and for the burning out and melting of the slag; this is followed by an afterburning chamber 9 with an addition device 10, for example air supply for lingering and afterburning still combustible parts and then an empty draft for the flue gases to be discharged, which leads into a boiler group 11 for lowering the temperature and using the flue gases for heat; This is followed by an electrostatic filter 12 and a flue gas cleaning system 13 for cleaning the flue gases and finally the chimney 14 for discharging the cleaned flue gases into the atmosphere. A whole number of process paths designated with letter groups intervene in the process at various process points, the meaning of which is explained in connection with the function discussion.

First, the waste is conveyed to a feed grate via a feed device in a generator. Partial degassing and gasification and partial combustion take place here in a substoichiometric environment. The garbage is soaked and preheated. Since the processes in the generator (grate), in contrast to the most widespread grate systems, with much smaller amounts of air, especially with a smaller amount of underwind resp. smaller (substoichiometric) excess air, much less so-called "hot combustion nests" (hot spots) are formed in the micro or local area. This causes a strong reduction in NOx emissions (probably 50% -70%).

The rotary kiln is connected to the generator for melting its own and foreign substances into the slag. A transition of the generator to the rotary tube is well distributed into the air under controlled conditions Rotating tube injected. In the same region, foreign matter, recirculated dusts, dusts and slag from other plants and so on can also be abandoned. A combustion of the carbonization gases generated in the generator and a burnout of the solid feed material then occur. As a result of the energy released in the process, the temperature in the rotary tube is raised above the slag melting point and the entire solids (self-slag and foreign substances) are liquefied. The circulation of the slag in the rotary tube leads to thorough mixing, homogenization and good burnout. The slag flows out of the slightly inclined rotary tube into a pre-cooler and then into a detoxifier.

For complete combustion of the flue gases, secondary air is fed into the flue gas chamber, which causes the gases to burn out properly during the same dwell time. Instead of secondary air, flue gases can also be recirculated or vapors injected. The boiler of the reactor presented here must be designed for the higher flue gas temperatures of this process. By means of large radiation areas and a long gas path, the flue gas temperature is lowered to the first convection part below the air traffic jam softening point.

After the boiler, the reactor can be equipped with the gas cleaning components currently on the market, such as dust filters, laundry, denox and dioxin separation. However, these components can be designed for ^* significantly lower gas volume flows compared to conventional waste incineration plants. Since the final temperatures of the combustion process are lower in a standard system than in the process discussed here, correspondingly larger gas volumes result. For this reason, in the method according to the invention Efficiency of the plant higher than with conventional waste incineration plants.

Trials on a modified plant

Plants of this size cannot simply be set up on a trial basis or existing plants can be converted on a trial basis. However, it is also an aim of the invention to align the method with the use of as many proven and commercially available plant parts as possible.

To test the process, a specially selected plant was modified in terms of process engineering to match a reactor according to the invention. Various shortcomings were accepted, which are there: the amount of waste, that is, the energy required to liquefy slag, was difficult to regulate; the relationship between smoldering and combustion air could only be approximated; the injection of the combustion and burnout air could only partially take place in the correct amount and well distributed. In addition, the operational safety of the system had to be guaranteed.

Despite these restrictions, it was possible during several attempts to reach the temperatures required for the slag melting in the rotary tube. The calorific value was measured on average at H _u = 10,890 kJ / kg. Based on the knowledge gained, the minimum calorific value for the process according to the invention with controllable air supply can be operated at an estimated 7,500 kJ / kg. By preheating the combustion air and adding additives that lower the melting point of the slag and increase the inclusion of heavy metals it is possible to process waste with an even lower calorific value. The trials were not pre-sorted and shredded for the trials. In any case, it would make sense to separate certain fractions such as metals.

Something has to be considered especially. It is possible with the inventive method, for example foreign slag, that is slag from incineration plants in which melting is not possible, or fly dusts, ashes from other plants, in short foreign substances, to be melted in the same process. The melting reactor, which is supposed to melt foreign slag, ash, dusts and the like and which is operated with waste as an energy source, must of course be supplied with the necessary amount of energy for its maintenance, but preferably in the form of waste.

The foreign matter application and melting was tested on the basis of a recirculation task. After domestic waste slag was melted down alone during a test and this test gave positive results, the melting of filter dusts from the electrostatic precipitator of the plant into the slag was examined in a further investigation. An addition of residues from the flue gas cleaning (filter cake) was initially avoided. However, it is possible to process such residues in the reactor according to the invention. It is assumed that if the most significant proportion of heavy metals that occur during waste incineration can be smelted into slag permanently (the scale for this is, for example, an eluate test), this relieves all of the decks intended for this purpose ponia and their capacities. One could proceed to disposing of polluting substances by melting them down according to the invention by incorporating them in slag. The filter dust was added as recirculate via a specially made, water-cooled lock construction, which was attached close to the rotary tube (feed point 6, FIG. 1). The filter dust was introduced into the system in batches. During a certain period, an average of about 10%, later 20% of the amount of waste given during the main test was put into the plant and melted down (see FIG. 3).

During the test, the waste load in front of the electrostatic precipitator increased slightly due to an excessive waste task. Even if, which is unlikely, the entire increase in the dust concentration in the flue gas could be attributed to the recirculate, depending on the temperature, at least 91% of the recirculate was incorporated into the molten slag. This corresponds to approx. 82 kg to 182 kg filter dust per ton of incinerated waste. On the other hand, there is an "own" dust accumulation when burning one ton of waste of approx. 33 kg, which corresponds to approximately 3%. In other words, considerable quantities of toxic waste, which originates from other plants and had to be deposited under expensive conditions, can additionally be disposed of with the aid of the melting process according to the invention with the help of waste. FIG. 6 roughly shows the composition of the amount of residual material when 1 ton of waste is incinerated.

Regarding the question of pollutant emissions in the method according to the invention, the following can be carried out: Several samples of rubbish slag melted in this method with and without addition of recirculate or. with and without the addition of filter dust were tested with an eluate test (CH-TVA test). The molten rubbish slag without recirculation added not only fulfilled the eluate test according to the TVA for an inert substance; it also has a loss on ignition of only <0.1%. All declared highly harmful hydrocarbon compounds such as dioxins, furans etc. are below the detection border. The evaluations show that the TVA limit values for inert substances (eluate test) of all examined samples were not exceeded. The TVA limit values for inert substances were not exceeded in both eluates (Test 1 and Test 2). The slag thus fulfills the requirements of the regulation with regard to the tested parameters.

During the test with the addition of filter dust, the concentration of the most important exhaust gas emitters was determined in addition to the regular measurements on the system in addition to the temperatures and moisture contents.

The dust concentration in the raw gas after the boiler, which in normal operation is in the middle of the usual range, increased somewhat during the test phase. This is due to an increased waste task due to poor control options. The clean gas, on the other hand, meets the requirements of the TVA of the 17th BImSchV.

The nitrogen oxide or NOx emissions during the test with filter dust additives were 2.5 times lower than in normal operation and below the regulation in Switzerland. The average daily value reached was approx. 141 mg / m ³ _n based on 11% 0 ₂ . The sulfur oxide or SOx concentration in the clean gas rose during the experiment. This is probably due to the temperature-related decomposition of metal sulfates.

The method according to the invention discussed here offers the possibility of melting slags, ashes and fly dusts without the supply of energy from the outside. As the eluate tests show, heavy metal compounds are practically insoluble in the slag. The molten slag also has a very low loss of ignition, and the dioxin values are not below the detection limits. In contrast to other processes, the melt does not only take place without external energy supply; it is even expected to be more efficient than conventional incinerators. The system offers the possibility of discharging waste incineration residues in an environmentally friendly manner and reducing the costs of disposal.

The diagram in FIG. 2 shows the temperature profile measured in the test in the reactor. The low temperature range from 600 ° C to 1000 ° C of the generator and the high temperature range from 1000 ° C to 1400 ° C of the rotary tube can be seen. In the afterburning chamber and the idle draft, the temperature control is reduced to lower temperatures in order to lower it completely in a subsequent boiler group for the purpose of heat recuperation and recirculation. The solid line shows the thermal course of a theoretical (ideal) combustion and the dashed line shows the temperature course of the system in standard operation. The course shown with dots shows the melting operation.

Furthermore, two flow diagrams are shown in FIGS. 3 and 4, which, based on the process, essentially show the mass flow and the associated energy flow. It is clear that these diagrams with absolute numbers indicate a very specific course and composition, which depends on the plant and combustion material, but essentially show the effectiveness of the method according to the invention. Discussion:

The reactor presented here essentially consists of a combination of a closed gas generation generator 2 with a mechanical feed grate 3 and a downstream rotary kiln 7 and a plurality of process-engaging connections (for example additions, recirculation etc.). The usual flue gas cleaners and a device for discharging the liquid slag are connected downstream. From these modules, process-engaging returns (feedbacks) lead back to the generator / rotary tube group.

According to FIG. 1, the process path begins at entry 1, into which solid and liquid waste RG, additives AD, recycled rust diarrhea RD and foreign matter FR (for example slag from other domestic waste incineration plants for melting) are introduced. These substances reach the moving grate 3, where they are smeared but not gasified with the addition of other substances such as rust air RL, vapors BR, smoldering air VL, foreign substances FR and oxygen-containing gases 02. This is achieved by blowing in a substoichiometric amount of rust air RL very slowly after being heated by the grate. Recirculated flue gas RR, vapor BR and smoldering air VL can be added through a plurality of air nozzles 4. By means of two further addition devices 5, 6, namely a feed device for solids 5, for introducing solid residues of boiler ash KA, filter dust FS and foreign matter FR, and an addition device 6 for introducing a preheated gas / air mixture VV from the area of the collecting hood 8 above the Rotary tube, vapors BR, combustion air (better gasification or smoldering air) VL, and oxygen-containing gas 02, air, for example, to be added. In this system, no additional energy supply is required for the actual process in addition to that from the solid waste, the air supply and for the drive units. Via the additional feed device 5, the solid residues boiler ash KA and filter dusts FS as recirculation RZ or from domestic waste incineration plants as foreign matter FR can be added to the plant close to the rotary tube and melted with the residues of the generator. Such foreign substances and residues, as already mentioned above, can also be added as dietary fiber for the targeted change in the composition of the carbonization material as soon as it is introduced. By melting the residues and the recirculate, as well as the foreign substances FR, an immobilization of their pollutants, in particular the heavy metals, is achieved. For this purpose, the A ¹ '-.. "Tung on the side walls of the Genera¬ tors addition points 4 for feeding \> .. combustion air VL, vapors BR or recirculated flue gas RR In the area of transition from the grate firing capture zone to the rotary tube is a plant 6 is provided, which is used to add a preheated gas / air mixture from the area of a (provided) hood 8 above the rotary tube, and of combustion air VL, vapor BR or oxygen 02. In addition, afterburner 9 is after the rotary tube a further system 10 for adding combustion air VL or vapors BR is provided, as well as minimizing the heat losses, in particular in the rotary tube operated with negative pressure, which practically always has leaks, with the consequent and targeted return of unprocessed , Energy-containing substances and thermal energy, a very high process yield can be achieved.

In the area of the transition from the generator to the rotary tube, boiler 5 KA and filter dusts FS from the company's own plant or from external incineration plants FR can also be added via the device 5. An addition is advisable at this point so that the dust does not from the generator air guided through the grate are immediately discharged into the flue gas.

The preheated and partially degassed solid residues of the generator get into the rotary tube. The air VL, 02 introduced in the area of the transition from the generator to the rotary tube causes the generator gases to burn in the rotary tube. The temperature reached in the rotary tube leads to a complete burnout and to the melting of the solid reaction products, which are melted away from the rotary tube. The melting process destroys all organic compounds at a temperature of 1300 ° C - 1400 ° C and heavy metals are permanently integrated into the glass structure of the slag. The glazed slag only releases little of the bound heavy metals on the surface.

In the afterburning chamber 9 behind the rotary tube, there can be a supply of combustion air VL or vapors. The combustion air leads to the final combustion of the combustible substances of the flue gas as well as the temperature control of the flue gases. Thermal energy can be obtained from the boiler group 11 after the afterburning chamber by utilizing the energy content of the flue gases in the form of steam (electricity) and district heating.

Most of the known slag and residue melting processes require an energy supply from outside, for example by means of fossil fuels or by electricity. This is not necessary in the process according to the invention. Due to the special structure and the special air flow of the plant, the energy content of the solid waste is completely sufficient for the reaction products of the generator and the other residues, which are also added will melt down. In comparison to conventional domestic waste incineration plants without molten slag, less, but more energy is dissipated for other purposes (such as electrical energy, district heating). But above all a noteworthy circumstance comes to the fore here: The energy for the melting comes from waste that should have been burned one way or the other and would have produced slag and residual materials, and the process according to the invention not only melts its own slag and residues, but still has the capacity to process foreign matter.

Since it is a very inhomogeneous mixture of household waste and household-like waste, which constitute the largest part of the feed of this facility, the described reaction sequences in the generator cannot be delimited spatially. The supply of the different gases at the various points should be adapted as best as possible to match the different calorific values of the feed material and its composition.

FIG. 2 now shows the approximate temperature profile of the process in the reactor. The process begins with task 1, where the temperature is still that of the environment. Seen in the process direction, in the generator at the beginning of the grate, the temperature is a few 100 ° C and increases with increasing swelling (gasification) at the end of the grate to about 1000 ° C, but without forming significant heat spots or hot spots. The temperature of the swelling is controlled by the targeted addition of rust air RL under the grate and by the addition of vapors BR and / or smoldering air VL. At the beginning of the rotary tube, in which the burnout and slag liquefaction take place, the temperature rises quickly through ignition of the carbonization gases to the high temperature range between 1200 ° C and 140Q ° C. Burning out and melting take place at this temperature. At the transition point to the afterburner chamber, the temperature remains essentially the same due to the action of further supplied combustion air and then gradually drops again in the direction of the low temperature range to 1100 ° C. by the targeted addition of further (cooling) combustion air VL and / or vapors BR. The flue gases are cooled to 200 ° C. in the boiler 11.

It can be seen from this diagram that the very high temperatures above 1000 ° C. at which the slag begins to melt and at which parts of the plant which are not designed for this temperature begin to take damage, for example from the grate into a rotary tube designed for these temperatures ¬ oven. These high temperatures at the suitable location, which can only be achieved in a targeted manner by the process according to the invention, are delegated, so to speak, in the rotary kiln which can be better designed for high temperatures. By delegation is meant not only the combustion at another location but also the transfer of the energy sources to this location. Here it is combustible gases which result from the charring on the grate and which, together with the still combustible but degassed residues, now enable the desired high temperatures in the rotary tube. The substoichiometric charring is largely or completely supported by recuperated, recirculated thermal energy from the area of the rotary kiln (house 8).

FIG. 3 shows a diagram for the addition of filter dust within the test series, which was briefly discussed above. For a little over two hours, the fractions were added in two proportions: initially about 10% based on the amount of rubbish, then about 20%. With automated addition, the task can be staggered in finer steps. FIG. 4 shows, in the form of a pie chart according to Vehlow, an exemplary composition of the residues from a ton of waste. This composition is of course largely dependent on the initial composition of the waste. It denotes: A = burned and evaporated portion; B = rust discharge; C = RGR residues, salts; D = filter dust; E = kettle ash; F = rust diarrhea.

Claims

PATENT CLAIMS

1. A process for melting residues into slag, characterized in that waste materials are used as the energy source and the thermal material conversion process is divided into a low-temperature process (smoldering process) and a subsequent high-temperature process (combustion process), the low-temperature process (smoldering process ) combustible gases obtained are fed to the high-temperature process (combustion process).

10

A method according to claim 1, characterized in that the low-temperature process is a substoichiometric process of entangling on a combustion grate with a substoichiometric amount of grate air which is forced through the material to be burned as a downwind with little pressure, or by means of underpressure above the grate through the Is consumed.

3. The method according to claim 1, characterized in that the Hoch¬ temperature process is a combustion process in which residues 20 from the carbonization are burned together with carbonization gases with the addition of combustion air in order to reach the melting temperature of slag and the liquefied slag from the To be able to branch off the process.

25th

4. The method according to any one of claims 1 to 3, characterized gekennzeich¬ net that the high temperature process is a post-combustion process with the supply of combustion air.

5

5. The method according to claims 2 or 3, characterized in that foreign substances for melting in slag are fed to the low-temperature process or the high-temperature process.

10

A method according to claim 5, characterized in that the foreign substances are recirculates or come from third-party plants and that they are either introduced into the charring process as fiber or are fed directly to the high-temperature process. 15

7. The method according to claim 2, characterized in that heat energy which is released in process steps which follow the process of the melting process is returned to the same. 20th

A method according to claim 7, characterized in that to support the low-temperature process waste heat from the high-temperature process (combustion process) is fed to the low-temperature process (charring process) for heating the material to be converted.

9. The method according to claim 2, characterized in that combustion air for maintaining the combustion of in the high-temperature The carbonization gases passed through the equipment are mixed upstream of the high-temperature part, where the mixture is ignited.

10. The method according to claim 4, characterized in that combustion air 5 is introduced into an afterburning area in order to burn out the combustible residual gases from the flue gas.

11. The method according to any one of claims 4 or 10, characterized in that an excess amount of combustion air or vapor is introduced into the afterburning area for temperature control (cooling).

15

12. The method according to any one of claims 2 or 3, characterized gekennzeich¬ net that vapors are introduced to control the process in the phase of Ver¬ smoldering and / or in the post-combustion phase.

20th

13. The method according to any one of claims 1 to 12, characterized in that air (VL), vapors (BR) from the sewage sludge combustion for nitrogen oxide reduction and / or recirculated flue gases are added via nozzles on the side walls of the generator. 25

14. The method according to any one of claims 1 to 12, characterized gekennzeich¬ net that via a special feed device (5) addition of boiler ash and filter dust from the own process and from 30 external processes, in particular domestic waste incineration plants. is seen, on the one hand, to melt them together with the solid reaction products of the generator and, on the other hand, to use them as ballast material for regulating the process.

15. The method according to any one of claims 1 to 5, characterized gekennzeich¬ net that an addition of air (VL) and vapors (BR) can take place in the afterburning zone between the rotary tube and the boiler in order to achieve afterburning and temperature control of the flue gases ¬ chen. 10

16. The method according to any one of claims 1 to 15, characterized gekennzeich¬ net that gas is generated in a generator, which is heated in a downstream rotary tube by supplying air to about 1400 ° C 15 and on the other hand the garbage on the grate the degassing is preheated to approx. 1000 ° C. at the transition to the rotary tube before this slag mixed with foreign substances is melted in the rotary tube by burning the carbonization gases.

20th

17. Device for melting combustion residues such as slag, ash and the like, characterized in that it consists of a low-temperature section (carbonization generator) and a downstream high-temperature section (rotary kiln) 25, in which low-temperature section (carbonization generator) the combustible substances in combustible gases and combustible residues are implemented in order to support a combustion process in the high-temperature section (rotary kiln) with the combustible gases, so that the slag becomes molten and means for recycling waste heat from the high-temperature section. -? ^* - »-

are provided in the low-temperature section to support the implementation of the combustible substances.

18. The apparatus according to claim 17, characterized in that the low-temperature section consists of a carbonization generator which has a conveyor grate on which the process material is carbonized substoichiometrically and that it has feeds for adding process materials controlling the carbonization.

10

19. The apparatus according to claim 17, characterized in that the

High-temperature section consists of a rotary kiln, at the entrance of which means for adding combustion air and foreign substances and at the exit of which means for withdrawing liquid slag 15 are provided.

20. The apparatus according to claim 17, characterized in that the

High temperature part is an afterburning chamber with feeders for 20 means for controlling the burning out and / or cooling of the flue gas.

21. The apparatus according to claim 17 to 20, characterized in that 25 of the reactor has recirculations for heat energy and solid materials from the process in order to enable a recirculation of energy and residual materials.

30th

22. Device according to one of claims 17 to 21, characterized gekenn¬ characterized in that the rotary kiln (7) and the afterburning chamber is followed by a boiler (11) to make the heat content of the flue gases usable in the carbonization process if necessary.

5

10