EP1261827B1 - Reactor and method for gasifying and/or melting materials - Google Patents

Abstract

A reactor used for gasifying and/or melting feed materials comprises a feed section, a pyrolysis section, gas feed devices, and a melting and super heating section. A reactor comprises a feed section (1) having an opening (2) for the feed materials; a pyrolysis section (8) connected to the preceding section to expand the cross-section so that a debris cone (9) of the feed materials is formed; gas feed devices (10) which open out into the plane of the expanded cross-section in the pyrolysis section and feed hot gases to the debris cone; a melting and super heating section (14) connected to the pyrolysis section; upper feeding devices (15) for introducing an energy-rich medium into the melting and super heating section; a reaction section (20) connected to the melting and super heating section and containing gas suction devices (21) for removing excess gases; a hearth (25) with a tap (27) for collecting and deviating metal melts and slag melts; and lower feeding devices for introducing an energy-rich medium to prevent solidification of the melts. An independent claim is also included for a process for carrying out gasifying and/or melting of feed materials. Preferred Features: A pre-tempering section (5) is arranged between the feed section and the pyrolysis section and has double walls to create a hollow chamber (6) into which a heat transfer medium is fed.

Description

The present invention relates to a reactor and a Process for gasifying and / or melting substances. Especially the invention relates to the material and / or energetic Utilization of any waste, e.g. with predominantly organic components but also of hazardous waste. The reactor according to the invention and the process are suitable but also for gasification and melting of feedstocks any composition or for energy through the use of organic substances.

For some time, solutions for thermal disposal various types of waste and other substances sought. Besides combustion processes are various gasification processes known, which aim primarily to produce results to reach the environment with a lower pollutant load and the expense of treating the feeds though also reduce the gases produced in the process. The However, known methods are complicated and only by a hard-to-control technology, as well as related high disposal costs for the person to be treated Feedstock or the waste labeled.

In DE 43 17 145 C1 is a on the principle of degassing based method of disposal of differently composite Waste materials described. According to the specified Processes are expected dusty gases as recycle gas be deducted completely and subsequently in the Melting and overheating zone burned with oxygen become. This cycle gas guide and the further described Extraction of the excess gas between the recirculation gas suction opening and the melting and overheating zone leads However, as experiments have shown, not to the desired Target, a contaminated with only a few pollutants excess gas to obtain. If the also in this document indicated circulating gas cupola furnace to carry out the Method is used, i.a. the pollution the excess gas so large that the thereby necessary Gas economy for cleaning the excess gas so consuming is that an economic disposal of appropriate Waste materials is no longer possible.

In DE 196 40 497 C2 is a coke-heated recycle gas cupola for the recovery of waste materials. This cycle gas cupola is characterized in that below the funnel an additional gas vent is arranged. The pyrolysis gases withdrawn at this point be via a cycle gas guide in the lower furnace section fed back to cause combustion of the gases there. Since the exhaust zone for the excess gases above the hot zone is arranged, not only excess gases but also sucked off a large proportion of pyrolysis gases, whereby in the gas mixture u.a. difficult to remove Hydrocarbons are included. This will be the subsequent Gas economy extremely complex and the environmental impact is increasing.

In contrast, DE 198 16 864 A1 shows a coke-heated Circulation gas cupola, in which the excess gas suction is arranged below the melting and superheating zone. Although this can increase the quality of the excess gases, because the extracted gases when flowing through the overheating zone are largely reduced, however, leads the spatial Near the overheating zone to very hot excess gases, the subsequently have to be cooled consuming. Problematic is also that it by the chosen arrangement to Ansinterungen of slags and dusts in subsequent components of the downstream Gas way comes. On the other hand, the temperatures are in the hearth area below the gas extraction no longer sufficient high, around the existing metal melts and Slag melts under different conditions of use to keep fluid. The necessary tapping is thereby disturbed or completely impossible.

The solutions known from the above-mentioned prior art always lies the basic principle of the circulation gas guidance for a partial flow of the gases formed, the gases sucked in the upper part of the furnace and in the lower part be fed again. Experts have assumed that that this gas guide also to warm the pillar under Use of the countercurrent principle is necessary. The cycle gas principle bring u.a. the following disadvantages The gases rising in the shaft furnace cool down the pouring column, so that condensation phenomena of Pyrolysis products in Gasabsaugbereichen, in the recycle gas lines and in the recirculation of the cycle gases required gas jet compressor lead, causing the Function of the cycle gas furnace is disturbed. In the recirculation gas extraction according to the prior art become inevitable also dusts and smaller waste particles sucked, which with the condensed pyrolysis products throughout Circulation gas guide to hard-to-remove deposits to lead. Furthermore, the pouring column by the ascending Circulating gas can be heated only relatively slowly, so that it especially in the gasification of waste with higher Proportions of plastics to adhesions and adhesions of the Waste parts come to the wall of the shaft, which ultimately can lead to complete blockage of the furnace.

An object of the present invention is therefore to an improved reactor and method for gasifying and To provide melts of feedstocks which the Avoid disadvantages of the prior art. A special one The task is simple, inexpensive and environmentally sound material and / or energy recovery of waste to enable. In particular, the aim is functional reliability to increase a corresponding reactor, by the associated with the recirculation gas guide Operating uncertainties are largely avoided. A Another object of the invention is the pollution in the suctioned off excess gas significantly reduce the effort in a subsequent gas purification can be minimized.

These and other objects are achieved by the in claim 1 dissolved reactor. According to the invention in the state The technique followed for some time approach of the cycle gas process leave and instead comes as a reactor a shaft furnace used, the DC principle is working. By completely abandoning the Conventional cycle gas management are all related to it standing problems of condensation of pyrolysis products and the formation of unwanted deposits completely avoided. Continue to take place already in the upper part the reactor a partial conglomeration of the starting materials, due to the shock-like heating of the pouring column, so that Adhesions on the inner wall of the reactor largely excluded are. The double injection of oxygen or Fuel gas (gas mixtures) enables combustion on the one hand the pyrolysis gases and allowed on the other hand in the lower reactor section maintaining a high enough level Temperature, so that the melting there collecting liquid being held. Forms between the two Eindüsungsmitteln There is a reduction section through which all gases before the suction and in which they therefore largely be reduced.

In one embodiment, in particular for gasification of waste, attaches to the feed section a Pre-tempering section, in which the waste For example, predried at temperatures around 100 ° C. become. In modified embodiments may in this Section may also be a cooling of the starting materials if this is useful for the overall process.

An advantageous embodiment of the reactor is apparent characterized in that the total length of feeding section and Pre-tempering section several times larger than the diameter of the feed section. Through this design, the effect Shake column in the supply and Vorstemperierungsabschnitt as a top-closing plug, the suction to large portions of ambient air into the reactor prevented.

In a modified embodiment, the reactor can its upper end by a lock, a double flap system or a similar facility. This is the uncontrolled entry of ambient air and the escape of gases from the bed even better avoided.

Conveniently, the reactor is substantially cylindrical constructed and the Gaszuführraum and the Gasabsaugraum are designed annular, so that the gas supply and the Gas extraction on the entire circumference of the Schüttsäule respectively. This embodiment is particularly suitable for Utilization of predominantly organic starting materials. Other Embodiments, e.g. more suitable for other starting materials are non-cylindrical basic shapes and different positioned and shaped gas extraction means and own feeder.

It is particularly advantageous, although the pyrolysis section the reactor is double-walled and in the wall cavity a heat transfer medium is guided. On the one hand can be cooled by the wall, causing the material stress is reduced, on the other hand, depending on used feedstock and the resulting Heat demand of the Schüttsäule if necessary additional heat be supplied or derived from this heat.

The o.g. Objects of the invention are also by the in Claim 12 specified method for gasification and / or Melting of ingredients dissolved, which u.a. advantageous for material and / or energy recovery of waste and other input materials.

The process steps essential to the invention can be advantageous be further developed by a predrying of Feedstock by heating the pouring column above the Level at which the shock-like heating takes place about 100 ° C is made. This will be water shares of Feedstock largely evaporated, which also the desired automatic downward movement of the insert is improved. In a modified process variant there is no pre-drying of the starting materials or a Cooling of the starting materials, the latter being expedient can be used to adhere to the hot starting materials Wall of the feed section to avoid.

It is also particularly advantageous if the negative pressure for the extraction of the excess gases is controllable, wherein the Extraction should be done so that on the one hand no gas upwards escapes from the reactor and on the other hand only minimal Sucked additional amounts of ambient air through the pillar become. Minimizing the amount of in the reactor existing false air aims to reduce the proportion of nitrogen oxides to reduce in excess gas and also the total amount of gas keep small to the subsequent gas economy easy to design.

Further advantages, details and developments result from the following description of preferred embodiments of the invention, with reference to the attached Drawing.

The single figure shows a simplified sectional view a reactor according to the invention.

Hereinafter, with reference to FIG 1, a preferred embodiment a reactor described. In connection with the Explanation of the details of the reactor will also be the Procedural steps indicated in the treatment of Wastes with organic components as feedstocks in run this reactor. As from the appended claims is recognizable, is the implementation of the invention However, not necessarily method to the illustrated reactor bound, but may possibly also be modified using Plants are running. When using others Feedstocks could be modifications of the reactor and / or the Method are appropriate (e.g., flexible assembly and Design of the technical design of the gas supply and removal, heating or cooling of the reactor jacket etc.). In general, different starting materials can be combined be, for example, by adding feeds with higher energy value (for example, organic wastes, polluted Waste wood or the like) during gasification / melting of non-organic Feedstocks.

The reactor shown in the figure has at its upper end a Zuführabschnitt 1 with at least one Feed opening 2, via which the material and / or energy is fed to be recycled feedstock. Preferably In this feedstock, the proportion of organic predominates Ingredients, so that the reactor and the described method especially for the treatment of conventional Domestic waste and household-type commercial waste is suitable. Provided for certain feed compositions, the flammable ones Components are not sufficiently high to prevent the combustion and to carry out gasification processes, the Feedstock combustible additives or energy sources be added. It is possible in conventional To add a certain amount of coke or the total calorific value to increase by adding wood. In certain circumstances it may also be useful to add other additives, for example, the adjusting pH to influence. Such measures are, however, those skilled in the art known, so that on a detailed presentation of this Job is omitted.

About a suitable conveyor 3, the feedstock and optionally the additives via the feed opening 2 in the Reactor introduced. This forms a pouring column 4 out. With not separately designated Füllstandsmeßgeräten the height of the Schüttsäule 4 is monitored. This dumping height is between a minimum and a maximum level too hold. The minimum level is chosen so that the pouring column 4 in the upper section of the reactor as a barrier layer affects the penetration of larger amounts of ambient air prevented in the reactor.

At the feed section 1, a pre-tempering section closes below 5, in the example shown, the pre-drying the feedstock serves. The feeding section and the Vorstemperierungsabschnitt are advantageous cylindrical or conically shaped with slight cross-sectional increase downwards. The pre-tempering section 5 has a double Wall, wherein a wall cavity 6 is formed in which a heat transfer medium is guided. With help the heat transfer medium can the Schüttsäule in the area of the double-walled predrying section 5 heat be fed so that the feedstock preheated or is pre-dried. Possibly. the wall cavity can be omitted and the heat directly, for example by heat conduction from the hotter zones of the reactor. The Heat input is dimensioned so that adherence of certain Feedstock components on the wall largely excluded is. In addition, by pre-drying water constituents be discharged, so that these the other Do not add extra weight to the gasification process. In the pre-tempering section 5, the pouring column 4 tempered at about 100 ° C. become.

The pre-tempering section may possibly be omitted altogether, if a predrying due to the composition of the Feedstock is not required, or the Vortemperierungsabschnitt is used in special cases for cooling the Feedstocks used.

Below the Vortemperierungsabschnitt 5 closes Pyrolysis section 8, wherein it is at the transition between Pre-tempering section (or the feed section, if the Pre-tempering section omitted) and pyrolysis section a sudden cross-sectional expansion comes. Preferably increases the free shaft cross section in this Transitional area at least twice, which on the one hand reduces the rate of descent of the starting materials and on the other hand a bulk cone 9 is formed. Of the Bulk 9 is centrally from the pouring column 4 in the predrying section fed. At the edge areas the flattens Abrasive cone, so that there is a free space. In this upper edge region of the pyrolysis section 8 are located Gas supply 10, which in the example shown as an annular gas supply space 10 is configured, which is approximately in the plane of the cross-sectional widening in the pyrolysis section 8 is open. The purpose of the gas supply space 10 is to introduce hot gases to the bulk cone 9. The gas supply means may also serve as nozzles, wall openings or other devices designed to be the feed allow hot gases to the pouring column. This leads to the shown example, at least one combustion chamber 11, at least equipped with a burner 12, in the Gaszuführraum 10. The burner 12 generates the required hot gas, which preferably tangentially over the combustion chambers and the Gaszuführraum is brought to the bulk cone 9. In modified Embodiments may include multiple combustors or several burners are used, if this is for one As uniform as possible heating of the bulk cone desirable is.

The combustion in the burner 12 is expediently carried out under oxygen deficiency, so that by a nearly stoichiometric Combustion of an inert combustion gas at temperatures of about 1000 ° C is provided. At least during start-up operation the burner will need foreign fuels that are not immediately be recovered from the reactor. For example, come Natural gas, oil obtained from a previous gasification process generated and cached excess gas, gas mixture, Liquid-gas mixture, dust-gas mixture or others under energetic aspects suitable media used. As soon as the reactor its operating condition described below has taken the burner 12 can also with an optionally operated previously purified excess gas. By the Supply of combustion gas, which under suitable control is largely composed of carbon dioxide and water vapor, the in the bulk cone area existing feed shock-like heated. The very rapid heating of the material to temperatures between 800 ° C and 1000 ° C causes a very fast Drying of this material, causing sticking and sticking is avoided on the wall. Rather, it comes at least partly to a conglomeration of the starting materials. Furthermore is already in this upper section of the reactor the Expelled from pyrolysis products. Since that supplied gas is largely inert, these pyrolysis products supplied to combustion only to a small extent, as far as air is piled up above the bulk pile Schüttsäule 4 can be sucked or from the feedstock is carried. Due to the fast and strong heating of the Starting materials are also fine dusts and smaller Particles quickly gassed or burned, so far in the State of the art resulting problems in the dust treatment be avoided. Rather, the feedstocks in Relationships now specifically determine dusts and fines be added.

The feed then continues to sink in the pyrolysis section 8 down, pyrolysis being continued, i.a. also at the materials kept in the center by heat transfer also heated. The wall of the pyrolysis section is preferably thermally insulated and / or double-walled formed so that, if necessary, in the formed wall cavity also a heat transfer medium are performed can. The heat insulation or the additional heat with Help of the heat transfer medium are dimensioned so that the starting materials in the lower part of the pyrolysis section 8 a temperature of preferably over 500 ° C. exhibit. The temperature desired at this point may be in Dependent on the specific feed materials targeted be managed.

Below the pyrolysis section 8, a melting point closes. and overheating section 14. This has a cross-sectional narrowing due to which the sinking rate changed the feedstock. In the example of Treatment of predominantly organic waste is a cross-sectional narrowing by at least 10%, for example by conical indentations of the corresponding shaft part in an angle of about 60 ° to the horizontal is generated. They are also in the melting and overheating section 14 upper injection means 15, in the example shown formed by a plurality of circumferentially distributed oxygen lances 16 are. To prevent the oxygen lances 16 from overheating protect, for example, these are water cooled. at other designs come nozzles, burners or the like used as upper injection means, over which controlled supplied various fuel gases or gas compositions with the aim of reducing the temperature in the melting and overheating zone to a desired value. If the supply of oxygen is not sufficient for this (If, for example, no starting materials with sufficiently high energy value at this position stand), can also external fuel gases or from the reactor obtained excess gases supplied via the injection means become. In the specific example, using the top Eindüsungsmitell 15 the targeted and metered addition of Oxygen just below the plane of cross-sectional narrowing. This forms in the area of melting and Overheating section 14 of a hot zone 17, in which preferably temperatures of 1500 ° C to 2000 ° C, but which are to be matched to the respective feedstock.

The over the Gaszuführraum 10 supplied (inert) combustion gases and the pyrolysis gases formed in the pyrolysis section 8 are sucked through this hot zone 17. The oxygen supply in the hot zone is controlled so that combustion takes place under oxygen deficiency, the finally to a further increase in temperature and to extensive coking of the residues of the feed to lead. The temperature in the hot zone 17 is adjusted that slag-forming mineral constituents and metallic constituents melted in this zone being a certain proportion of in the feedstock contained pollutants (e.g., heavy metals) in these Melting is solved. The molten metal and the slag melt then drip down. The largest possible coked residues also sink further down.

Below the melting and overheating section 14 is then a reduction section 20 is formed, in which the coked residues with sufficient residence time on sink downwards. The reduction section 20 includes a Gasabsaugraum 21, sucks over which excess gases become. All extracted gases must therefore both the hot Zone 17 as well as one under this by the coked residues flow through trained reduction zone 22. In the Reduction zone 22, the gases using the existing there Reduced carbon. In particular, it comes to Conversion of carbon dioxide into carbon monoxide, taking in particular The carbon still contained in the bed is used up and thus continue to be gassed. When passing through the reduction zone 22, the gases are also cooled so that they with a technically controllable temperature, preferably about 800 ° C to 1000 ° C, can be aspirated. The sucked off Excess gases will be following (not shown) Cooling and / or cleaning stages and a suitable Conveyor (compressor or blower) supplied. at the gasification of waste with predominantly organic components After that, for example, about 80% to 90% of the Excess gases as fuel gas for a material and / or energetic Usage available. It can be a partial flow of about 10% to 20% as own gas the o.g. Burner 12 and / or be fed to the Eindüsungsmitteln, wherein the Cooling / cleaning for this partial flow to a minimum can be limited. The Gasabsaugraum 21 is in turn advantageous (but not mandatory) ring-shaped, a connected conveyor of the suction of the Gases serves.

Below the Gasabsaugraumes 21, a refractory closes lined stove 25 at. In the hearth 25 are the molten metals and the slag melts collected. So that these Melting liquids remain immediately above Melting and below the Gasabsaugraumes 21 lower injection 26 provided, in the example shown again several oxygen lances 16 (possibly water-cooled) exhibit. The lower injection means may alternatively designed and operated as above for the top Injection means 15 has been explained. About the injection of a suitable amount of oxygen, gas, fuel gas o.ö. becomes one Temperature set for the melts that sufficient is high to keep the melts fluid and after corresponding collection via a tap 27 from the reactor to be able to leave. For example, temperatures of about 1500 ° C appropriate. The division of the total amount of supplied oxygen / fuel gas to the combustion chamber 11, the upper injection means 15 and the lower injection means 26 is dependent on the feed used and to optimize from the other process parameters, with the The aim of the extensive utilization of the feedstock and the Minimization of pollutant content in the residues.

It will be understood by those skilled in the art that, for example for the sake of cost reduction instead of oxygen also an oxygen-air mixture or an oxygen-fuel gas mixture can be supplied. It is also obvious that the temperature values given by way of example depend on of the feedstocks to be processed and the to be adapted to the desired process speed. It is also understandable that the feeds under circumstances to undergo mechanical comminution before they are introduced into the reactor to clog avoid. Depending on the input materials and of the desired final products can be added to certain additives Stabilization of the calorific value and to increase the yield on excess gas and to improve slag formation, basicity and slag flow.

If liquids are also to be reacted in the reactor, These can be advantageous via a Flüssigkeitsseindüsung 30th be fed, which opens into the gas supply chamber 10 or with other gas supply means is combined. About the liquid injection 30 may be water, water vapor or others Disposal certain liquids are introduced, wherein in addition to the desired disposal, a regulation of Temperature of the inert combustion gases, the pyrolysis process and / or the composition and temperature of the excess gases becomes possible.

Furthermore, it is possible to selectively dispose of if necessary To introduce dusts via a dust feed 31 in the process. The dust feed 31 is preferably a center in the Feeding section 1 and guided in the pre-tempering section 5 Metering tube, which ends in the vicinity of the bulk cone 9. The dusts are therefore immediately in the vicinity of the shock-like Heat the feedstock transported so that they Exiting the metering tube immediately a high temperature effect are exposed to a burning or gasification causes, without causing deflagration or the like.

Although the above specific embodiment explained in particular for the treatment (gasification and melting) of It is suitable for waste with organic components the skilled person will be apparent that in use other feedstock Modifications of the reactor required or expedient. In general, also special waste or starting materials treated with higher metal content be partly with the gasification and partially the Melting principle will predominate. It can also be different Starting materials are combined. That's the way it is, for example possible, for melting non-organic starting materials targeted input materials with higher energy value (for example, organic Waste, contaminated waste wood or the like).

Claims (16)

1. Reactor for gasifying and/or melting materials, consisting of:

   A feed section (1) with a feed aperture (2) through which the materials are introduced into the reactor from above;

   A pyrolysis section (8) which adjoins the foregoing section (1, 5) at the bottom to create a cross-sectional enlargement so that a discharge cone (9) of the material may form;

   Gas supply means (10) opening into the pyrolysis section (8) approximately at the level of the cross-sectional enlargement, through which hot gases are supplied to the discharge cone (9);

   A melting and superheating section (14) which adjoins the pyrolysis section (8) at the bottom to create a cross-sectional narrowing;

   Upper injection means (15) through which a high-energy medium is introduced into the melting and superheating section (14) immediately below the level of the cross-sectional narrowing;

   A reduction section (20) which adjoins the melting and superheating section (14) at the bottom and consists of gas exhaust means (21) through which surplus gases are extracted;

   A furnace (25) with a tap hole (27) below the reduction section (20), for collection and discharge of metal melts and slag melts;

   Lower injection means (26) through which a high-energy medium is supplied immediately above the melts and below the gas exhaust means (21), to prevent the melts solidifying.
2. Reactor according to claim 1, characterized in that a pretempering section (5) is located between the feed section (1) and the pyrolysis section (8).
3. Reactor according to claim 2, characterized in that the pyrolysis section (8) and the pretempering section (5) are in double-walled form, at least in sections, to create a wall cavity (6) and a heat transfer medium being carried in the wall cavity (6).
4. Reactor according to one of claims 1 to 3, characterized in that the gas supply means are in the form of a gas supply space (10), opening into which is at least one combustion chamber (11) equipped with at least one burner (12) which supplies hot gases at approximately 1000°C to the discharge cone (9) through the combustion chambers and the gas space, the gas supply means (10) and the gas exhaust means (21) being in annular form on the circumference of the reactor.
5. Reactor according to one of claims 1 to 4, characterized in that the feed section (1), possibly the pretempering section (5), the pyrolysis section (8) and the reduction section (20) are cylindrical or slightly wider and conical towards the bottom in form, the total length of the feed section (1) and pretempering section (5) is at least three times the diameter of the feed section at the top and the cross-section of the pyrolysis section (8) is at least twice the cross-section at the bottom of the predrying section.
6. Reactor according to one of claims 1 to 5, characterized in that the upper and/or lower injection means (15, 26) consist of several oxygen lances (16) or nozzles arranged in circles on the circumference of the reactor, through which oxygen or a fuel gas mixture is supplied.
7. Reactor according to one of claims 1 to 6, characterized in that the gas supply means (10) are connected to a liquid feeder (30) through which liquid or vaporous materials may be supplied.
8. Reactor according to one of claims 1 to 7, characterized in that a powder supplier (31) is further provided, through which powder may be supplied directly to the level of the cross-sectional enlargement between the feed section (5) and the pyrolysis section (8).
9. Reactor according to one of claims 1 to 8, characterized in that the feed section (1) is largely gasproof sealed at the top, the material being supplied through a lock device.
10. Method for gasifying and/or melting materials consisting of the following steps:

    Formation of a discharge column (4) largely insulated from the environment in a shaft-type reactor;

    Shock heating of the discharge column (4) by supplying hot gases in the top section in order to initiate pyrolysis in the materials;

    Production of a hot zone (17) lower down with temperatures above 1000°C by supplying high-energy media;

    Burning of the pyrolysis products, melting of any metal and mineral constituents contained in them and extensive carbonization of the residues of the materials in the hot zone (17);

    Suction of all the gases to the bottom through the discharge column (4), the hot zone (17) and a reduction zone lower down (22);

    Discharge of reduced surplus gases from the reactor in the reduction zone region (22);

    Collection of any metal and/or slag melts in the bottom section of the reactor;

    Introduction of high-energy media immediately above the collected melts to keep them liquid;

    Casting of the melts if necessary.
11. Method according to claim 10 in which the high-energy media supplied are oxygen, fuel gases, contents of the extracted surplus gas, liquid fuels or powder fuels.
12. Method according to claim 10 or 11 further consisting of the following steps:

    Level monitoring of the reactor, so that the discharge column is always at a level between a minimum value and a maximum value;

    Setting of the minimum value so that the discharge column is insulated from the environment above the shock heating point by relatively tightly packed material.
13. Method according to one of claims 10 to 12 further consisting of the following steps:

    Predrying of the materials by heating the discharge column above the shock heating point to approximately 100°C;

    Regulation of the vacuum for extraction of the gases so that almost no gases escape upwards out of the reactor and only minimal quantities of additional ambient air are drawn in from above through the discharge column.
14. Method according to one of claims 10 to 13 further consisting of the following steps:

    Production of the hot gases for shock heating of the discharge column by burning external fuels in the starting phase of the method;

    Production of the hot gases for shock heating of the discharge column by burning the reduced surplus gases discharged from the reactor, which are at least partially scrubbed, in combination with external fuels if necessary;

    Anoxic burning method, so that an inert combustion gas consisting mainly of carbon dioxide and steam is generated.
15. Method according to one of claims 10 to 14 further consisting of the following steps:

    Supply of the discharged surplus gases to a downstream gas utility for cooling and/or scrubbing;

    Supply of recyclable powders immediately adjacent to the shock heating of the discharge column.
16. Method according to one of claims 10 to 15 in which a reactor is used according to one of claims 1 to 9.

Images