DE4030554A1 - Procedure and device for thermal treatment of waste materials - comprises reactor combustion zone charged with waste, coke and lime, and gas produced passes through hot coke be also located in reactor - Google Patents

Abstract

Waste material can be thermally treated in a reaction vessel. The reactor is loaded with the waste material (21), coke (22) and excess of a Ca- contg. material (24) such as lime or CaCO3. This mixt. is placed in a combustion and melting zone (V) which is separate from a coke bed (K) also located in the reactor, and is melted there. The gas (G) produced is passed through the coke bed at a high temperature in order to convert its CO2 content into CO. The melting zone is located above the coke bed, and the gas is passed through the coke bed and leaves the reactor at one side or at the top (16). Alternatively, the melting zone may surround the coke bed, the gas passing upwards, and the melted material downwards, through the coke bed. The melted material is collected at the floor of the reactor. Waste material, coke and Ca-rich material maybe loaded into the reactor in layers. An oxidn. substance (8) such as air or oxygen, and a fossil fuel (9), may be introduced into the melting zone and the coke bed from one side or from above. USE/ADVANTAGE - For thermal treatment of waste material such as household waste, industrial waste, filter dust, sewage sludge, packing material etc. The waste material is disposed of in a manner which is neutral to the environment, and in particular organic components are reliably destroyed and the products of the procedure can either be re-used or can be disposed of without problems.

Description

The invention is directed to a method for thermal loading handling of waste materials such as household waste, commercial waste, industry garbage, building rubble, filter dust, sewage sludge, packaging material, Suspensions, solutions or the like in a reaction container which is present at least in solid and / or lumpy form Waste in the reaction vessel of a combustion and Melting zone is supplied, in which it burns with Carbon and / or carbonaceous fuel when it is created a reaction gas is heated to liquefaction.

Furthermore, the invention is directed to a device for Implementation of the process, consisting of a shaft furnace-like Lichen, essentially closed reaction vessel with upper oven, furnace and rack, at least one, the Reak gas-tight and pressure-tight loading device direction, lines for feeding an oxidizing Mit means and possibly a fuel in the reaction vessel and Lei to lead exhaust gas out of the reaction vessel and Tapping lines for the removal of slag and melt, whereby in a coke bed and one on top of it the or attached solid bed of feed material are to be trained.  

Despite diverse considerations of reuse and reuse recovery of waste materials through recycling and processing there are still waste materials that have to be disposed of. There Landfill areas are becoming increasingly scarce, is used to reduce waste drop volume waste thermally treated. This happens in garbage incinerators. Household waste is usually found in garbage burners burned systems that trained similarly to firing boilers det and to which the garbage is fed on a traveling grate. The waste is fed into the lower part of the boiler burned and partially melted. The exhaust gas is after led out of the firing boilers at the top. The sensible warmth the exhaust gas is used to heat and evaporate water uses. Waste incinerators have come under fire because from their chimneys despite complex exhaust gas cleaning systems Dioxins escape. Polychlorinated dioxins and furans are formed usually especially when cooling the flue gases from waste incineration plants at temperatures between 500 and 300 ° C. Construction stones are more or less contained in waste materials Chlorides and soot.

Furthermore, it is known to thermally wastes in rotary kilns to treat. The waste is burned, gasified and opened melted. Rotary kilns have the disadvantage that the off burning of lumpy waste material that tends to foam and / or whose slag does not disintegrate, does not occur completely. It bil There is often a porous protective layer around the pieces of waste the exchange of materials and heat and thus a further burnout prevented. For example, charred filter cake lumps from the biological wastewater treatment only on the surface and burn in the core not completely out. Furthermore, there is a Feeding of barrels with high calorific liquids of the night  part that the degassing and gasification and the combustion after the Leakage or bursting of the barrels is so fast that a local lack of air and soot, which also occurs in one any intended afterburner only partially burns and the is poorly separated in the flue gas cleaning.

Finally, there are also pyrolysis plants for thermal treatment known from waste materials. These work at temperatures that a complete gasification and decomposition of organic stock parts, especially of hydrocarbons, do not guarantee.

The object of the invention is to provide a solution with which Treat waste materials thermally and dispose of them in an environmentally neutral manner and in particular organic components are to be decomposed safely as well as products that are intended for further use leads or can be deposited safely.

In a method of the type mentioned, this task is solved according to the invention in that the reaction tank with thermally treated waste material, coke and possibly calcium-containing material, in particular lime (CaO) or limestone (CaCO ₃ ), preferably in Excess, is charged and the feed in the reaction vessel at least one combustion and melting zone, which is arranged and formed at least substantially outside a coke bed formed in the reaction vessel, and is melted there to form the reaction gas, and that the reaction gas after at least area contact with the molten constituents of the feed before it leaves the reaction vessel through which a coke bed which is sufficiently high for the conversion of carbon dioxide (CO ₂ ) into carbon monoxide (CO) is conducted.

By the invention, a method and as below be wrote a device created with which waste materials ther must be treated as mixed and disposed of in an environmentally neutral manner. In particular In particular, organic components are safely decomposed, as well as Pro receive products that are intended for further use or use can be pegged without any restrictions. A dioxin problem arises not in the invention, since there is no soot in the exhaust gas. The Soot is in the coke bed in the process according to the invention converted to carbon monoxide. The coke fill also works as a dust filter, so that it is still bound to dust particles Dioxins and furans retained in the area of the coke bed will. Acidic gas components are in the invention Process on calcium-containing material, especially lime, lime stone or milk of lime, bound. This calcium-containing material can optionally be fed to the reaction vessel with the feed but also in various other areas of the reacti onsbehälters supplied, blown or injected. With With the help of this calcium-containing material, chlorine, fluorine and Sulfur bound and prevents this with the exhaust gas the Re leave the action container. These substances can be found in the Melting or slag bath. Preferably with lime in the over shot, d. H. in excess especially with respect to the reak chlorine, fluorine and sulfur, worked, so that acid gas components that are released safely through the supplied given lime. With appropriate cooling of the slag removed from the frame and joder from the melting bath a stabilization of the lime excess, so that at least the then most of the heavy metals, sulfur and fluorine  is in water-insoluble form. This in the fiction Discharge can be deposited in an environmentally friendly manner if necessary be kidneyed. The slag is burned out very well and can possibly even used as granules in the construction industry.

The method according to the invention and the device according to the invention tion are relatively insensitive to all sorts set waste materials and enable combustion, gasification and melting of almost all waste materials.

In the process according to the invention, a fixed bed is used works. This enables an intensive exchange of substances. By adding a solid feed to the reaction vessel and the formation of a fixed bed are also sufficient To achieve standing times for the brick lining. Partially protects and the added feed cools the furnace lining The liquid slag and smelt components also carry wisely to protect the brick lining. Aggressive metal oxide molten slags, for example FeO-containing slags, are immediately reduced in the fixed bed by the CO that forms graces. The fact that both the molten constituents as also the gaseous reaction products in cocurrent through the Fixed loading bed are performed, there is sufficient Heat transfer and heating of the feed material.

The coke added to the feed is in the area of the feed kungsfestbettes preferably burned with oxygen, so here very high temperatures, up to approx. 2800 ° C, arise. The one with the Feed coke shows just like the coke the coke Filling grain or particle sizes of 10-100 mm. Hereby sufficient gaps are created in the fixed loading bed,  which have good gas flow and problem-free dripping of the ensure molten components. In support of the Dripping and gassing can in the area of loading fixed bed for the injection or injection of liquid or gaseous substances flowing into the reaction vessel Lines should be aligned in such a way that they counter the heavy directed media and substances into the reaction vessel blow. As a result, at least in certain areas, vortex zones and a loosening of the fixed feed bed created a favorable contribution to heat transfer and to gasification and Perform draining.

The control of the combustion in the area of the loading fixed bed tes can be determined by specifying a certain amount of combustion air or The amount of oxygen and / or the amount of waste depending on temperature or other process parameters. Each According to the calorific value of the waste, there can be quite a large excess of air numbers of over 2.0 result, but it can already be an air an excess of 1.2-1.3 is sufficient.

In the area of the coke fill there is good gas flow as well problem-free drainage of the molten components Ensure grain or particle sizes of the coke of 10-100 mm continuous In that the emerging from the fixed loading bed hot reaction gas through the coke bed out of the reak tion container is withdrawn, prevail in the coke fill tem temperatures of over 1000 ° C. In the area of the fixed loading bed formed and not decomposed heavy hydrocarbons, tars and other high molecular weight products will be called red hot Coke bed converted to low molecular weight gases. These in Be rich of the loading fixed bed has not yet completely burned  th gaseous products can completely in the coke burn out. This is supported, albeit in the coke area blown oxygen into the reaction container and thus temperatures of up to approx. 2800 ° C can be reached.

With the inventive method or the inventive The device can thus in particular also highly chlorinated coals hydrogen, such as B. fluorine-chlorine hydrocarbons, chlorine-Koh Hydrogen oils and sulfur-containing organic compounds and Salts are burned and completely destroyed. For example can continue to use brominated and chlorinated benzenes, polychlorinated Biphenyls (PCB), phenols, etc. can be disposed of.

The dust discharge from the reaction vessel is low because the Coke fill serves as a dust filter. In addition, can be provided be a steam injection in the area of the gas outlet make the coke fill so that here an additional cooling Development and retention option for dusty and gaseous components ten is formed. Approximately still in the reaction gas to dust particles Bound existing dioxins and furans can in this way Reaction container retained or pre-continued by the see injection of calcium-containing material bound. In principle, however, there is no risk of dioxin formation ben, because the reaction gases for a relatively long time at a high temperature level and the exhaust gas is still in the reaction vessel leaves with temperatures of over 1000 ° C, if in the range of A steam injection is not carried out. Of course, the exhaust gas emerging from the reaction vessel can continue exhaust gas treatment systems, such as dust filtering and / or a gas wash.  

Furthermore, the residence time of the substances to be burned or Gases in the reaction vessel are extended and their full Destruction ensured when the method and the device according to the invention under an increased pressure of can be operated up to 10 bar.

First of all, the added feed components gasified and melted in the method according to the invention and in the area of the coke fill a reducing environment sets, so that the feed components used reduce rend melted down to slag and in particular a ferrometal will.

The from thermally treated waste material, coke and possibly calcium-containing material feed is called a fixed bed first fed to a combustion and melting zone. Here ent stand by the introduction of an oxidizing agent, preferably oxygen, such high temperatures that the loading materials to form a reaction gas melt and completely gasify and decompose organic compounds be set. In addition, there is a sufficiently long dwell time in the Guaranteed area of these zones with high temperature. These The combustion and melting zone is outside a coke bed, through which the molten feed stock parts and then the reaction gas in contact with each other be directed. There is a close and intensive exchange of substances both within the molten constituents (diffusion) and also between the molten components and the reacti onsgas instead. In the molten components that the Melt comprising slag and ash components Sulfur, fluorine, chlorine and acidic gas components bound. Gas  shaped components are reduced on the hot coke bed. The carbon dioxide formed in the combustion and melting zone reacts to carbon monoxide at the coke bed. That the reaction Exhaust gas leaving the container is rich in carbon monoxide and calories. The molten constituents collect as and / or slag bath in the bottom area of the reaction container. There they can be removed from the reaction vessel and ge after cooling stored and later used for further use. Each according to the composition of the reaction vessel in the Invention feed material supplied in accordance with the method, which in addition to the components already listed also iron oxide and / or metal oxide-containing components and silicon oxide and can contain substances containing alkali oxide, these substances can be found in the iron or metal industry as well as the glass or cement industry use.

Molten components and reaction gas are preferred led in cocurrent through the coke bed, but it is also possible, this only in regions in direct current through the coke lead and then the reaction gas up through the Lead coke out of the reaction container and the molten constituents in the frame of the reaction container collect.

In the method according to the invention there are no problems with the Refractory lining of the reaction vessels, because the furnace outside masonry through the feed materials or the coke fill is protected as well as at the high reaction temperatures wise iron oxide-containing slags and melting components relative can be reduced quickly.  

Furthermore, the exhaust gas is almost completely free of stick oxides, because any nitrogen oxide formed in the reaction vessel is broken down again by reducing gas components.

In addition to the removal of waste materials, which is in the foreground by thermal treatment in the ver Mainly drive a carbon monoxide and high calorie Produces gas. This gas is preferred by injecting Oxygen into the coke bed and the coke and / or coal ent fixed bed loading and the implementation of carbon dioxide generated at the coke fill. This can reduce the Coke consumption both in the fixed loading bed and in the loading Coal is richly fed with coal and gasified. The The carbon dioxide that forms during coal gasification is produced at the Coke fill also converted to carbon monoxide. It was ge found that up to 60% of the coke used by coal are replacing. There only has to be so much coke that the conversion of carbon dioxide into carbon monoxide is guaranteed and the coke fill its further function as a supporting structure for the fixed loading bed can still meet and sufficient Interspaces for the gassing and draining of the melt components are present.

The carbon monoxide and calories leaving the reaction vessel rich exhaust gas can be used for the synthetic generation of liquid Koh hydrogen or used to generate a synthesis gas will. For example, the exhaust gas rich in carbon monoxide can be used Methanol or be used for oxo synthesis. Depending on the type of the intended use for the exhaust gas is to blow in Steam and / or hydrogen in the reaction vessel moderate.  

To take advantage of the resulting in the inventive method of the exhaust gas, it is provided according to a further invention Process further process steps for thermal waste treatment, such as a pyrolysis device or a sludge drying device, assign and feed the exhaust gas. Part of the exhaust gas can also be returned to the reaction vessel be returned.

The configuration is particularly expedient and advantageous in that Area of the reaction gas leading out of the reaction container of steam and / or water and / or alkali, ins special calcium-containing material in the reaction container passed and brought into contact with the reaction gas. By the introduction or injection or the injection of water vapor or water can regulate the temperature in this area and significantly reduced and dust particles retained. Alka Containing material, especially calcium-containing material, is in this Area supplied to the interior of the furnace, so that this may still acidic gas components present in the reaction gas react and this may be retained in the reaction vessel and thus from the Exhaust gases are kept away.

Further advantages through further training and design of the Ver driving result from the subclaims.

In a device of the type described in the introduction standing object according to the invention in that the loading material to be thermally treated waste, coke and optionally contains calcium-containing material and the reaction container in the transition area from the solid bed from the feeder  Material for coke filling in the direction of flow of the reaction gas has a cross-sectional expansion.

This device is also relatively insensitive to all possible waste materials used and burns, gasified and melts almost all waste materials that are supplied. Although are Generic devices from DE-OS 33 24 064 and DE-OS 32 16 019 known, but it is not in this device seen to thermally treat waste materials here. Through the im Transition from the loading material fixed bed to the coke bed Cross-sectional change formed is achieved that by flow in this area the flow rate of the reacti onsgases in the coke bed is reduced.

Further advantages through further training and design of the inventions Device according to the invention emerge from the subclaims. Further advantages are in the further and the above Be spelling listed.

The invention is below with reference to the drawing, for example explained in more detail. This shows in

Figure 1 is a schematic sectional view of a first embodiment example of a reaction vessel for performing the method.

Figure 2 is a schematic sectional view of a second embodiment example of a reaction container for performing the method.

Figure 3 is a schematic sectional view of a third embodiment example of a reaction container for performing the method.

Fig. 4 is a principal sectional view of an embodiment of a reaction vessel with the exhaust gas outlet to the top;

Fig. 5 shows a modified design of the sub-furnace of a reaction container and in

Fig. 6 shows a schematic diagram of a system for carrying out the method with further assigned waste treatment devices.

The reaction vessel designated overall by 1 in FIG. 1 is essentially a melting gasification furnace which consists of an upper furnace 2 , a lower furnace 3 and a frame 4 with furnace bottom 5 . Upwards, ie above the upper furnace 2 , the respective reaction vessel 1 with a not shown in FIGS . 1 and 2, but visible from FIGS. 3 and 6 loading device 6 essentially gas and pressure-tight ver closed. Overall, the reaction vessel 1 or the melting gasification furnace is an essentially closed vessel. The container walls consist of a refractory lining, which in the upper furnace 2 , in the lower furnace 3 and in the frame 4 and the base area 5 consist of different material or can have a different composition. Suitable refractory materials are known to the person skilled in the field of furnace construction and the iron and steel industry.

The reaction vessel 1 is substantially cylindrical with several cross-sectional enlargements and constrictions. From continuously from the cylindrical frame 4 a subsequent cylindrical part 3 closes after top with a conical cross-sectional widening 3 a, b and a subsequent conical section narrowing 3 c of the lower furnace. 3 The lower furnace 3 then goes into the upper furnace 2 through which a cylindrical ring portion 2 a, a conical cross-sectional widening 2 b and a cylindrical extension Wan range 2 c is. In the cylindrical region 2 c of the upper furnace 2 , pipes 7 radially distributed on the inner wall of the furnace open through openings to the furnace or container interior. Oxygen 8 and fuel 9 are to be injected or blown into the upper furnace 2 through these pipelines 7 . The oxygen 8 is preferably technically pure or industrial oxygen. However, it is also possible to blow in air here, which, however, has then preferably been preheated to a temperature of 500.degree. Coal dust, coke breeze, oil, natural gas or the like can be blown in as fuel. Depending on the reaction or process control through the pipes 7 or other pipes, not shown, a Flußmit tel or slag generator 10 , such as powdered limestone (CaCO ₃ ) or calcium oxide (CaO) and / or water vapor, as by arrow 11 shown, and / or hydrogen (H ₂ ) blown into the upper furnace 2 . In the sub-furnace area 3 c adjoining the upper furnace 2 with a conical change in cross-section, a plurality of feed lines 12 in the form of slides, which are distributed radially around the circumference of the furnace, open with passage to the furnace interior. The coke 13 is to be fed to the lower furnace 3 through these lines 12 . The coke 13 has a grain size of 10-100 mm, preferably 30-60 mm. Furthermore, lime 48 , preferably calcium carbonate (limestone) or calcium oxide (CaO), can also be fed through the lines 12 to the lower furnace 3 . This either in layers or in a mixture with the coke 13 . Below the feed lines 12 , further lines 49 open into the furnace as they pass through to the interior of the lower furnace. Further oxygen 50 can be blown into the lower furnace 3 through these lines 49 . In the lower area of the cylindrical part 3 of the lower furnace 3 b is arranged externally about the lower furnace 3 around a ring line fourteenth From this ring line 14 go radially around the order of the sub-furnace 3 distributed branch lines 15 , which open into the interior of the sub-furnace 3 with through openings. By the stubs 15 and the ring lines 14 is withdrawn in the direction of arrow 16 created in in the melting-gasification furnace 1 the reaction gas, indicated by arrows G, from the reaction vessel. 1 In the area of the frame 4 closable lines 18 and 19 are arranged, through which slag F (line 18 ) and melt S (line 19 ) are drawn off or tapped from the frame 4 . Furthermore, the melting gasification furnace 1 according to FIG. 1 in the area of the frame 4 still has an electric additional heater 20 .

From above, by means of the not shown in Fig. 1, the Reakti ons container 1 to the top sealing device 6 , the reaction container 1 is charged with the thermally treated waste material 21 . The waste material is preferably pretreated to the extent that it is in lumpy or solid form. However, it is also entirely possible to introduce waste materials present in pasty or pasty form or even as a liquid through the feed system 6 into the melting gasification furnace 1 . Any waste material can therefore be introduced into the melting gasification furnace. The waste material can be household waste, commercial waste, industrial waste, building rubble, - preferably ground up -, dust, filter dust from exhaust air and exhaust gas cleaning systems, sewage and other sludge, - these preferably pre-dried -, plastic waste of all kinds, containers with liquids such as Solutions, suspensions, slurries, waste material that has already been pretreated in another treatment device, for example solid residues of coked and / or smudged waste materials in a pyrolysis plant, or the like. More.

Furthermore, there is the possibility, through the feed device 6, to supply the upper furnace 2 with coke 22 and / or coal 23 as well as with other substances 24 . These aggregates 24 are lime (CaO) or limestone (CaCO ₃ ) or other blast furnace oiler ingredients added to blast furnaces for example in the blast furnace technology for producing pig iron. These additive substances 24 are added depending on their task and are intended to act as a flux for example, ie melt relatively quickly in the upper furnace 2 , but for example also bind reaction products formed in the reaction in the upper furnace 2 or lower furnace 3 . For example, added lime (CaO) is said to bind sulfur, fluorine, chlorine and acidic gas components. When the process is carried out, the added additives 24 collect in the slag F and / or the melt S in the frame 4 of the reaction container 1 . Lime or limestone is preferably added in excess with respect to the chlorine, fluorine and sulfur loading of the feed.

Finally, there is the possibility through the feed device 6 other to feed in the upper furnace 2 aufschmelzende additives or feed materials 25 to the upper furnace. 2 These further feed materials 25 can be, for example, metal oxide-containing particles, preferably iron ore, but also silicon oxide and alkali oxide-containing substances. This feed materials 25 are melted in the upper furnace 2 and accumulate in the implementation of the process in the melt S and / or the slag F in the frame 4 of the reaction vessel. 1 The entire loading of the upper furnace 2 , consisting of the waste material 21 and the coke 22 and / or the coal 23 as well as any additional additives 24 and feed materials 25 , is fed to the upper furnace in layers or as a mixture, the waste material being preferably used as the upper furnace 2 separate layer and the other substances 22-25 can also be added as a separate layer or as a mixture.

The the upper furnace 2 supplied feed passes into the upper furnace 2 where it remains resting ver initially supported as a fixed bed on the ausgebil Deten in the lower furnace 3 packed bed of coke K and from this and remains lying. By blowing oxygen 8 and possibly fuel 9 through the lines 7 into the upper furnace 2 and since also into the fixed loading bed located there, the combustion and melting zone V is formed in the upper furnace 2 . The combustion and melting zone V essentially fills the entire upper furnace 2 . In the combustion and melting zone V, a temperature of over 2000 ° C (up to approx. 2800 ° C) is reached. This high temperature causes that the upper furnace 2 loading loading, ie above all and at least the waste material, is converted into a molten and / or gaseous state. Molten components and a reaction gas form in the combustion and melting zone V. The molten stock parts emerge from the lower furnace 2 and flow or drip in the direction of the double arrows through the coke bed K formed in the lower furnace 3 and are collected or collected in the frame 4 as a melting bath S and slag bath F. The Reakti onsgas G also emerges downwards from the upper furnace 2 and flows through the coke bed K in close contact with the molten stock. The reaction gas G is drawn off through the lines 15 and the ring line 14 as waste gas 16 from the melting gasification furnace 1 . The hot reaction gas G emerging from the upper furnace 2 and the molten constituents give off this heat when flowing through the coke bed K and heat it to temperatures of over 1000.degree. Carbon dioxide (CO ₂ ), which has formed through reactions in the combustion and melting zone V and in the area of the coke feed 12 , is unmixed in the coke bed K with the carbon of the coke to carbon monoxide (CO), so that the exhaust gas 16 only very much has low levels of carbon dioxide. The exhaust gas also has very low nitrogen oxide (NO _x ) contents. Due to the very high temperatures in the combustion and melting zone V, the reductive reaction gases (CO) that form there and the subsequent flow through the further reducing coke bed K, any nitrogen oxides that have formed are reduced and atomic nitrogen may form. Coke consuming in the lower furnace 3 is refilled through the lines 12 . The lines 12 are sealed with the feed device 26 shown in FIG. 3 in a gas-tight and pressure-tight manner with respect to the outside atmosphere. Before feeding materials into the upper furnace 2 , the lower furnace 3 is first filled with coke 13 .

The illustrated in Fig. 2 another embodiment of a re action container 1 a differs from the embodiment of FIG. 1 by a different design of the upper furnace 2 and the transition from the upper furnace 2 to the lower furnace 3rd This embodiment form of the upper furnace 2 can be combined with both the lower furnace 3 according to FIG. 1 and with the lower furnace 3 according to FIGS . 3-5. Parts, areas and lines which correspond to those described for FIG. 1 or which are identical to them are given the same reference numerals in FIG. 2, as in the subsequent FIGS. 3-6, without these in each Case must be listed again in the description.

The first furnace according to FIG. 2 differs from the upper furnace according to FIG. 1 in that it has a greater overall height and here several injection levels are provided one above the other. Wei terhin the transition from the upper furnace 2 to the lower furnace 3 is different ge. Here joins the cylindrical upper furnace region 2 a conical cross-sectional widening 2 d to the cylindrical in a wei lower region 3 d of the upper furnace 3 runs out, the upper half of the conical wall region 3 c of the upper furnace of this connecting. In the wall area 2 d, pipes 27 lead into the furnace interior. Through these pipes 27 , in particular finely divided coal 28 is to be fed into the furnace interior. Below the pipelines 27 open further feed lines 29 in the wall region 2 d into the furnace interior, through which an oxidizing agent, preferably oxygen 30 , is blown or injected into the furnace interior. As a result, the supplied coal 28 is burned and forms the further combustion zone V ₃ in the furnace interior. For temperature control within the combustion zone V ₃ , additional steam, if necessary, can additionally be blown into the furnace interior through further injection openings, not shown. Otherwise, four superimposed injection levels are formed in the upper furnace 2 by lines connected to feed lines, each radially distributed on the inner circumference of the inlet openings. The uppermost, first injection level is formed by lines 31 which lead to the furnace interior. These feed lines 31 can be conventional burners through which a fuel 9 a and an oxidizing agent 8 a, such as air or oxygen, are blown into the upper furnace and burned there. When loading the upper furnace, the furnace space above the mouths of the lines 31 is not filled with material, so that a space remains in the furnace space. Here, the combustion zone V _ox forms, in which mainly oxidizing reaction conditions exist. Down to this combustion zone or the confluence of the lines 31 , the upper furnace 2 is filled with feed material. Below this first level, a second injection level is formed by the confluence of the lines 7 . These lines 7 are already described in FIG. 1 and allow the supply or introduction of fuel 9 , oxygen 8 and kalziumhal term material or substance 10 , such as calcium oxide, and possibly water vapor 11 and / or hydrogen (H ₂ ) in the Interior of the upper furnace 2 . This level is filled with loading material, ie the fixed loading bed extends into this zone. A combustion and melting zone V _{1 is} formed here. Below this injection level, a third injection level is formed by the confluence of pipes 32 and 33 in the interior of the furnace. In this level, waste material 34 present in liquid form, gaseous waste material 35 or an exhaust gas 36 can be blown or introduced into the upper furnace 2 . The substances supplied in this plane 34 , 35 , 36 can either be injected separately into the furnace or previously brought together and blown as a mixture into the upper furnace. The exhaust gas 36 may be partially recirculated exhaust gas 16 drawn from the sub-furnace 3 and / or exhaust gas that comes from further waste treatment systems, such as sludge drying or a pyrolysis system, which at least partially flows into the upper furnace into the injection level 2 is supplied. Below this water injection level, a fourth injection level formed from outlets of pipes 37 into the furnace interior is provided. Through the pipes 37 , the furnace interior is again supplied with oxygen 8 b, so that a further combustion and melting zone V _{2 is} formed here.

The reaction vessel 1 a shown in FIG. 2 or melting gasification furnace is suitable for thermally decomposing waste material of any kind and decomposing it into a reaction gas and molten constituents. In particular, the reaction vessel 1 a is suitable for absorbing and treating thermal waste materials if the composition and the quantity of waste material fluctuates over time and is unpredictable.

In the exemplary embodiment according to FIG. 2, the added waste material 21 and the added coke 22 as well as the possibly further feed components coal 23 , additive material 24 and feed material 25 first flow through the space formed in the area of the first injection level and thus the combustion point. and melting zone V _ox until they come to rest on the fixed material bed formed in the upper furnace 2 , which is supported on the coke bed K, which in turn floats on the melting and slag bath S, F. After trickling through the oxidizing combustion and melting zone V _ox , the feed material reaches the combustion zone V ₁ . Carbon-containing material is burned in this zone and temperatures are so high that solid material is melted and a reaction gas is formed. In the level below, further waste material is injected in liquid form 34 , in gaseous form 35 or exhaust gas 36 . Depending on the composition of the other substances supplied here, a reducing atmosphere can develop in this area. Below this level, the further combustion and melting zone V _{2 is} formed by the injection of oxygen 8 b through the lines 37 . In the transition from the upper furnace 2 to the lower furnace 3 , the feed material is finally fed to the further combustion and melting zone V ₃ formed in the region of the supply of coal 28 and oxygen 30 . Overall, this arrangement of the various combustion and melting zones V _ox , V ₁ , V ₂ and V ₃ ensures that sufficiently high temperatures prevail in the upper furnace for the thermal treatment of waste and zones of temperatures above 2000 ° C with certainty. The substances supplied to the upper furnace 2 and feed components, ie above all and at least the waste material, emerge from the upper furnace in gaseous form as reaction gas G or in molten form and subsequently flow or flow through the coke bed K in contact with one another in contact with the arrows indicated way. The reaction gas G is drawn off in the lower furnace through lines 15 and 14 as waste gas 16 , the constituents which are melt-like are collected in frame 4 as melt S or slag F.

The various arrangements shown in FIGS . 1-6 of injection levels formed in the upper furnace 2 are purely exemplary. Depending on the composition and volume of the various substances and materials supplied to the upper furnace and the reaction procedure derived therefrom, it is readily possible for the person skilled in the art to provide other arrangements and / or a different number of injection levels. For example, the free space and the combustion and melting zone V _{ox can be} dispensed with. According to the invention, it is important alone that at least one combustion and melting zone is generated in the upper furnace 2 by burning carbon-containing material with an oxidizing agent and, if appropriate, calcium-containing material is added. If, for example, waste material present only in liquid form is to be thermally treated in a melting gasification furnace 1 , 1 a or 1 b according to the invention, the upper furnace 2 of the reaction container is to be sent, for example, only with a mixture of calcium-containing or silicon-oxide-containing and alkali-oxide-containing material, the liquid waste material 34 is then blown into or injected into this material feed in the upper furnace or previously mixed with the feed. Essentially, a derar term melting gasification furnace is then used for the production of glass or water glass components which melted in the upper furnace 2 and, after flowing through the coke bed K in the lower furnace frame 4, are collected and, if appropriate, continuously withdrawn. Quasi as a by-product, liquid waste material is then to be thermally treated in such a reaction container and a carbon monoxide (CO) - and possibly hydrogen (H ₂ ) - as well as high-calorie exhaust gas 16 is generated. Likewise, the reaction vessel can be designed to mainly produce a pig iron melt, a feed consisting mainly of iron ores then being fed to the upper furnace 2 .

In addition to the injection levels shown in FIGS . 1-6, it can also be provided to additionally see 3 additional injection openings (not shown) for the injection of oxygen in the lower furnace.

A further exemplary embodiment for a reaction vessel 1 b or a melting gasification furnace is shown in FIG. 3. This reaction container 1 b differs from the exemplary embodiments according to FIGS. 1 and 2 by a somewhat different arrangement of injection levels in the upper furnace 2 and by additional injections in the lower furnace 3 or in the frame 4th In addition, loading devices 6 and 26 are shown in FIG. 3. Parts, loads, etc., which have already been described correspondingly or identically to FIGS. 1 and 2, are given the same reference numerals in FIG. 3 and are not expressly mentioned again in every case. Fig. 3 shows the reaction container 1 b gas and pressure-tight closing Beschickungsvor direction 6 , which is also present in the reaction containers 1 and 1 a, but is not shown in FIGS. 1 and 2. The feed device 6 consists of a double bell lock 6 a and a feed line opening there with a double lock lock 6 b. Type and operation of the Doppelglockenver circuit 6 a and the double lock 6 b are known from the blast furnace and steelmaking technology. With the help of the feed device 6 , the feed material is entered into the upper oven 2 from above. The charging device can be loaded with waste of any kind, such as was enumerated at the beginning of this special description, coke 22 , coal 23 , additives 24 and other charging materials 25 . It depends on the individual case whether all these substances are fed into the loading device. It is entirely possible to operate the reaction vessel if only one of these feed substances is supplied to the reaction vessel. However, solid or lumpy waste material 21 and coke 22 or coal 23 as well as material containing calcium oxide should preferably be supplied at least to the reaction container 1 b. The upper furnace 2 is designed like that of the reaction container 1 according to FIG. 1 and has several injection levels which are formed by feed lines 7 , 32 , 33 and 37 , through which various substances are blown or injected into the upper furnace, as is the case with Fig. 2 has been described.

The lower furnace 3 also has the shape already described for FIG. 1. The supply of coke 13 and calcium-containing material 48 into the feed lines 12 is carried out by means of feed devices 26 . Below the confluence of the supply lines 12 , 3 c pipelines 38 are provided in the sub-furnace wall area with a confluence with the furnace interior, through which further oxygen 39 can be blown into the sub-furnace 3 and thus into the coke bed K. Further injections for oxygen 40 by means of an injection line 41 , 42 and 43 are provided in the lower region of the lower furnace 3 and in the frame 4 . The injection lines 41 are arranged so that they open above the slag bath F, but below the gas outlet 15 for the exhaust gas 16 , in the lower furnace wall area 3 a in the lower furnace 3 and oxygen can be blown into the coke bed K at this point. The injection lines 42 are arranged such that oxygen can be injected through them into the slag bath F and the injection lines 43 are arranged in the bottom region 5 of the sub-furnace, so that oxygen can be injected through them into the melting bath S. The technology of injecting gaseous and / or particulate components into a molten bath is also known from the iron and steel industry. Possibly. can be fed through the injection lines 41 , 42 and 43 even more calcium or alkali-containing material to the reaction vessel 1 b. Furthermore, bottom-side feed lines 44 for blowing in coal dust 9 c and 45 for injecting gaseous waste substances 35 or liquid waste materials and a line 46 for injecting further gaseous constituents 36 , which are partially recirculated exhaust gas 16 or from other processes, e.g. . B. a sludge drying and / or a pyrolysis, ge exhaust gas can act provided. In addition, a tapping channel 47 is also shown schematically in FIG. 3, via which the molten bath S and the slag F are drawn from the frame 4 . The slag F - and, depending on feed the melt S - containing the b into the reaction vessel 1 is introduced calcium and the formed compounds immediately prior preferably after leaving the melting-gasification furnace 1 b, quenched, for example with water. The embodiment of the melting gasification furnace 1 b with various injection options in the bottom 5 is particularly advantageous if larger quantities of fine-grained or lumpy iron ore particles are fed to the upper furnace 2 and a melting bath S made of liquid pig iron is in the frame 4 Forms temperatures between 1500 and 1700 ° C.

Fig. 4 shows an embodiment of a reaction container 1 c, in which the exhaust gas 16 is withdrawn from the top of the reaction container.

The reaction vessel 1 c or melting gasification furnace 1 c has an upper furnace 51 with a feed device 52 arranged centrally above. By means of this central loading device 52 , the reaction container 1 c with coke 13 and optionally at least calcium-containing additive or material 48 , preferably as lime (CaO) or limestone (CaCO ₃ ), is to be fed centrally. Coke 13 and calcium-containing material 48 are added either in layers or as a mixture. Between feed device 52 and upper furnace 51 lead lines 53 from the reac tion vessel 1 c out, through which the exhaust gas is withdrawn from the reaction vessel 1 c sixteenth By the feed device 52 is preferably so much material is - coke 13 and possibly calcium-containing material 48 - was added that the upper edge of the ranges in the reaction vessel 1 c forming coke charge C to just below the junction of the lines 53 into the reaction tank 1 c. Furthermore, the upper furnace 51 has a plurality of lateral feed lines 54 distributed radially on its circumference, which lead into the lower furnace 55 in the lower region of the upper furnace 51 just above its transition into the upper furnace 51 . By means of charging devices 56 , which are designed like the charging device 52 as a double bell closure, the feed lines 54 of the thermally treated waste material 21 , coke 22 , possibly coal 23 , additives 24 and possibly further loading materials 25 are fed and through the lines 54 introduced into the upper furnace 51 . In the area of junction of the feed lines 54 into the upper furnace 51 is a cross-sectional enlargement is the Zulei obligations 54 is formed, in which open the pipes 7, already described for the previous embodiments. Oxygen 8 , fuel 9 , possibly water vapor 11 or water and possibly further calcium-containing material 10 , such as lime or limestone, are to be supplied to, or blown into or injected into, the upper furnace 51 through these lines 7 . In the area of the supply lines 54, combustion and melting zones V form in front of the confluence of the pipelines 7 .

The upper furnace 51 is followed by the lower furnace 55 , in which the slag bath F and the melting bath S collect. At least one tapping line 19 for the melt S and one tapping line 18 for the slag F are provided here. Of course, it is also possible in the exemplary embodiment according to FIG. 4 to let further, unillustrated feed lines open into the upper furnace 51 and / or the lower furnace 55 , through which oxygen, further liquid waste material, further gaseous waste material, further fuel and / or recirculated exhaust gas can be injected or blown into the reaction container 1 c. As already described for the above exemplary embodiments according to FIGS. 1-3, these additional feed lines can be seen and arranged on the reaction vessel, depending on the desired procedure, the amount and composition of the waste material to be treated thermally, and other parameters. With the off operation example of FIG. 4 it will be shown that it is also possible to carry out the inventive method in an apparatus in which the exhaust gas is drawn off upwards. In the exemplary embodiment according to FIG. 4, the material supplied through the feed lines 54 is melted and gasified in the combustion and melting zones V. The molten constituents or components flow downward through the coke bed K arranged centrally in the reaction container 1 c - as arranged by the double arrows - and collect in the lower furnace 55 or frame 57 . The resulting in the combustion and melting zones V and by further reaction in the coke bed K reaction gas leaves the reaction vessel 1 c - indicated by the arrows G - up through the coke bed K and passes through the lines 53 as exhaust gas 16 from the reaction vessel 1 c. The upper furnace 51 can also - unlike shown in FIG. 4 - be filled with coke 13 and possibly calcium-containing feed material 48 beyond the mouth of the feed lines 53 . In this case, it may be appropriate in the area of the mouths of the exhaust pipes 53 to expand the cross section of the upper furnace 51 with injection options for water vapor or possibly water and / or calcium-containing material, in particular lime (CaO), limestone (CaCO ₃ ) or an aqueous calcium hydroxide solution (Ca (OH) ₂ ; milk of lime), as described below in connection with FIG. 5, for example for the exhaust gas outlet from the lower furnace 3 according to one of the exemplary embodiments according to FIGS . 1-3. Also in the reaction container 1 c, reaction gas G and molten constituents come into close and intensive contact with one another at least in the area of the combustion and melting zones V.

FIG. 5 shows the lower region of a lower furnace 3. Here, a further cross-sectional expansion of the furnace interior is formed between the sub-furnace regions 3 a and 3 b in the area of the openings of the lines 15 . In this area lead to additional lines 58 . In order to be able to treat and / or influence the temperature of the reaction gas G leaving the furnace as exhaust gas 16 shortly before leaving the reaction vessel or melting gasification furnace, this area can pass through the lines 58 through steam or water and / or kalziumhal term material such as lime, limestone or milk of lime (aqueous calcium hydroxide solution) or other alkali-containing material, e.g. B. sodium hydroxide solution (NaOH) can be added. These additional substances are expediently injected or blown into the furnace interior at this point. Solids can, however, also be fed as a bed, similarly or analogously to the coal 28 according to FIG. 2.

For further treatment of the exhaust gas 16 , an exhaust gas treatment consisting of a dust filter and / or gas cleaning, for example a gas scrubber, can be connected downstream of all the reaction containers shown in FIGS. 1-6.

For all of the exemplary embodiments it is stated that the loading possibly contain calcium-containing material. Possibly. because the calcium-containing material does not necessarily add to the feed must be given, but also by means of further described Lines or leads to the respective reaction container can be led. The only important thing is that the reaction vessel calcium-containing material is supplied and this preferably in Excess.

Fig. 6 shows a system diagram in which a reaction container 1 b according to FIG. 3 is shown in conjunction with other waste treatment devices. These waste treatment devices are a pyrolysis device 59 , a sludge drying device 60 and a storage device 61 for liquid waste materials. Solid waste materials are preferably coked and / or charred in the pyrolysis device 59 . The pyrolysis device 59 is branched from the exhaust line 62 of the reaction tank 1 b by means of a line 63 to exhaust 16 . Here, the b from the reaction vessel 1 exhaust gas leaving 16 can be cooled before and / or be performed, for example, by an air preheater 64 may be heated by means of which b supplied in countercurrent to the reaction vessel 1 combustion air. The pyrolysis device 59 removed solid reaction products are, as indicated by line 65 , the loading device 6 of the reaction container 1 b supplied. The exhaust gases produced in the pyrolysis device 59 are, as indicated by the line 66 and its branches or branches, partially returned to the reaction container 1 b. Pyrolysis gas which is not recycled is fed to another treatment, as indicated by arrow 67 .

Furthermore, part of the exhaust gas 16 leaving the reaction vessel 1 b is branched from the exhaust line 62 by means of a line 68 to the sludge drying device 60 . The gaseous reaction products 69 emerging from the sludge drying device 60 , like the gaseous reaction products of the pyrolysis device 59, can be passed into the reaction container 1 b, as indicated by line 66 . For example, the indicated line 69 can open into the line 66 . The resulting solid reaction products in the sludge drying 60 , indicated by the line 70 , as well as the solid reaction products of the pyrolysis device 59 leads to the feed 6 . B escaping from the reaction vessel 1 and the pyro lytic apparatus 59 or the sludge drying apparatus 60 unused exhaust gas 16, further treatment devices as indicated by the double arrow 69, fed.

The stored in the storage device 61 liquid waste are materials, as indicated by the lines 71 and 72 and their removal or branches, either the reaction vessel 1 b or the pyrolysis device 59, possibly after injection into conduits for gaseous substances, is supplied. Blowers, control devices, etc. arranged in the lines are not described in detail.

In the installation according to Fig. 6, the reaction vessel 1 b, the center or to the engine or the heart of an accumulation of various associated thermal Abfallbehandlungsvorrich obligations. The reaction vessel 1 b thus forms the core of a, preferably central, local waste treatment or disposal center.

The melting gasification furnaces according to FIGS. 1-6 can be operated at a pressure of 1-10 bar. The working pressure is preferably 3-5 bar.

To support the draining and gassing process, the lines in the area of the loading fixed bed and / or the coal feed guide 27 for blowing or injecting substances into the reaction container can be oriented such that they blow media and substances directed against gravity into the reaction container, as shown in FIG. 2 by way of example for the lines 37 . All or only individual lines through which liquid or gaseous substances are blown into the respective reaction vessel can be aligned in this way. As a result, at least in regions, vortex zones and a loosening of the fixed feed bed are created, which make a favorable contribution to heat transfer and to the gasification and draining process.

To reduce the coke consumption both the loading fixed bed and in the area of the coke bed K coal 23 , 28 can be fed and gasified. The carbon dioxide formed is also converted to carbon monoxide at the coke bed K. Up to 60% of the coke 22 , 13 used is coal 23 , 28 to put it. There only has to be so much coke that the conversion of carbon dioxide into carbon monoxide is guaranteed and the coke bed K can still fulfill its function as a supporting structure for the loading fixed bed, and there are sufficient spaces for the gassing and dripping of molten components.

The carbon monoxide and calorie-rich exhaust gas 16 , 69 leaving the reaction vessel can be used for the synthetic production of liquid hydrocarbons or for the production of a synthesis gas. For example, the carbon monoxide-rich exhaust gas for methanol or oxo synthesis, but also as a reducing gas, for example for the reduction of iron ores, can be used. Depending on the type of further use provided for the exhaust gas 16 , 69 , the blowing in of water vapor and / or hydrogen into the reaction vessel is expedient.

Before commissioning the melting gasification furnaces or reaction containers according to FIGS . 1-6, the respective sub-furnace 3 , 55 is first filled with the coke bed K. Subsequently, the upper furnace 2 , 51 is fed by means of the loading device 6 or the loading device 56 with the further loading material, ie at least waste material 21 , coke 22 and possibly calcium-containing aggregate 24 . In the combustion and melting zones, the added waste material is gasified and decomposed at temperatures of up to 2800 ° C with the formation of molten components and a reaction gas. The high temperatures are generated by blowing oxygen into the coke components of the feed and possibly into the coke bed K formed in the reaction container. The molten constituents and the reaction gas formed in the at least one combustion and melting zone flow through the coke bed K at least in regions in contact with one another and on the one hand (the reaction gas G) leave the reaction vessel as exhaust gas or on the other hand (molten constituents) collect as melt S or slag F in the frame 4 of the respective reaction container.

The reaction containers described above are are smelting gasification furnaces with which any waste Type, d. H. solid, lumpy, liquid or gaseous waste thermally treated fabric and the inventive method can be carried out. In addition to this main task, namely Ab thermally treat waste and dispose of it, become a CO and calorie rich exhaust gas as well as a re evaluation or reuse of feedable residues, namely the Melt S and the slag F, generated. Not again or further usable residues can be deposited easily.

The method according to the invention and the device according to the invention are relatively insensitive to all possible waste materials used and burn, gasify and melt almost all waste materials that are supplied and eliminate them in a virtually environmentally neutral manner. The feed is gasified, decomposed and melted in the upper furnace and exposed to a reducing environment in the coke bed K. With the method according to the invention or in the devices according to the invention, even brominated and chlorinated benzenes, polychlorinated biphenyls (PCB), phenols, fluorine-chlorocarbons, chlorine-hydrocarbons and sulfur-containing organic compounds, as well as dioxins and furans, can be completely destroyed. At the high temperatures prevailing in the upper furnace, the organic compounds are completely decomposed. Acidic constituents of the reaction gas, like sulfur, chlorine and fluorine, are bound to the added calcium-containing material and passed into the slag F or the molten bath S. At the latest, these substances are combined with the added calcium shortly before the reaction gas G emerges from the reaction vessel when it flows through the special reaction zone shown in FIG. 5, in which water vapor and / or calcium-containing material is injected into the lower furnace through lines 58 . By injecting water vapor and / or water, such a reduction in temperature is achieved that the added lime and / or limestone and / or milk of lime react with the acidic components still present in the exhaust gas and can form connections. It is particularly favorable, especially with a view to the small amounts of harmful residues still contained in the exhaust gas, when the working time of the substances or gases to be burned to ensure their complete destruction in the reaction vessel is achieved by working under increased pressure up to 10 bar is extended even further.

With appropriate cooling of the withdrawn from the frame Slag and / or the melting bath undergoes basic stabilization excess lime and then lie heavy metals, sulfur and fluorine in water-insoluble form in the slag in front.

As the main product, the exhaust gas 16 is obtained in the reaction containers, since the described reaction containers are melting gasification furnaces, in which fuel is gasified in situ, preferably by means of oxygen, mainly coke and coal, to a hot gas to melt the furnace feed and generate a reaction gas that has CO and possibly H ₂ as the main components. Here, the coke bed K carries on its top or outside the coating, which is melted by combustion and the reaction gas or hot gas drawn off, preferably downwards. The coke bed K acts as a support structure and keeps the feed in the upper furnace 2 , 51 . Furthermore, the coke bed K has sufficiently large cavities through which the molten slag F and melt S formed in the upper furnace 2 , 51 and possibly also in the lower furnace 3 , 55 can flow down at least in regions in cocurrent with the resulting reaction gas G. The exhaust gas 16 leaving the melting gasification furnace is a hot gas of high calorific value and a reducing gas. The coke bed K usually has a temperature of approximately 1800-2000 ° C. in its upper region or the region bordering the combustion and melting zones and a temperature of approximately 1600-1650 ° C. in its lower region. The upper region of the coke bed K in the reaction container 1 c according to FIG. 4 also has a temperature of over 1000 ° C. It thus has a constant temperature by which carbon dioxide (CO ₂ ) reacts with the carbon of the coke bed K to carbon monoxide (CO). The cavities or interstitial spaces of the coke bed K and the area (s) with coke formed by the coke 22 added to the feed in the loading fixed bed (s) are of the type that the hot gas or reaction gas G flowing through, at least in some areas, in direct current contact with the downward flowing, molten constituents or components. The fact that the feed coke 22 is added, a good gas and flow through the loading fixed bed in the area of the upper furnace 2 , 51 and the various combustion zones is ensured and also ensured during operation of the reaction container. The coke used can, for example, have a diameter of 30 mm, a size which, however, can vary depending on the size of the furnace used, the operating conditions and other factors. The height of the coke layer can be approx. 4-5 m. The coke bed K is sufficiently firm to hold and support the feed consisting of waste material, coke, coal, possibly calcium-containing feed materials and possibly other additives and feed materials on its top or outside. It occupies the main area of the furnace, i. H . the height of the lower furnace 3 is generally greater than the height of the upper furnace 2 . However, this is not mandatory, as is shown, for example, by the exemplary embodiment according to FIG. 4, in which the upper furnace 51 is larger than the lower furnace 55 . The calcium-containing feed material preferably has a grain size of 6-50 mm. Calcium-containing material blown in through feed lines can, however, also be in powder or dust form.

The CO ₂ components of the reaction gas G formed in the upper furnace 2 , 51 are converted to CO on the hot coke layer. The coke consumption is compensated for by the addition of coke 13 through the feed lines 12 or according to the exemplary embodiment according to FIG. 4 by the central charging device 52 . To reduce the coke consumption, it is provided in the embodiment according to FIG. 2 to supply coal 28 in the transition area from upper furnace 2 to lower furnace 3 and to burn it by means of oxygen 30 . The resulting CO ₂ is also converted into CO at the coke bed K. Again, the addition of calcium-containing material, such as. B. limestone in powder form, may be provided to promote the rapid formation of slag and improve the fluidity ver.

K Sauer can also be in the lower furnace in the area of the coke fill are blown in, so that here too temperature ranges of over 2000 ° C.

Pure oxygen is preferably used as oxygen (purity 99%  or more), although for economic and other reasons too industrial oxygen with an oxygen content of 96-97% or even about 90% can be used. Furthermore, in the Smelting gasification furnace also liquid oxygen as oxygen source are injected, which is so gassed that, for example a gas with a pressure of 2-5 bar is obtained without ir blower is necessary.

In the coke bed K in the or the combustion and Melting zone (s) V gaseous Pro not yet completely burned burn out products completely. Soot is in the reaction tanks burned or reacted or to reduce feed fen exploited.

With coke sizes of 10-100 mm there is K and in the coke bed the fixed loading bed has good gas flow and a problem guaranteed free dripping of the molten components. With the addition of metal oxide-containing feed material in the slag flowing or dripping through the coke bed K. F contained metal oxides by means of coke and reduced coal Substance of the coke bed K is in the flowing or through flowing melt S solved.

The dust discharge from the reaction containers is low, since the coke bed K acts as a dust filter and trap as well as an adsorption and absorption medium. In addition, the injection of water and / or water vapor through the lines 58 described in FIG. 5 can be provided, so that here additional cooling of the coke bed K is achieved or endothermic reactions take place, so that here additional cooling and retention possibility for dust - And gaseous components is formed.

The fact that a fixed bed is formed in the upper furnace on the coke bed K and or in that both the melting constituents and the gaseous reaction products of the feed are at least partially passed through the furnace in cocurrent results in an intensive material and heat output exchange. 1-3 and 5, an intensive reaction between the molten and gaseous components is achieved by the direct current of feed or molten constituents and reaction gas G, in particular in the reaction vessels according to FIGS . Adequate heat transfer and heating of the feed material is guaranteed, especially in the fixed loading bed. By adding the solid feed to the upper furnace, sufficient service life for the furnace lining can also be achieved. On the one hand, the added charge protects and cools the furnace lining, and on the other hand, the liquid slag and smelting components also help to protect the furnace lining. Metal oxide-containing, for example FeO-containing, molten constituents are immediately reduced by the added coke and / or the carbon monoxide that forms.

Furthermore, the exhaust gas is almost free of nitrogen oxide (NO _x ), since nitrogen oxide formed in the coke bed K is broken down again at the latest.

The be from the thermal waste treatment in the rotary kiln knew disadvantage that the burnout of lumpy waste, which for tends to foam and / or its slag does not disintegrate in the devices according to the invention or the invention Procedure not. Due to the high temperatures in the upper furnace prevents a porous protective layer from surrounding the above Forms pieces that the material and heat exchange and thus one further burnout prevented. For example, charred filter cake lumps  from biological wastewater treatment completely - and not only on the surface like in rotary kilns - and burn to the core constantly out.

Also the disadvantage known from rotary kilns that when task Degassing and gasification of drums with high calorific liquids as well as burning after the barrels have spilled or burst quickly runs that a local lack of air and soot ent ent stands, which ver only partially in an afterburning chamber burns and is poorly separated in the flue gas cleaning, does not occur.

In the devices according to the invention melted barrels zen in the upper furnace. Liquids in barrels can be in quantities of Depending on the calorific value, 10-20 kg are safely placed in the upper furnace be. The oxygen excess in the upper furnace is generally sufficient mean to burn these amounts without sooting. Bran Other soot quantities that could always arise locally can be found in the Upper furnace or lower furnace always enough oxygen or coal dioxide and sufficient temperatures for combustion or formation of carbon monoxide. The control of the combustion in the upper furnace can by specifying a certain amount of combustion air or acid Amount of substance and / or abandonment of the amount of waste depending on temperature or other movement 02460 00070 552 001000280000000200012000285910234900040 0002004030554 00004 02341 parameters. Air Excess numbers from 1.2 to 1.3 may be sufficient. But excess air numbers of over 2.0 are also possible.

When liquids tend to explode or deflagrate with these sufficient amounts of additives, e.g. B. sand, too are given. This makes it possible to burn Letting liquids run slower in containers.  

It is also possible to use liquid waste in a prep riding level, e.g. B. with sawdust to mix, so that one in essential puncture-resistant mass arises that the invention Reaction containers can be supplied.

Doughy or highly pasty wastes can be used in larger quantities, e.g. B. in larger containers, such as 60 kg drums, are added. The degassing and gasification is such that a complete burnout is guaranteed. Such containers are preferably added through the double lock 6 b.

In addition to the essentially CO ₂ -free and very calorie-rich gas, which can be used for various purposes, in particular the claims, the slag F and melt S are obtained as further products. Depending on the composition and quantity of the various additives and / or feed materials, slags F and melts S are obtained which, after cooling and possibly quenching, are used as raw materials or feedstocks in the steel, metal, cement, glass or water glass industry can be. An iron and / or metal-rich melt can be used after cooling in the steel or metal industry when smelting or melting ores or metal-containing materials. After cooling, a calcium-rich slag or melt can be used and utilized in the cement industry, for example, and a silicon and alkali-rich slag or melt can be used in the glass industry. After passing through a reaction container according to the invention, the slags are very well burned out when the process according to the invention is carried out and can also be used as granules in the construction industry or disposed of without thought, since the glassy structure of the slag contains harmful substances in their water-insoluble form.

Claims (54)

1. Process for the thermal treatment of waste materials, such as domestic waste, commercial waste, industrial waste, building rubble, filter dust, sewage sludge, packaging material, suspensions, solutions or the like, in a reaction container in which waste material present at least in solid and / or lump form in the Reaction vessel is supplied to a combustion and melting zone in which it is heated to the point of liquefaction under the combustion of carbon and / or carbon-containing fuel when a reaction gas is formed, characterized in that the reaction vessel with waste material to be treated thermally, coke and possibly calcium-containing Material, in particular special lime (CaO) or limestone (CaCO ₃ ), preferably in excess, is fed and the feed in the reaction vessel at least one combustion and melting zone, which is arranged at least substantially outside of a coke bed formed in the reaction vessel and from born is formed, fed and melted there to form the reaction gas, and that the reaction gas after at least area-wise contact with the molten constituents of the charge before it emerges from the reaction container through one for the conversion of carbon dioxide (CO ₂ ) in carbon monoxide (CO) sufficiently high temperature coke bed is passed. 2. The method according to claim 1, characterized, that the solid and / or lumpy loading of a preference as in the upper region of the reaction container at least in  Ver formed above the coke bed combustion and melting zone is fed and the reaction gas in cocurrent with the melted feed stock divide by below the combustion and melting zone Coke is carried until the gas flow has been as exhaust gas Lich or led out of the top of the reaction vessel becomes. 3. The method according to claim 1, characterized, that the loading preferably radially around the at at least partially arranged centrally in the reaction vessel Coke poured around combustion and smelting zone is supplied and the reaction gas through the coke bulk tion as exhaust gas upwards or laterally from the rear action container removed and the melted load ingredients down through the coke bed the. 4. The method according to any one of the preceding claims, characterized, that the solid and / or lumpy loading by a in combustion space formed in a free space of the reaction container tion and melting zone is performed. 5. The method according to any one of the preceding claims, characterized, that the melted feed components below the Lump of coke at the bottom of the reaction vessel as a melt and / or slag bath are collected or collected.   6. The method according to any one of the preceding claims, characterized, that coke, waste and possibly calcium-containing material alternately in layers, above the at least a combustion and melting zone to the reaction vessel be performed. 7. The method according to any one of the preceding claims, characterized, that at least one combustion and melting zone laterally and / or an oxidizing agent from above, in particular their air or, preferably technically pure, oxygen, is fed. 8. The method according to any one of the preceding claims, characterized, that the coke bed laterally has an oxidizing effect tel, especially air or, preferably technically pure, Oxygen, is supplied. 9. The method according to any one of the preceding claims, characterized, that at least one combustion and melting zone and / or the coke bed laterally and / or a fossil from above Fuel such as coal, petroleum or natural gas is supplied. 10. The method according to any one of the preceding claims, characterized, that solid waste of at least one combustion and Melting zone in lumpy or granular form, if necessary after previous grinding, is fed.   11. The method according to any one of the preceding claims, characterized, that up to 60% of the coke fed is replaced by coal will. 12. The method according to any one of the preceding claims, characterized, that layer as a further loading of the reaction container wise or as a mixture of metal oxide-containing particles, preferably wise iron ore, especially in fine-particle form, and / or additives such as lime or other blast furnace oil substances, and / or silicon oxide and alkali oxide Substances and / or coal at least one combustion and Melting zone are fed. 13. The method according to claim 12, characterized, that the further loading to form another Re action gas also in the at least one combustion and melting zone melted and preferably in cocurrent with the further reaction gas through the coke bed is, the melt in the melting and / or slag bath caught at the bottom of the reaction vessel and the rest Reaction gas as exhaust gas preferably from the side of the reactor ons container is brought out. 14. The method according to any one of the preceding claims, characterized, that coke, waste and further feed to the reak tion container are fed as a mixture from above.   15. The method according to any one of the preceding claims, characterized, that the feed melted in the reaction vessel substances together in the smelting and / or slag bath on the bo that of the reaction container and the gaseous Reaction products together as waste gas from the reaction containers are withdrawn. 16. The method according to any one of the preceding claims, characterized, that the feed in the reaction vessel several Ver combustion and melting zones is supplied. 17. The method according to any one of the preceding claims, characterized, that in the area of the reaction gas withdrawal in the reaction vessel water vapor and / or water and / or alkali, ins special calcium-containing material introduced and with the Reaction gas is brought into contact. 18. The method according to any one of the preceding claims, characterized, that solid and / or lumpy and / or as sludge gender, pasty waste material at least partially in one upstream or assigned process stage first in one or more further reaction vessels of a pyro supplied lysis, in particular coked and / or charred, and the solid reaction product of this process stage the at least one combustion and melting zone of the reak tion container supplied and the gaseous reaction product this stage in the smelting and / or slag bath  and / or at least one combustion and melting zone of the Blown or injected reaction vessel and / or on is blown. 19. The method according to any one of the preceding claims, characterized, that in pasty or pasty form, especially as sludge, present further waste material at least partially in egg ner further upstream or assigned method stage first in one or more further reaction areas hold, in particular by means of a so-called grinding rock tion, is dried and the solid reaction product of this further process stage of the at least one combustion and melting zone of the reaction vessel supplied and the gas shaped reaction product of this further stage in the melting and / or slag bath and / or at least one Combustion and melting zone of the reaction vessel turned on blow or injected and / or inflated. 20. The method according to claim 18 or 19, characterized, that in at least one reaction vessel upstream or assigned waste pyrolysis and / or waste drying further waste present in liquid form blowing or being injected. 21. The method according to one or more of claims 18-20, characterized, that parts of the solid reaction products of the upstream or assigned one or more process stages  Blown in the melt and / or slag bath and / or inflated. 22. The method according to one or more of claims 18-21, characterized, that the exhaust gas from the reaction vessel at least partially and if necessary after going through gas cooling or waste heat utilization one or more reaction vessels of one or more ren upstream process stage (s) is supplied. 23. The method according to any one of the preceding claims, characterized, that the exhaust gas from the reaction vessel is partially recycled and in the area of the coke bed and / or at least one Combustion and melting zone in the reaction container is directed. 24. The method according to any one of the preceding claims, characterized, that further waste in liquid form in at least one combustion and melting zone is blown in or is injected. 25. The method according to any one of the preceding claims, characterized, that further waste material present in liquid form pre-gaseous reaction product of the one or more switched process stage (s) admixed and with this in the reaction container is blown in. 26. The method according to any one of the preceding claims,  characterized, that further waste material present in liquid form returned or that of the one and / or more switched process stage (s) admixed exhaust gas and with this in the or the respective further reacti ons container is blown. 27. The method according to any one of the preceding claims, characterized, that in the smelting and / or slag bath coal dust will blow. 28. The method according to any one of the preceding claims, characterized, that in the molten bath and / or the slag and / or above of the melting and / or slag bath but below the Ab gas escaping oxygen is blown into the reaction vessel becomes. 29. The method according to any one of the preceding claims, characterized, that the melting and / or slag bath generated electrically Additional heat energy is supplied. 30. The method according to any one of the preceding claims, characterized, that the process in the reaction vessel with a pressure of 1-10 bar, preferably 2-5 bar, is carried out. 31. The method according to any one of the preceding claims, characterized,  that the reaction vessel with a mixture of lumpy Waste, generated in an upstream process stage solid reaction product, coke, coal, iron ore and zu is loaded with impact materials, the added mixture carbonaceous material in a proportion to Contains ore of <0.7. 32. The method according to claim 31, characterized, that the amount of carbon halide contained in the mixture material contains up to 60% coal. 33. The method according to claim 31 or 32, characterized, that the carbonaceous material except for the Re ore required proportion of oxygen preferably technically pure oxygen, to carbon monoxide (CO) is burned. 34. The method according to any one of the preceding claims, characterized, that the sensible heat of the withdrawn from the reaction vessel Exhaust gas is used to generate steam. 35. The method according to any one of the preceding claims, characterized, that the exhaust gas of the reaction vessel for synthetic Er generation of liquid hydrocarbons or for production of a synthesis gas is used. 36. The method according to claim 35,  characterized, that the exhaust gas for methanol or oxo synthesis or Reduction of iron ores is used. 37. The method according to any one of the preceding claims, characterized in that the exhaust gas from the reaction vessel is used to produce tri-mellitic anhydride (C ₉ H ₄ O ₅ ). 38. Method according to one of the preceding claims, characterized, that the exhaust gas from the reaction vessel is at least partially egg Nem CHP plant, in particular a combined heat and power plant Combustion is supplied. 39. Method according to one of the preceding claims, characterized, that the exhaust gas from the reaction vessel at least partially for Heating or melting of scrap is used. 40. Device for performing the method according to one of claims 1-39, consisting of a shaft furnace-like, substantially closed reaction container ( 1 , 1 a, 1 b, 1 c) with upper furnace 2 , 51 , lower furnace 3 , 55 and frame 4 , Wei terhin at least one, the reaction vessel ( 1 , 1 a, 1 b, 1 c) gas and pressure-tight charging device ( 6 , 52 , 56 ), lines ( 7 ) for supplying an oxidizing agent ( 8 ) and, if necessary a fuel ( 9 ) in the reaction vessel ( 1 , 1 a, 1 b, 1 c) and lines ( 15 , 53 ) for leading exhaust gas ( 16 ) out of the reaction vessel ( 1 , 1 a, 1 b, 1 c) and tapping lines ( 18 , 19 ) for removing slag (F) and melt (S), wherein in the reaction container ( 1 , 1 a, 1 b, 1 c) a coke bed (K) and one lying on or adjacent to it Solid bed of feed material are to be formed, characterized in that the feed material thermally Treating waste ( 21 ), coke ( 22 ) and possibly calcium-containing material ( 24 ) and the reaction vessel ( 1 , 1 a, 1 b, 1 c) in the transition area from the solid bed from the loading material to the coke bed (K) in the direction of flow of the reaction gas (G) has a cross-sectional expansion ( 3 c). 41. Apparatus according to claim 40, characterized in that above the cross-sectional widening ( 3 c) the wesent union cylindrical furnace ( 2 ) with mouths of Lei lines ( 7 ) for supplying oxygen ( 8 ), fuel ( 9 ), calcium-containing material ( 10 ), water vapor ( 11 ) and water is formed. 42. Apparatus according to claim 40 or 41, characterized in that the lower furnace ( 3 ) in the region ( 3 c) of the cross-sectional extension has supply lines ( 12 ) for supplying coke ( 13 ) and calcium-containing material ( 48 ). 43. Device according to one or more of claims 40-42, characterized in that the lower furnace ( 3 ) at least in the area ( 3 c) of the cross-sectional extension leads ( 38 , 49 ) for supplying oxygen ( 39 , 50 ). 44. Device according to one or more of claims 40-43, characterized in that the lower furnace ( 3 ) in the transition to the frame ( 4 ) has a loading area ( 3 a) with cross-sectional constriction, in which exhaust pipes ( 15 ) from the lower furnace ( 3 ) lead out. 45. Device according to one or more of claims 40-44, characterized in that the upper furnace ( 2 ) further feed lines ( 31 , 32 , 33 , 37 ) for the supply of fuel ( 9 a), oxygen ( 8 a), liquid according to waste material ( 34 ), gaseous waste material ( 35 ) and a feed or recirculated exhaust gas ( 36 ). 46. Device according to one or more of claims 40-45, characterized in that the upper furnace ( 2 ) in the transition to the lower furnace ( 3 ) has a cross-sectional area ( 2 d) with feed lines ( 27 , 29 ) for coal ( 28 ) and oxygen ( 30 ). 47. Device according to one or more of claims 40-46, characterized in that the frame ( 4 ) has an additional electrical heater ( 20 ). 48. Device according to one or more of claims 40-47, characterized in that in the region of the frame ( 4 ) and / or the Unterofenberei ches ( 3 a) further feed lines ( 41-46 ) for the supply of oxygen ( 40 ), Fuel ( 9 c) - preferably coal dust -, liquid waste, gaseous waste ( 35 ) or exhaust gas ( 36 ) are formed. 49. Device according to one or more of claims 40-48, characterized in that in the region of the mouth of the gas exhaust lines ( 15 , 53 ) a cross-sectional area with inlets leading into the furnace interior ( 58 ) for supplying water vapor and / or water and / or alkali-containing, in particular calcium-containing, material is formed. 50. Device according to one or more of claims 40-49, characterized in that in the lower region of the upper furnace ( 51 ) a plurality of feed lines ( 54 ) distributed radially on the periphery of the furnace for supplying waste material to be treated thermally ( 21 ), coke ( 22 ), possibly coal ( 23 ), aggregate ( 24 ) and possibly further feed material ( 25 ) lead in and that in this central region supply lines ( 7 ) for supplying oxygen ( 8 ), possibly fuel ( 9 ), possibly Limestone ( 10 ) and possibly water vapor ( 11 ) are arranged. 51. Apparatus according to claim 50, characterized in that the reaction vessel ( 1 c) is provided on the gout side with a central charging device for coke ( 13 ) and calcium-containing material ( 48 ), below which exhaust pipes ( 53 ) lead out of the upper furnace ( 51 ) . 52. Apparatus according to one or more of claims 40-51, characterized in that the lines ( 7 , 29 , 31 , 32 , 33 , 37 ) opening in the area of the fixed loading bed into the upper furnace ( 2 , 51 ) for liquid or gaseous substances are at least partially aligned such that they blow against gravity in the direction from below obliquely upward substances into the reaction container ( 1 , 1 a, 1 b, 1 c). 53. Device according to one or more of claims 40- 52, characterized in that the reaction container ( 1 , 1 a, 1 b, 1 c) is designed for operation at a pressure of 1-10 bar, preferably 2-5 bar is. 54. Device according to one or more of claims 40-53, characterized in that the reaction container ( 1 , 1 a, 1 b, 1 c) one or more waste treatment devices, in particular a waste pyolysis device ( 59 ), a sludge drying device ( 60 ) and / or a storage device ( 61 ) for liquid waste and associated with the reaction vessel line ( 62 , 63 , 65 , 66 , 68 , 69 , 71 , 72 ).