DE3507465A1 - Process for waste incineration - Google Patents

Abstract

In a process for the incineration of waste materials, in particular refuse, the waste materials being dried in a first process step in a drying stage, dryer waste gas arising, and being incinerated in a second process step in an incineration stage, furnace waste gas arising, it is proposed that a part of the furnace waste gas from the incineration stage and a part of the dryer waste gas from the drying stage are in each case branched off and mixed to give a first mixed gas, and that the first mixed gas is recycled to the drying stage and used for drying the waste materials, and that the remaining part of the furnace waste gas is mixed with the remaining part of the dryer waste gas to give a second mixed gas whose utilisable calorific content is used for generating useful energy.

Description

Process for incinerating waste materials

The invention relates to a method for incinerating waste materials, in particular of garbage, with the waste materials in a first process step be dried in a drying stage, with dryer exhaust gas, and in a second process step are burned in a burning stage, furnace exhaust gas accrues.

The economic elimination of waste materials, such as in particular Garbage, presents a difficult problem. This is especially true when such waste materials can be disposed of in conventional waste incineration plants. These are mostly with Grate furnaces which have to be operated with a large excess of air, to ensure an almost complete combustion.

For example, there are excess air numbers in such grate firing systems from 1.8 to 2.2 common. This has significant disadvantages, among other things in that such operated furnaces large amounts of flue gas with relatively little Release temperature, for example 800 OC. The efficiency of one in the exhaust side Flue gas flow switched device for generating useful energy, for example for steam or electricity generation, is relatively low as a result. Furthermore, condition large amounts of flue gas large and therefore costly exhaust gas cleaning systems.

As a result of material inhomogeneity and different calorific values the waste and the difficulty of swirling it through the grate furnace to keep it sufficient Bringing into contact with combustion air, there are zones in the furnace in which for example a firing temperature of less than 800 OC is reached and / or There is a lack of oxygen. This situation is especially true during such periods critical, where relatively moist and / or low calorific waste is used comes. This creates uncontrollable areas of incomplete combustion in the furnace, which is preferred in the presence of chlorine and / or aromatic Basic bodies (for example made of chlorine-containing plastics, ligninsulphonic acids, pentachlorophenol, polychlorinated biphenyls, etc.) present in the waste, polychlorinated dibenzodioxins and / or form dibenzofurans, in particular TCDD and TCDF. In particular the dioxins are still very stable even at temperatures of 1000 OC, so that they can be used in a grate incineration plant not disintegrate. There were already dioxin levels in the fly ash and in the clean gas dust various garbage incineration plants detected (Die Zeit ", 02.03.1984 Dioxin, the avenger from the retort ").

The extreme toxicity of dioxins is well known (Bild der Wissenschaft ", Nov. 1984, pp. 64-76). Conventional waste incineration is thus generally in Questioned (Chemical Engineering, June 6, 1983, pp. 20 to 64).

Theoretically, dioxins that are produced during combustion could be Bring it back to disintegration by adding an afterburning stage to conventional waste incineration downstream with a furnace temperature of at least 1200 OC. That would however, require increased investment and the use of conventional fuels and would consequently involve an uneconomical hone in costs tied together.

The combustion at relatively low temperatures continues to have the Disadvantage that only a small part of the heavy metals or heavy metal compounds of the waste is volatilized. The rest is carried out with the slag, which the Utilization of this slag for road construction and similar fields of application in question represents.

As a result, conventional waste incineration plants are more modern Knowledge on the one hand uneconomical and on the other hand due to the emission of highly toxic organic compounds as well as because of the resulting non-leaching-resistant Ashes that contain toxins that are soluble in groundwater, because of the resulting effects no longer responsible for unsustainable environmental pollution.

In order to overcome the difficulties identified, it has already been suggested that Household waste, for example, in the production of Portland cement clinker in the The combustion zone of the clinker kiln, where the temperature is high, should be introduced and to burn in it, and the ashes from the garbage melt into the cement clinker add (DE-AS 23 38 318).

Obviously, one needs to do a cement burning process in this way Waste or rubbish contributed as additional fuel carefully and consequently relatively expensive processing. Furthermore, there is a coupling of waste incineration and production of cement clinker limits and difficulties.

It must be ensured that the garbage the quality of the Firing product Portland cement does not affect it, and it can only ever be a relatively minor one Amount of garbage added and burned in relation to clinker production will. A flexible adaptation of the disposal of garbage to the accumulation of garbage is therefore not possible, especially since cement firing systems are not available in many places stand.

In addition, fluctuations in the composition of the waste, in particular with regard to its calorific value, as a result of the proportions of water contained therein on the one hand and flammable substances on the other hand, lead to considerable difficulties in terms of controllability the burning process.

Disposal of waste by incineration in cement production there are therefore narrow limits.

Next is a method for the combined incineration of garbage and Sludge known, in which the hot exhaust gases resulting from waste incineration a sludge drying device, preferably a sludge drying drum, fed in and in this in cocurrent with the sludge through the drying drum are performed, the sludge up to a water content that allows combustion pre-dried and then fed to the incineration. This is done under Use of your own calorific value in a deck oven. According to one in the pre-release A maximum gas temperature of 800 OC reached (DE-OS 17 51 233).

A similar process for the combined drying and burning of Waste materials can also be found in US Pat. No. 2,177,487.

The disadvantage here are on the one hand those caused by the use of deck ovens high investment costs in relation to the amount of waste collected and operating costs, and on the other hand those for thermal decomposition of toxic ones organic compounds inadequate combustion and exhaust gas temperatures.

The invention is based on the object of specifying a method which has the following improved properties compared to the prior art shown has: a) It should be significantly cheaper in terms of thermal technology, b) the emission of odorous compounds should be avoided, c) the Waste incineration should take place at high temperatures to avoid the emission of toxic organic compounds, especially of dioxins, should be avoided, d) slag should be discharged molten from the firing stage, and thus more resistant to leaching Form that can also be re-used, for example, as a building material or as Cement clinker addition does not exclude e) exhaust gas from the combustion stage should be in as possible small amount and at the highest possible temperatures, on the one hand to a to enable economic generation of useful energy from waste heat, and on the other hand to keep the costs of aie exhaust gas cleaning as low as possible, f) a flexible adaptation of the process to different calorific values as a result of different Condition and especially different water and fuel content The waste materials should be possible without any problems, g) the process should be uncomplicated uno be easily controllable.

The task at hand is achieved with a method of type mentioned at the beginning with aer invention in that each one Part of the furnace gas from the burning stage and part of the dryer waste gas from the drying stage is branched off and are mixed into a first mixed gas, and that the first mixed gas for the drying stage recycled and used to dry the waste, and the remainder Part of the furnace exhaust gas is mixed with the remaining part of the dryer exhaust gas to form a second mixed gas and that its heat content is used to generate useful energy.

The method according to the invention has a number of advantages: a) By drying the waste materials, their calorific value is increased and consequently increased the firing temperature, b) the dried waste is more easily ignitable and thus more easily burned out, as a result of which the combustion can take place with only a little Excess air can be operated at high firing temperatures, c) exhaust gas from the firing stage is on the one hand reduced by the amount of water vapor and on the other hand falls during operation of the burning stage in the stoichiometric best point in terms of quantity at the theoretically lowest Limit on, d) the firing temperature of at least 1200 OC is sufficient, to break down organic and especially toxic compounds into their elementary components to be thermally disassembled and thus rendered harmless, e) because it comes from the gas cycle The dryer exhaust gas discharged from the drying stage with the very hot furnace exhaust gas to the second Mixed gas is mixed, such high temperatures are reached in this mixed gas that oass the odor-causing components in the exhaust gas are thermally destroyed, f) the profitability of generating useful energy from waste heat is improved, g) the final cleaning of the exhaust gas, which has been reduced to approximately the theoretical minimum amount is made possible more cost-effectively.

One embodiment provides that the dryer exhaust gas in a Separation stage of entrained, non-gaseous substances is separated and the separated Substances are added to the waste to be incinerated.

Another embodiment of the method advantageously provides that the heat content of the second mixed gas in two stages to generate useful energy is used, whereby in a first stage, at a relatively high temperature level, For example, steam or mechanical or electrical energy obtained and in one second stage useful heat to a heat transfer medium at a relatively low temperature level is delivered.

This can be done, for example, in the manner of warmth of the second mixed gas is used in the first stage by means of a hot gas urine to generate mechanical or electrical energy.

In the second waste heat recovery stage, a usable Remaining heat of the second mixed gas is used to make combustion air for the combustion stage to warm up. As is well known, heated combustion air has the advantage that the combustion temperature Nearest values are reached in the firing stage, preferably temperatures in the range of or over 1200 ° C.

In this way, the usable heat content can be used of the second mixed gas with high thermal efficiency.

To cover the need for thermal energy for the required drying performance the drying stage is the first mixed gas between 40 and 80 percent by volume, occasionally between 55 and 70 percent by volume of the drying exhaust gas, and between 5 and 40 percent by volume, preferably between 10 and 20 percent by volume supplied to the furnace exhaust gas.

A setting which is provided here as being essential to the invention The proportions of these gases in the case of the first mixed gas enable an operating mode the drying stage in each case at the best point in flexible adjustment to throughput, condition and in particular moisture of the waste materials.

It is advantageously provided for this that the ratio of the first Mixed gas supplied dryer aogas to the kiln exhaust gas amount according to aer temperature aes first mixed gas is set.

In the case of an almost even load on the drying stage With this uncomplicated control process, a consistently good drying performance can be achieved be provided. Conversely, there can be flexibility in the performance of the drying stage can be achieved with an advantageous and uncomplicated method of regulation by, that the temperature of the first mixed gas in accordance with the required power the drying stage, that is, according to the amount of waste material that has passed through and their average water content per kg of wet waste.

And finally, an advantageous regulation of the drying stage also be made so that the temperature of the first mixed gas - ourch tinslelluny the proportions of dryer exhaust gas and ufen exhaust gas - according to the temperature of the dryer exhaust gas is set at the exit of the drying stage.

Provided that the drying performance is almost permanent In the drying stage, an operational equilibrium of the parameters can be advantageous can be achieved very easily in that the drying stage with constant set temperature of either the mixed gas at the inlet or the dryer exhaust gas is operated at the output.

In any case, one or the other type of regulation serves the purpose of in adaptation to the power requirement of the drying stage according to the quantity, Type and humidity of the waste materials, to drive them at the best point and a pre-dried one and to deliver loosened firing material.

Achieving this goal is a prerequisite for those in coupling operated drying and firing stages to ensure proper Ausrana oer ADfallsioffe with the lowest possible excess of air at high firing temperatures and without use to achieve high-quality foreign fuels.

In this way it is possible with the method, the firing by a to operate the controlled drying process so intensively that a guarantee for the complete destruction of toxic organic compounds in the exhaust gas, in the dust of the Exhaust gas, and in the residues of the furnace on the part of the company and given can actually be complied with.

It is also provided that the waste materials are crushed prior to drying will.

This opens you up better, while drying it more intensively, are more likely to ignite and, as a result, burn out better.

The dried waste is advantageously disposed of immediately after it has been dried and preferably while maintaining its tactile quality achieved as a result of drying Heat content supplied to the combustion.

On the one hand, a loosening of the Adfallstoffe both in the drying stage as well as in the burning stage is further provided with the invention, that a drying drum is preferably built in to dry the waste materials Lifting and dividing means and a rotary kiln for incinerating the waste materials is used.

Both units result from their overturning movements and in particular in conjunction with built-in lifting equipment, optimum loosening and movement of waste materials resulting in the best possible surface contact between Solid and drying or fuel gas, and enable them through their simplicity and controllability, for example the speed of rotation, the respective setting optimal operating conditions. The throughput is also in relation to the investment costs these units are economically very favorable.

It is advantageous for additional chemical or adsorptive bonding of pollutants provided that the incineration of waste materials with the addition of calcareous minerals, preferably in the form of rock flour will.

Especially with relatively moist and / or low-calorific waste it is advantageous to use the air for the incineration of the waste, for example through indirect heat exchange with the second mixed gas to preheat such waste to be able to burn at high temperatures.

Finally, it is envisaged that the ashes of the firing stage will be molten is carried out in a water bao. Advantageously, the slag falls in a more resistant to leaching Shape and can either be safely deposited or used economically, for example as a building material surcharge, for example for black ceiling mix, or as a surcharge when grinding clinker to ready-to-use cement, or for similar purposes.

The invention is explained below with its advantages based on an im Block circuit diagram shown embodiment as well as based on heat calculations explained in more detail.

The block diagram shows a drying stage 1 and a firing stage 2. Garbage is fed to drying stage 1 at 3 and dried therein. Dried Garbage is given up according to the line 4 of the burning stage 2.

This carries out molten slag as a combustion product at 5.

Drying gas is drawn off on the discharge side of drying stage 1 and after the separation of non-gaseous substances in a separation stage 39 with the line 6 partially returned to the feed side 7 of the drying stage 1 and with it Exhaust gas of the combustion stage 2 from line 8 is mixed to form the first mixed gas 9 and as Drying gas introduced into drying stage 1. From the dryer exhaust gas in the separation stage 39 separated non-gaseous substances are fed to the firing stage 2 una aarin incinerated along with the rest of the waste. There is a system gas in the circuit a fan 27 switched on, which the pressure energy required for the gas transport supplies.

Combustion air is fed to combustion stage 2 via line 10. Included it can be cold fresh air from the Line 10 'or around warmed Act air from aer line 11. In the system of gas guides can be adjustable Throttle elements 14 to 18 can be provided, through which the quantity and / or mixing ratios the gas flows can be adjusted to each other.

An advantageous regulation of the system is also with the fans 27 and 38 possible, as well as with the adjustable throttling devices 15 and 16.

A control device provided for this purpose, which is responsible for the implementation the control method steps according to the invention is used, comprises at least two Temperaturmeßstellen, namely one at 29 for determining the temperature of the first mixed gas 9, and another at 30 for determining the dryer exhaust gas temperature. Signal lines 31 and 32 lead from these to a control and comparator unit 33, which connects the corresponding temperature-compliant electrical signals will. This unit 33 compares the actual temperature values with the target values, that of the comparator unit from the setpoint input unit 34 to the signal line 35 can be activated. If the TARGET / ACTUAL values are not equal, the Computer unit 38 calculates a correction pulse and uses the control lines 36 and 37 causes an adjusting movement of the throttle elements 15 and 28. These will, preferably with delay damping, adjusted until they are equal the TARGET / ACTUAL values have been reached and the actuating impulses have decayed towards zero.

Of course for the person skilled in the art, the control device can also nor to adjust further throttle elements 14, 16, 17, 18 and / or for example to the Influencing the speed of the system fan 27 expanded are deemed necessary on a case-by-case basis based on professional judgment should be.

The exhaust gas of the combustion stage 2 is discharged via line 19 and after mixing with the part of the dryer exhaust gases that did not lead to the first mixed gas are mixed to a second mixed gas.

This is, for example, a two-stage process for generating useful energy Heat transfer device 21 and 22 supplied and then via a gas cleaning device 23, for example a flue gas scrubber and a dust extractor, into the atmosphere discharged. In the first heat transfer device 21, an essential part the usable heat of the second mixed gas at a relatively high temperature level, for Example around 900 OC, used, for example, a purely schematic To operate exhaust gas turbine 25 and generate electricity with this via a generator 24. A cooler 26 arranged in the circuit of the exhaust gas turbine 25 can also be used can still be used for hot water preparation.

That used in the heat transfer device 21 for thermal purposes una aaDei, the temperature-reduced second mixed gas enters the recuperator 22, in which air is heated by renewed heat exchange and used as warm combustion air with the pipe 11 of the firing stage 2 is fed.

The following is a numerical example to estimate the order of magnitude of the amount and temperatures of the gas flows when using household waste Invention submitted.

The invoice is based on the following information: - lower calorific value Garbage 2000 kcal / kgM (M = wet garbage) - garbage moisture content 30% - heat consumption for 800 kcal / kg H20 drying (including losses) - dryer exhaust gas temperature 150 ° C excess air of combustion 20% - combustion heat losses 10% - furnace exhaust gas temperature 1200 ° C Cp Kiln exhaust gas 0.4 Kcal / Nm3 0C This results in: 1.) Heat consumption for drying of waste = 0.30 x 800 = 240 kcal / kgM This energy must be taken from the burning stage will.

2.) This requires a removal of the 1200 ° C hot gas from the firing stage of 240 kcal / kgM 0.4 kcal / Nm. UC x (1200 - 150 OC) = 0.57 Nm3 / kgM 3.) The amount of exhaust gas The following can be estimated from the combustion stage: The amount of flue gas during combustion of moist garbage is at a calorific value of 2000 kcal / kgM and an excess of air from experience of 20% about 4.20 Nm3 / kgM. However, 30% moisture will already be discharged in the drying stage.

With a specific weight of the water vapor of 0.768 kg / Nm aas specific volume 0.3 / 0.768 = 0.39 Nm3 / kgM. When the Garbage in the dryer is therefore with an actual amount of flue gas from the burning stage from 4.20 - 0.39 = 3.81 Nm3 / kgM to be calculated.

The amount of flue gas from the firing stage, including in the drying stage conduct, corresponds to 0.57 / 3.81 = 15% of the total amount of flue gas (see claims 8 and 9).

4.) In the incineration of waste and assumed heat losses (Slag heat and wall losses) of 10 X results in a temperature of the exhaust gases the firing level of about: 2000 0.10) = 1180 OC; 0.4 x 3.81 This roughly corresponds to the initial value of 1200 OC assumed above, 5.) Moves the drying stage to Example with an exhaust gas amount of 3 Nm3 / kgM, 10% of which, i.e. 0.3 Nm3 / kgMmit False air would have to be estimated and 0.39 Nm / kgM come from the water vapor, so would be the following subsets of the dryer exhaust gas with exhaust gas from the combustion stage to the second Mixing mixed gas: 0.57 + 0.3 + 0.39 = 1.26 Nm3 / kgM.

6.) The remaining amount, i.e. 3.00 - 1.26 = 1.74 Nm3 / kgM, is with the 0.57 Nm / kgM partial exhaust gas of the combustion stage is mixed to form the first mixed gas and in aie Returned to the drying stage. The result is an amount of the first mixed gas of 0.57 + 1.74 = 2.31 Nm3 / kgM with a temperature of about 1200 x 0.4 x 0.57 + 150 x 1.74 x 0.36 = 420 OC.

(0.57 + 1.74) 0.38 7.) When completely dry, place in the dryer an amount of water of 0.39 Nm3 / kgM is removed. In a state of equilibrium this must The amount of water vapor can be completely removed with the partial amount of the dryer exhaust gases, which leads to the second mixed gas. Since this is 1.26 Nm / kgM, the water vapor content corresponds of the dryer exhaust gas 0.39 / 1.26 = 31 X (in reality it is a bit higher, there too the exhaust gases from the combustion, which are fed into the drying stage, water contained as combustion product).

8.) The exhaust gases discharged from the drying stage are combined with the remaining Combined exhaust gases from the combustion stage to form the second mixed gas. It turns out a lot from 1.26 + 3.81 - 0.57 = 4.5 Nm3kgM at a temperature of about: 1200 x 0.4 x (3.81 - 0.57) + 150 x 0.36 x 1.26 (1.26 + 3.81 - 0.57) 0.39 = 925 ° C 9.) The variable in the above calculation is the assumed amount of exhaust gas from the dryer: If you put other dryer exhaust gas quantities under otherwise identical conditions and leads to the Using the same calculation as before, the following table of values is obtained: A) Dryer exhaust gas quantity (Nm3 / kaM): 1.5; 2.0; 3.0; 4.0; 5.0; B) Partial amount of dryer exhaust gas to the second Mischaas (Nm) / kgM): 1.11; 1.16; 1.26; 1.36; 1.46; C) Partial amount of dryer exhaust gas for the first Mischaas (Nmi / kgM): 0.39; 0.84; 1.74; 2.64; 3.54; D) C / A (S): 26.0; 42.0; 58.0; 66.0; 70.8; E) Temperature of first mixed gas (° C) 787; 588; 419; 346; 306; F) temperature second Mixed gas (oC) 952; 943; 925; 908; 891; G) Water vapor content dryer exhaust gas (%) 35.1; 33.6; 31.0; 28.7; 26.7; x x x x x +) Temperature assumed to be 150 OC in each case the end From the invoices it can be concluded that the system is advantageous when using household waste the dryer stage must be operated with at least 2.0 or 3.0 Nm³ / kgM exhaust gas quantity, otherwise the temperature of the first mixed gas assumes an undesirable order of magnitude. As a result, it is appropriate to design the system for 3.0 to 5.0 Nm3 / kgM.

The high combustion temperature of around 1200 OC arises in all So that no polychlorinated hydrocarbons can form, or possibly existing toxic organic compounds are decomposed.

The first mixed gas is always at temperatures of over 800 OC, so that the decomposition of odorous compounds that can arise during drying is guaranteed. For waste with less It is recommended to use the combustion air for calorific value and / or higher moisture contents preheat in order to maintain these advantageous temperature conditions.

From the dependence of the temperature of the first mixed gas on the Relative composition of dryer exhaust gas and kiln exhaust gas flows the advantageous effectiveness of the provided with the method according to the invention Measures for regulation according to those provided in claims 10 to 14 Characteristics.

The invention thus optimally fulfills the task Requirements listed at the beginning.

- Empty term -

Claims (22)

Method for incinerating waste materials, in particular of garbage, the waste materials in a first process step in a drying stage are dried, whereby dryer exhaust gas is produced, and in a second process step are burned in a firing stage, whereby furnace exhaust gas is produced, characterized in that that in each case a part of the furnace gas from the firing stage and a part of the dryer exhaust gas from the drying stage branched off and mixed into a first mixed gas, and that the first mixed gas returned to the drying stage and used to dry the waste materials, * and that the remaining part of the furnace exhaust gas with the remaining part of the dryer exhaust gas to one second mixed gas is mixed, and that its usable heat content for extraction is used by useful energy. 2. The method according to claim 1, characterized in that the dryer exhaust gas is separated from entrained, non-gaseous substances in a separation stage and the separated materials are added to the waste to be incinerated. 3. The method according to claim 1 and 2, characterized in that the Heat content of the second mixed gas in preferably two stages to obtain Useful energy is used, in a first stage at a relatively high temperature level for example steam or mechanical or electrical energy obtained, una in a second stage at a relatively low temperature level useful heat to a heat transfer medium is delivered. 4. The method according to claim 1 to 3, characterized in that heat of the second mixed gas is used in the first stage, for example by means of a hot gas turbine to generate mechanical or electrical energy. 5. The method according to any one of claims 1 to 4, characterized in that that heat of the second mixed gas is used in the second stage to generate combustion air to heat up for the firing stage. 6. The method according to one or more of claims 1 to 5, characterized characterized in that the first mixed gas is between 40 and 80 percent by volume of the dryer exhaust gas amount are fed. 7. The method according to one or more of claims 1 Dis 5, characterized characterized in that the first mixed gas is between 55 and 70 percent by volume of the dryer exhaust gas amount are fed. 8. The method according to one or more of claims 1 to 5, as a result characterized that the first mixed gas between 5 and 40 volume percent of the furnace exhaust gas amount supplied. 9. The method according to one or more of claims 1 to 5, characterized characterized in that the first mixed gas is between 10 and 20 percent by volume of the amount of furnace gas are fed. 10. The method according to one or more of claims 1 to 9, characterized characterized in that the ratio of the amount of dryer exhaust gas supplied to the first mixed gas adjusted to the furnace exhaust gas quantity in accordance with the temperature of the first mixed gas will. 11. The method according to one or more of claims 1 Dis 10, characterized marked that the temperature of the first mixed gas depends on the required Performance of the drying stage, aas means according to the amount of the Waste materials and their average water content per kg of wet waste will. 12. The method according to one or more of claims 1 to 10, characterized characterized in that the temperature of the first mixed gas in accordance with the temperature of the drying gas is set at the exit of the drying stage. 13. The method according to any one of claims 1 to 12, characterized in that This means that the drying stage with a constant set temperature of the first Mixed gas is operated. 14. The method according to any one of claims 1 to 12, characterized in that oass the drying stage with the same set temperature of the dryer exhaust gas is operated. 15. The method according to one or more of claims 1 to 14, characterized characterized in that a drum dryer is used to dry the waste materials will. 16. The method according to any one of several of claims 1 to 15, characterized characterized in that a rotary kiln is used to incinerate the waste materials wira. 17. The method according to one or more of claims 1 to 16, characterized characterized in that the waste materials are crushed before drying. 18. The method according to one or more of claims 1 to 17, characterized characterized in that the waste materials immediately after their drying and preferably are fed to the combustion while maintaining their sensible heat content. 19. The method according to one or more of claims 1 to 18, characterized characterized that the incineration of waste materials with the addition of calcareous Minerals, preferably in the form of rock meals, are made. 20. The method according to one or more of claims 1 to 19, characterized characterized in that preheated combustion air is used to burn the waste will. 21. The method according to any one of claims 1 to 20, characterized in that that the incineration of the waste is carried out at 1200 ° C or higher temperatures will. 22. The method according to any one of several of claims 1 Dis 21, characterized characterized in that the ashes of the firing stage are discharged in molten form into a water bath will.