LT3502B - Method for recircling and utilitization of waste and device for its realization - Google Patents

Abstract

The present invention relates to methods of waste processing and usage where unsorted waste is processed with at least one high temperature flow effect. The neutralised compound which is compressed with liquid using a load method to compact packages, while variety and structure solidity are preserved. The flow effect is maintained through pressing, and later the waste compound is led in appropriate form to a hot channel (above 100 degrees C). The compound is pressed in the channel, and when there is an appropriate contact with the walls of the channel it is kept until the primary liquid evaporates and mechanical counterforce of single neutralized components is voided and partial gas exhaust takes place. A hard lumpy conglomerate, which is pushed out of the channel and is stable in form and structure, is led to a high temperature reactor of at least 1,000 degrees C, where it forms a filling, pervious to gas. After abstracting some metal components and using the energy of the gas extracted from neutralized waste, the residual fluid material is led to a second high temperature melting process in one of the method versions. In the melting process, an energy characteristic of the alloy is used and inactive manufacturing products and/or semi-manufactures are produced.A high temperature is maintained in the gasification zone. The hot gas produced is used to warm the non-pyrolised neutralised waste compound, it is cooled and passes through the temperature area, needed for producing chlorinated hydrocarbons. The temperature is dangerous.Another method implementation is to use the first melting bath of 1,300 degrees C and the second melting bath of 1,500 degrees C to 1,800 degrees C coupled in tow. The second melting bath removes all non-homogeneous structures and toxic inserts remaining in the first melting bath in certain cases.

Description

The present invention relates to a method for the decontamination and utilization of all types of waste, wherein the unsorted, untreated, solid and / or liquid, industrial, household and special debris containing any harmful substances, as well as scraps of industrial products are subjected to a thermal flow according to claim 1.

The invention also relates to an apparatus for carrying out this method.

Known methods of waste decontamination do not solve the growing problem of litter, which is a major contributor to environmental pollution.

Scrap materials from industrial materials such as cars and household goods, as well as oils, batteries, varnishes, paints, poisonous slurry, medicines and hospital waste must be treated separately by legally prescribed decontamination measures. In contrast, household waste, which is an uncontrolled heterogeneous mixture that can contain fractions and organic constituents of almost all types of special waste, has not yet been categorized in terms of environmental contamination ratio for decontamination.

In landfills, household waste is improperly dumped, rotting gas and carbon dioxide are released into the atmosphere in an uncontrolled manner, waste liquids containing harmful substances and eluates pollute the groundwater.

It has already been proposed to compost the organic components of household waste and sludge-treated waste to reduce the amount of trash being treated. However, it also ignores the fact that these organic materials are heterogeneous and contain many non-volatile toxic components, such as chemicals, drug and heavy metal residues that remain in compost and return to plants and animals for bio-metabolism.

Garbage is also reduced by adding so-called valuable materials to the recycling process. However, in this case, the costs of separating and preparing this waste remain neglected; repeating the recycling process increases the cost and burden on the environment as the use of the resulting products decreases.

In known waste incineration plants, the decontaminated waste mixture passes a wide range of temperatures up to about 1000 ° C. At these temperatures, mineral and metallic residues do not dissolve. Typical for persistent solids, energy is underused or underutilized. The short-term presence of waste at elevated temperatures and the high generation of dust due to the high nitrogen content of the combustion air in the non-pressurized constituent waste contribute to the hazardous formation of chlorinated hydrocarbons. This has led to the incineration of the waste gases from waste incineration plants at higher temperatures. To justify the large investment in such Equipment, hot abrasive and corrosive exhaust gas with a high proportion of dust is removed through a heat exchanger. After a relatively long period of time in the heat exchanger, the recombinant synthesis results in the re-generation of chlorinated hydrocarbons, which bind to the dust introduced and eventually become highly toxic filtrates. It is not yet possible to estimate the consequences of the damage and the cost of repairing it.

Despite the high technical costs at the prior art, approximately 40% of the waste to be decontaminated remains in the form of an ash, slag and highly toxic filter, 3503 B, which is comparable in terms of hazard to radioactive fallout and has to be substantially decontaminated.

In order to reduce the amount to be deposited, it is self-evident that the metal components of the retained materials must be separated and used separately. The remaining ash and slag is subjected to a high temperature melting process with high energy consumption. Due to the heterogeneous molten starting materials, the slag is inhomogeneous and contains a significant proportion of organic residual material surrounded by non-oxidised liquid alloy.

Sudden cooling of the alloy in a water bath produces a heterogeneous alloy granulate which, at its thermal fracture sites, breaks down uncontrollably so that the harmful substances inside it become leached again. The high energy consumption of up to 200 liters of oil per tonne of alloy remains untapped, as the alloy granulate thus obtained can only be used as a filler in road construction and so on.

The temperature spectrum of the previous pyrolysis processes in conventional reactors is similar to that of waste incineration. The gasification zone is dominated by high temperatures. The resulting hot gas is used to heat the non-pyrolysed mixture of decontaminated waste, while it cools and passes an important temperature range of chlorinated hydrocarbons.

All known methods of pyrolysis of unsorted, unbound and dewatered wastes prevent the introduction of a gas-permeable core layer that requires excessive energy consumption for insufficient gas and long waste in the reactor.

Thermal currents and internal gas pressures produce a large amount of dust, which requires a high filter capacity. The production of water requires the supply of separately produced hot steam in the gas formation area, as well as domestic steam. The residual solids, as a rule, are not meltable but have to be taken to separate decontamination and can therefore be compared to a conventional incinerator.

The gas passes through a cracker prior to purification to produce ecologically non-hazardous useful pure gas. In addition, it is known how to utilize the heat energy inherent in hot gas when using a heat exchanger. At the same time, the gas in the heat exchanger generates chlorinated hydrocarbons, which are then released thermally using the resulting gas.

A significant disadvantage of using a shaft furnace for pyrolysis is that in the furnace, the waste to be pyrolysed accumulates and forms bridges, so such reactors are equipped with auxiliary mechanical means such as mixing rods, vibrators, etc., although this has so far not satisfactorily solved this problem.

Due to the mechanical friction of partially sharp-edged material waste into the furnace walls, rotary tubular and laminated carburetors have long downtime, very high dust formation and require gas-tight, technically costly locks. There is a considerable amount of maintenance work involved which is very costly.

In another known thermal decontamination method, the mineral and metal components are initially separated from the organic, and the separated organic components are dried and crushed (see German Patent

No. 4004336, TIKBO7B1 / 24, publ. September 12, 1991). The pulverized materials are introduced into a high temperature incinerator and immediately decomposed with oxygen or air enriched in oxygen, decomposing together with the destruction of harmful materials (see PCT Application 92/14562, BO9B 3/00 ONLY, 09.09.1992).

Although these methods produce satisfactory results from an ecological point of view, they have significant disadvantages. For example, it is not possible to decontaminate composite structures of liquid waste and solid waste. This also results in high costs.

Also known is pyrolysis recycling, whereby the waste is initially mechanically shredded and heated to a temperature of 116-371 ° C, thereby drying and releasing steam and other volatile components. The remaining dry materials are pyrolyzed at 371-760 ° C. Volatile components are further released at this stage. The remaining solid was further heat-treated at 760-1649 ° C. The remaining solids are removed from the furnace and recovered for further use. Liquid and gaseous materials obtained by pyrolysis are divided into fractions for further use (see U.S. Patent No. 4,977,840, F23G5 / 12 ONLY, published December 18, 1990).

A device for carrying out this method is described in the same U.S. Patent No. 4,600,151. No. 4,977,840, consisting of waste shredding and several waste heating and heat treatment vessels. These capacities are interconnected with transmission lines and conveyors.

The combustion and pyrolysis methods and devices described above have the common disadvantage that liquids or solids vaporized during incineration or pyrolysis decompose with incineration or pyrolysis gas before reaching the required temperature and lifetime for the destruction of all harmful materials. As a result, additional incinerators are connected to the incinerators and the cracker stages to the pyrolysis units, which makes the process complicated and energy intensive.

The present invention provides a process which, in any mixture of starting materials, removes the above disadvantages without polluting the environment, and at the same time allows to obtain highly valuable, incompletely prepared or prepared industrial, widely applicable products from residual materials, while minimizing the technical costs thereof. and the cost of being.

It is also an object of the invention to provide an appropriate device for carrying out the method according to the invention.

With respect to this method, the solution of the problem is achieved by virtue of the features set forth in claim 1 of the invention.

Useful improvements of this method are set forth in claims 2-14 of the invention.

with respect to the device, the solution of the problem according to the invention is set forth in claim 15 of the definition of the invention, and paragraphs 16 et seq.

Due to the breakage of industrial articles, such as non-woven refrigerators, washing machines, electrical and electronic appliances, cars disassembled in bulk, maintaining the mixing and bonding structure of the scrap, together with unsorted and untreated bulk litter and liquid waste, compressed into compact packages, moves through temperature steps in an upward direction without intercooling, and optimizes energy consumption with minimal waste volume, that is, by optimizing the unit's dimensions. The pressure supply support associated with the shape and strength contact of the waste compact packages at the reaction tank walls at least at one of the lower temperature stages, while guaranteeing a good heat transfer, rapid warming up of the compressed waste and high throughput of this thermal treatment step. Rapid cooling after complete heat treatment prevents unwanted re-production of harmful substances.

This method can be implemented without gateways; preventing harmful substances from escaping the process uncontrollably is reliably prevented.

Because the lower temperature stage of pressure contact with the reactor walls passes through the oxygen cut-off, the advantage is that the evaporation of the liquid in the waste and the subsequent degassing occurs under aggravating conditions. For example, dioxin production requires oxygen. Therefore, in order to complete the lower temperature treatment, the resulting materials must be conveyed to at least one high temperature stage by supplying oxygen, which has the advantage that organic carbon can be gas-supplied and that water vapor from waste water can be incorporated into the water. and the reaction of the gas. The supply of oxygen to this stage of the reaction allows the temperatures required for the indicated reactions to be reached. At the same time, the temperature range of 100 ° C to 600 ° C for lower temperature stages and temperatures above 1000 ° C for high temperatures guarantees the removal of gas from the organic material to the desired extent, gasification of pure carbon, water and gas reaction and, above all removal.

Due to the minimal void volume of the bulk waste due to compacting, the solid components of the solid waste are mechanically rigidly united, the excess liquids, together with the resulting compact packages, are compressed into an elongated externally heated conduit, forming a gas impermeable plug before the conduit. gas becomes a gateway function. The fluids do not need to be individually decontaminated and the heat insulated air does not need to be heated in bulk. The thermal conductivity of the compact material obtained by increasing retraction pressure is significantly improved by its available metallic and mineral materials and high density. High decontamination capacities are also achieved in low-design units without costly pre-treatment techniques such as separable collection and the technically demanding preparation, crushing, disassembly, drying and briquetting.

components measure function

The process is characterized in that the pressed compact packages holding the pressure load are pressed into a preheated conduit above 100 ° C, where, due to the existing gas pressure, it contacts the conduit walls with a hernia until the introduced liquids and volatile materials are evaporated and , and until the retrieved organic at least partially takes over the binder In this case, pyrolytic decomposition of the organic moieties in the channel must not occur or occur partially, although partial decomposition may be quite desirable. It is sufficient that all small parts are combined and conglomerates of stable shape and structure are produced. In the process of the present invention, shortly after the decontaminated waste in the heated passage, a solid shaped pressed structure is formed which binds together the fine particles and dust that are brought with the waste, because increased gas accumulates rapidly in the peripheral areas of the formation. At least the components of the organic constituents are thus plasticized by eliminating the reversibility of such debris constituents. With adequate strength of contact with the walls, the extruded material of the waste material flows through the process gas, which is formed on the hot wall of the duct and further inside it. This waste material sticks together, rocks and interacts with each other, releasing its moisture so that dust-free, stable form and structure conglomerates are produced up to the outlet end of the canal. These conglomerates of solids leaving the channel end and falling into the high-temperature gas generator shaft enable gas-free, dust-free bedding in a connected high-temperature reactor to be completely converted into gas at high temperature.

The compact packages, first heat-treated, according to the invention enter the high temperature gas generator immediately after leaving the heated channel. This high temperature reactor is characterized by maintaining a temperature of at least 1000 ° C throughout its volume.

The energy emitted from the central portion of the high temperature reactor may be utilized to affect the solids conglomerate obtained at the lower temperature by the flow of heat emitted at its inlet to the high temperature reactor such that the conglomerate will decompose into stable shaped pieces. These pieces are charred by lightning, at least on the surface of the pieces, upon entering the high temperature reactor.

The briquettes, with their characteristic energy, form a loose, gas-permeable layer of trash in the high-temperature gas generator.

Initial heat treatment in the duct prevents the formation of explosive gas mixtures throughout the system. The whole of the gaseous and solid wastes is exposed to a high temperature stream until all thermally reactive materials are destroyed. Since the organic constituents of the solid particles are pyrolitically decomposed immediately into the high temperature reactor, at least in their outer .zones, the debris column can be trapped and bridges formed and adhered to the reactor walls. Above the fill, a pure carbon-containing fluidized bed is formed, whereby water vapor from the fluid introduced with the compacted parent material passes through a heated channel. This ensures a water-gas reaction that has the advantage of eliminating the need for extraneous vapors. The gas-permeable filler allows a known Boudouard reaction to occur simultaneously. The carbon dioxide produced by gasification of pure carbon with oxygen as it passes through the waste column is converted into carbon monoxide.

The high-temperature reactor, which passes through all the gases, has a temperature of at least 1000 ° C above the filler for a long time, which ensures the decomposition of chlorinated hydrocarbons and the decomposition of long-chain hydrocarbons. Condensation, such as tar and oil, is reliably avoided.

The synthesis gas mixture, which has a temperature of at least 1000 ° C and is left in a high temperature reactor, is suddenly cooled to 100 ° C and evacuated to prevent the formation of new chlorinated hydrocarbons.

The melting of solids by high temperature flow inside the reactor occurs mainly at temperatures of 2000 ° C and above. These temperatures occur when pure carbon is converted to gas in the presence of oxygen.

In the high temperature reactor melting area, the bottom is filled with molten inorganic constituents, i.e. i.e., glasses, metals and other minerals. Part of the heavy metals contained in solids, when oxygen is metered in, is discharged in elemental form in a reducing atmosphere, forming alloys with other components. The liquid form is removed and fractionated if necessary.

At processing temperatures of 2000 ° C and above, most of the pyrolysis coke is burned during the exothermic reaction, with the resultant oxidation of the remainder of the components and the complete mineralization of the mineral components. However, leaky alloys exhibit a significant degree of inhomogeneous structure when the waste is unsorted. The higher melting components, such as pure carbon, certain metals, are still in a solid state and form inserts such that these slag residues cannot be properly utilized.

Therefore, it is useful and claimed in the proposed process that liquid residual products, which represent on average one percent of the initial volume of the decontaminated waste material, are further processed using the synthesis gas obtained from the thermal homogenization process. The alloy is clarified at 1800 ° C in an oxidizing medium until bladder-free, a homoLT 3502 B generic high temperature alloy. In one embodiment, the non-homogeneous alloy leaving the high temperature reactor may initially be significantly agitated in the collection tank, or may be partially due to alloy leakage. Sufficient alloy volume, in the continuous state of the art, is formed during the clarification process or subsequent fractionation by density separation, if desired. High temperature smelting removes all inhomogeneous structures without exception, so that they cannot be washed out over a long process. Such high temperature melting is characterized by a complete transformation of the starting materials.

The advantage of the proposed process is that the product obtained by high-temperature smelting can be processed into a wide range of fully-fledged industrial or semi-finished products. This alloy can be used to produce a high quality industrial product that is close to natural, utilizing its inherent energy, without intercooling. For example, the alloy can be spun into mineral fibers, or high-quality machine parts such as gears and the like can be made from this alloy by casting. Other fully-fledged industrial products can be processed using known methods of forming and reformatting. Low volume and weight insulators are blown. This requires optimum viscosity for the high temperature alloy, depending on the article and the method used, such as casting, twisting, shaping or reshaping.

For the first time, universal versatile decontamination is possible in the manner described above, which requires no pre-treatment of waste, such as crushing, separation, drying and briquetting, as well as recycling of all types of working materials. The resulting fluids are energetically utilized in the water-gas reaction, and all of the gaseous, liquid, and solid decontaminated products heated to above 1000 ° C are maintained in a high temperature reactor when cooled to reflux until the chlorinated hydrocarbons are thermally decomposed. , after separation of the metal fractions using their inherent energy, they are further processed into fully fledged industrial products.

This process according to the invention is advantageously carried out by means of a device which is capable of at least one de-oxygenation and at least one oxygen-based heat treatment and in which all the reaction tanks of the heat treatment stages are non-locked to each other. This has the advantage of avoiding clutter that is almost always available on gateway devices. Harmful substances are not allowed to enter the environment uncontrollably.

The reaction equipment, together with any facility for the disposal of mixed decontaminated waste, shall be disposed in a single, linear conveyor belt such that the fixed point of thermal expansion of the aggregate of equipment is the first step in the heat treatment process at its highest temperature. In this way, the thermal expansion of the reaction device is controlled and can be fully compensated. By choosing a reaction tank with zero thermal expansion point with the highest temperature load, the additional movement load is protected from this part of the thermal load.

It is expedient to position the reaction vessel horizontally in the decontamination of the heat treatment. a heated recess furnace or duct having a rectangular cross-section having a ratio: furnace width / furnace height greater than 2 may be defined by the length of the furnace as follows:

T> 1 S λ / P

-'- 'furnace - ^xr furnace where ^ furnace is the cross-sectional area of the recessed furnace. This inlet passage enables heat treatment with a defective oxygen cut-off. Adhesions to walls that cause difficulties in other furnace systems are eliminated by continuous pushing. The recessed furnace is a stand-alone system. The horizontal arrangement of the push-in oven allows it to be loaded at floor height.

A rectangular furnace cross-section with a cross-sectional pitch / height ratio greater than 2 provides a sufficiently large contact area between the heated furnace walls and the recyclable waste, which results in a rapid warm-up of the recyclable waste. If the furnace length is selected according to the ratio L _kiln> 15 'JF _furnace, it is being sold to waste, if necessary, can be completely and easily remove the gas.

The supporting rollers accept the thermal expansion of the reaction system. Having an unheated zone on the loading side of the stove will have the advantage that filling the stove with compacted loaded waste acts as a gas-tight stopper or gate. This is especially important when the length of the unheated zone of the retractable furnace is given by the ratio:

Frozen ~ Fkurning

In this case, the shut-off plug does not allow gas to escape at minimum oven length.

The exterior warm-up of the intake duct takes place in a way that is advantageous in that the duct is provided with a hood to remove flames and exhaust gases. A similar design allows the use of residual heat from other parts of the unit.

The tight connection of the loading portion of the inlet duct with the outlet portion of the waste compression press provides the advantage that the gas-tight stopper can be formed externally and introduced into the inlet duct so that the longitudinal forces affecting the inlet furnace are minimized. Significant compaction forces are received from the waste compression press. The best compression results are obtained by compaction, first in the vertical and later in the horizontal direction. With its support rollers, the waste compression press is able to follow the thermal expansion movement of the push furnace without interfering with it.

The outlet portion of the inlet passage is tightly coupled to the inlet portion of the vertically mounted high temperature shaft furnace while the gaseous, liquid and solid reaction products are treated at temperatures above 1000 ° C to supply oxygen. The direct, non-locking, solid connection of the feed duct to the high temperature treatment stage shaft furnace reliably prevents any uncontrolled release of harmful substances from this system. The vertical arrangement of this reaction tank ensures that the solid reaction products from the feed furnace, resulting from the decommissioning of the oxygen supply and falling due to the force of gravity to the high temperature reactor, first form a permeable gas bed. Pure carbonaceous substances are initially oxidized to carbon dioxide due to the current of oxygen. Due to the high temperatures of the carbon components, the solids fill from the high temperature reactor solids and can be removed by draining all mineral and metal components. On the surface of a heated, pure carbon filler, the carbon dioxide is partially reduced to carbon monoxide by Boudouard equilibrium.

The vertical shaft furnace is placed at a high temperature approximately the height of its inlet to process the reaction products of the sliding furnace. This allows rapid replacement of the lower part of the reaction tank. This is expedient due to the fact that the lower part of the high temperature reactor must take into account the increased wear due to the extremely high oxygenation temperatures. Separate replacement of this heavily loaded part of the furnace enables a spare part, pre-prepared and already heated, to be brought in as quickly as possible, thus reducing decisively the downtime of the entire unit. After the high temperature treatment, the reactor tank is fitted with a reactor vessel which is tightly connected to it and where the molten metal and mineral constituents from the high temperature zone can be subsequently treated with oxygen and energy. The advantage is also that the solids alloy can subsequently be homogenized. The resulting pure carbon particles are oxidized by high-temperature oxygen treatment to yield a pure product that is immediately reused.

The lower part of the reactor vessel of the high temperature treatment reactor and the vessel of the subsequent heat treatment reactor may be lowered together and tilted at an angle of 90 ° to the base. This reduces the duration of repairs and inspections. Due to the combustion of oxygen in the high temperature reactor solids, the viscosity of the fusible mineral and metallic constituents in the middle of the filler is extremely low, which makes it possible to operate the reactor by draining. The same is true for a temperature after-treatment reactor, which it is expedient to pour directly into a water bath. Upon entering this bath, the molten liquid components are granulated. They can then be easily retrieved from a water bath, such as bucket lifts, for further use. It is expedient to connect the gas outlet portion of the high temperature reactor to a fast acting gas cooler having a water injection device for injecting cold water into the hot gas stream. Rapid cooling of the gas prevents the re-synthesis of harmful substances. Injection of cold water removes fluid and solids particles, brought along by the flow of gas, resulting in a well-purified synthesis gas after rapid cooling.

Because gas pressurization is already carried out in the plunger furnace without degassing the gas, it is expedient that the gaseous waste heat treatment products pass through the whole unit at pressurization and that the unit has a throttle device at the end of the gas path such as an adjustable throttle valve. The design of the sluice-free installation does not pose any problem of gas overpressure delivery. Throttle control at the end of the gas path is the simplest and most reliable form of operation. The simplest and most reliable way of delivering this gas is by limiting the pressure to the water valves.

The described devices can be placed on the loading side in front of any waste-picking and loading devices of the present state of the art, and bundles of known equipment for gas cleaning and utilization. The advantage of using oxygen to convert pure coal into gas is that it does not produce nitrogen in the air, resulting in a significant reduction in gas volumes. Bundled gas purification units can be minimized in size and offer the most favorable prices.

Multiple Arrangements of the described type, when used in parallel with the Arranged Arrangements, provide the advantage that standardization of the equipment components can be achieved, and secondly, the capacity can be easily expanded. At the same time, the cost of equipment is reduced and construction time is shortened.

The invention is illustrated in Figures 1-4.

FIG. 1 is a flow chart of the process according to the invention.

FIG. 2 - characteristic mode parameters, with an example of their realization.

FIG. 3 is a schematic sectional view of a device according to the invention.

FIG. 4 is a simplified view of a device according to the invention implemented in two lines.

FIG. Steps 1 through 8 'of this method are symbolically depicted. The waste, without pre-treatment, i.e. sorting and shredding, is introduced into the 1 'stage where it is compacted. Compacting results are significantly improved with the pressure planes operating in both vertical and horizontal directions. Greater compaction is required here, since the loading opening of the inlet passage in which the 2 'stage of the process occurs is closed by a compressed waste stopper.

The pressurized waste passes the inlet passage in step 2 'without supplying oxygen at temperatures up to 600 ° C. The organic constituents of the waste are degassed. The gas flows through the incinerator waste in the direction of step 3 '. During the passage, they contribute to a good warm-up as well as the intense pressure of the waste into contact with the sliding furnace walls. By continuously attracting highly pressurized waste, the pressure contact is maintained throughout the length of the furnace and the whole of the duct planes so that the removal of gas from the organic components is substantially complete when the waste has passed the inlet duct.

Coal gas, water vapor from natural wet waste, metals, minerals, and organic carbon with the gas removed are co-fed to the 3 'stage of the process, which primarily oxidizes pure carbon to oxygen. Temperatures of 2000 ° C and above dissolve metallic and mineral constituents such that they can be removed in an alloyed state at step 6 '. In parallel, organic carbonation gas compounds are destroyed above the high temperature range of the heated coal bed at temperatures above 1200 ° C. For these temperatures available C, CO _2, CO and H ₂ O equilibrium produces a synthesis gas consisting mainly of CO, H ₂ and CO ₂ to 4 'in a quickly cooled to lower than 100 ° C. Rapid cooling prevents new production of organic pollutants, reduces gas volume and facilitates gas scrubbing that occurs in the 5 'stage. After its synthesis, the gas is very pure and suitable for the intended use. The metals and minerals removed by alloying in step 6 'are further treated with oxygen at more than 1400 ° C in step 7'. At this stage, any carbon residue left over is removed and mineralization is completed. Discharging solids, for example, in a water bath, completes the decontamination process at step 8 '.

Granules, which are obtained by removing solids from a water bath, contain metals, alloying elements and fully mineralized non-metals. Iron impurities can be magnetically separated. Antifouling-resistant mineralized non-metals can be used in a variety of applications, for example in the form of expanded grains or in the processing of mineral fibers, as insulating material or simply as granulate for fillers, in road construction and in concrete.

FIG. Figure 2 is a schematic view of an embodiment of a device according to the invention. The individual sections correspond to the standard mode execution data. It can be seen that the pressure depends on the pressure p and the composition of the waste. Gas removal is a function of temperature T, pressure and waste composition. The introduction of the gas depends only on the existing vapors of pure carbon, oxygen and water, except for pressure and temperature, the parameters of which remain high in the high temperature reactor, so that the introduction of gas is independent of the initial composition of the waste. Thus, according to the invention, regardless of the composition of the waste, synthesis gas is produced which, because of its constant quality, can be used, for example, in gas-jet gas engines.

FIG. The compacting press 1 1 corresponds in structure to a well-known scrap press, which is used to turn cars into scrap metal. The oscillating pressure plate 2 enables the compressor 1 to be loaded with the waste mixture in the perpendicular (dashed) position shown. The pressing plane 3 takes up the left position so that the loading chamber of the press is fully open. As the pressure plate 2 oscillates to reach a horizontal position as shown, the waste is initially compacted in a vertical direction. Thereafter, the pressurizing plane 3 moves horizontally to a position represented by a continuous line receiving the required compaction process in a line and compresses the waste package in a horizontal direction. Front sliding plate 4 rebound forces. After completion, the face plate 4 is pulled out and the pressurized waste plug is pushed against the pressure plate 3, which moves further to the right, into the unheated part 6 of the pushing furnace 5, thus further transporting the entire contents, compacting and maintaining its pressure contact with the channel or furnace. wall. The pressure plate 3 is then returned to the left end position, the counter plate 4 is pushed in, and the pressure plate 3 is rotated back to a vertical position, which is shown in dashed form. The packer 1 is ready for re-loading. The waste compression is so great that the waste plug is impervious to gas when pushed into the unheated part of the pusher furnace 5. The sliding furnace is heated by flame and / or waste gas passing the heating hood in the direction of arrow 7.

As the compressed waste is pushed through the furnace channel 5, the degassed zone 8 widens as shown towards the center plane of the pusher furnace 5, due to the large surface area associated with the rectangular cross-sectional aspect ratio> 2. The high temperature reactor 9 comprises a mixture of pure carbon, minerals and metals compacted by constant pressure during the passage. This mixture is exposed to very high heat radiation in the area of the inlet to the high temperature reactor. The associated rapid expansion of residual gas in carbonising products leads to fragmentation. The solid content of the solid thus obtained in the high-temperature reactor forms a gas-permeable layer 10, in which the pure carbon of the products to be carbonized is initially burned to CO ₂ or CO by the oxygen supplied to the tubes 11. The carbonation gas, which swirls through the reactor 9 over the bed 10, is completely decontaminated. During synthesis gas production, a temperature-dependent reaction equilibrium is established between C, CO ₂ , CO and water vapor removed from the waste. The temperatures present correspond to those in FIG. 2 specified. Synthesis gas in tank 12 is cooled to below 100 ° C by injection of water. The gas-derived components (minerals and / or metal in the form of an alloy) are precipitated in the cooling water, reducing the volume of the gas, facilitating the purification of the gas, which can join the sudden cooling in known Devices.

In the central part of layer 10, which has a temperature above 2000 ° C, the mineralized and metallic components of the waste to be charred are melted. Due to their different densities, they separate and separate. Iron alloying elements, such as chromium, nickel, and copper, form an alloy with the waste iron, while other metal compounds and aluminum oxidize and stabilize as oxide-mineral alloys.

These alloys enter the post-treatment reactor 13 where they are exposed to temperatures higher than 1400 ° C in the oxygen atmosphere formed by the tube 14, if necessary with the aid of gas burners (not shown in the drawings). The carbon particles introduced are oxidized, the alloy is homogenized and its viscosity is reduced.

The bulk discharge into a water bath 15 separates the granular mineral and the iron alloy and then magnetically segregates it.

FIG. 3 shows a post-treatment reactor 13 shown for clarity in a tilted 90 ° position. This reactor 13, together with the lower part of the high-temperature reactor 9, forms a structural unit that can be controlled and a working connection 16 of the unit.

to move the repair sideways off the line after loosening the flange

This line of the device (Fig. 3) is essentially arranged in a row extending over a considerable distance. Changing temperatures as the unit approaches and away from thermal equilibrium allow for significant thermal expansion. When the high temperature reactor 9 is stationary and the pusher furnace 5 is coupled to the compaction pressurizer 1, their wheels 17 can roll along the rails (not shown), but also accept the effects of lateral forces. In the high temperature reactor piping (for example 18), the pleated bellows 19 regulates expansion compensation.

In a simplified view from above (Fig. 4) created in accordance with the invention of Figs. Figure 2 shows the unit's bicycle fulfillment retains the part names. Both sections are supplied alternately from a common waste bin, and both have a state-of-the-art gas washing plant. The throttle valve 20 can be used to set an overpressure that can regulate the gas flow in the unit and is reliably controlled by the water valves 21 (not shown in Fig. 3).

The constant zero point of thermal expansion is between the high temperature reactors 9 and the position of the post-treatment reactors 13 which can be shifted across the main axis of the unit as shown in Figs. 4.

The multidimensional implementation of the inventive devices enables a large degree of adaptability to local conditions, while standardizing the design elements of the machine, reducing costs, improving spare parts supply and maintenance, and reducing machine production.

In another embodiment, unsorted municipal waste is fed in a compact or friable form to a low temperature pyrolysis furnace, also consisting of a horizontally located shaft chamber with front inlet and outlet ends. With the help of a suppressor, unsorted waste is pushed into the inlet end of the pyrolysis furnace and pushed through the furnace shaft, in accordance with intermittent feed. An appropriate temperature gradient throughout the furnace shaft length ensures that at the exit end, the pressurized and gas-free solid residues of the decontaminated waste are removed in the form of solid pyrolysis coke as well as mineral and metallic components. Immediately after the removal of these solid mineral, metal and organic components, it is exposed to an oxygen stream. Solid residues which have not been gasified by pressurization - pyrolysis at temperatures of approximately 700 ° C are substantially incinerated or oxidized, melted or gasified by exothermic oxidation in a connected reactor. A liquid slag is obtained which can be granulated in a water bath. However, such granules have inclusions, heterogeneities which are mineral, metallic or even organic in nature. Such an intermediate indicates that the rapid cooling of the liquid slag causes numerous cracks, cracked surfaces, etc. in the water bath, which also release toxic heterogeneities and do not provide the long-term durability of the required high temperature residual eluents.

Therefore, in this variant of the process, the intermediate product obtained in the first melting bath at a temperature of about 1300 ° C using the primary energy (pyrolysis gas) produced during gas removal is transferred to a second high temperature melting above 1350 ° C, preferably 1700 ° C. C or higher. When this high temperature alloy is cooled, a solid material with a homogeneous structure similar to ceramic is formed.

The fact that the second high-temperature alloy does not usually cool down without additional production operations, and on the contrary, it is further processed, utilizing its inherent high thermal energy, for example into a fibrous or planar intermediate, which is of great importance for the implementation of this process. Fibrous products can be used as valuable reinforcements for building materials or as mineral insulating fibers. The product produced in the proposed manner can perform not only on asbestos fibers but also on high-quality synthetic materials, alloying hard metals and the like. assignable tasks.

In the case where the second high-temperature melting produces structures of irregular surfaces similar to fiberglass, it is necessary to immerse the alloy-cooled centrifugal shaft with a suitably structured surface such that the dispersed liquid currents have an irregularly incised structure. Alternatively, two grinding rollers or a rotating plate can be used instead of the cooled centrifuge shaft. The fibrous structures leaking from these units can be varied depending on the shaft speed and the viscosity of the melt bath.

The following table summarizes the elution stability of the product prepared according to the above procedure.

The values in the table below were obtained by taking samples of the bulk melt of the product of the invention using 80 g disk samples. The basis for these studies was the current Swiss Technical Requirements for Waste (Technische Verordnung fur Abfalle) (TVA), adopted in 1990. December. These products are obtained by a high temperature process at temperatures above 1700 ° C, with changes in material. These products were identified by atomic spectroscopy.

The results show that aluminum and silicon are the major constituents of solids. Concentrations of all heavy metals are so low that they are below the limits established by known methods of measurement, at least much less than the established allowable values for the eluates. All requirements for inert materials are satisfied. Virtually no alkalinization has been detected. Thus, the product obtained in this way is a completely inert substance which by its content meets the most recent environmental requirements, as well as toxic components.

I

Table

H ₂ O - eluate TVA requirement for inert material TVA requirement remnant s material 24 hrs 48 h middle small pH value 7.20 7.14 7.17 6-12 fall 6-12 fall electricity 8.0 7.0 7.5 non- non- conductivity fishing fishing S / cm yeah yeah Ammonium -0.05 -0.05 -0.05 0.5 fall 5.0 fall NH ₄ -N, mg / l Cyanide -0.01 -0.01 -0.01 0.01 fall 0.1 fall CN, mg / l Fluoride -0.1 -o, i -0.1 1 fall 10th fall F, mg / l Nitrite min min min 0.1 fall 1.0 fall NO ₂ mg / L 0.005 0.005 0.005 Sulfide S, mg / l -0.01 -0.01 -0.01 0.01 fall 0.1 fall Sulphite -o, i -o, i -0.1 0.1 fall 1.0 fall SO ₃ , mg / l Phosphate -0.01 -0.01 -0.01 1 fall 10th fall PO ₄ , mg / 1 Chloride Cl, mg / 1 -1 -1 -1 no need. no need. Sulphate -1 -1 -1 no need. no need. SO ₄ , mg / l DOC C -1.0 -1.0 -1.0 20th fall 50 fall mg / 1 AOX ^x Cl mg / 1 -1 -1 -1 10th fall 50 fall

Continuation of the table

Aluminum 0.09 0.07 0.08 1 fall 10th fall Al, mg / l Arsenic As, mg / 1 ' -0.01 -0.01 -0.01 0.01 fall 0.1 fall Barry Ba -0.05 -0.05 -0.05 0.5 fall 5.0 fall mg / l Lead Pb min min min 0.1 fall 1.0 fall mg / l 0, 005 0.005 0.005 Cadmium Cd min min min 0.01 fall 0.1 fall mg / l 0, 001 0, 001 0.001 Chromium Cr ^xx min min min XX fall XX fall mg / l 0, 005 0, 005 0.005 Iron Fe 0.09 0.03 0.060 no need. fall no need. fall mg / l 0.05 0.5 Cobalt Co -0.01 -0.01 -0.01 0.2 fall 0.5 fall mg / l Copper Cu 0, 03 0.05 0.04 fall mg / l - Nickel Ni -0.01 -0.01 -0.01 0.2 fall 2.0 fall mg / l Mercury min min min 0.005 fall 0.01 fall Hg mg / l 0.0005 0.0005 0.0005 Zinc Zn -0.05 -0.05 -0.05 1 fall 10th fall mg / l Tin Sn -0.1 -o, i -0.1 0.2 fall 2.0 fall mg / l

^x ΑΟΧ is the sum of organic halogen compounds. This measurement measures both chlorinated solvents and lipophilic, non-volatile organic chlorine compounds and organic chlorine pesticides.

^xx Chrome-III = 0.05 / 2 Chrome -IV = 0.01 / 0.1

Minus sign or min. means that the measured value is below the limit of analytical determination.

The numeric value given is the limit of detection for the respective methods.

Claims (29)

DEFINITION OF INVENTION A method for the decontamination and utilization of waste, characterized in that it is unsorted, untreated, contains any harmful substances in solid and / or liquid form, industrial, domestic and / or special waste, as well as industrial products. graded heat flux, thermally separable or structurally removable, and, with maximum energy recovery, convert solid residues into a high temperature alloy, characterized in that the decontaminated waste mixture, together with the fluid parts, retains its mixing and unifying structure, is compacted by loading batches undergoes temperature treatment steps in the direction of rising temperature without intermediate cooling with at least one lower temperature step, providing contact with the reaction vessel walls at a predictable flow pressure and shape, and no material is removed from the reaction system during this transition the products shall be cooled rapidly when necessary after complete preparation, modification and subsequent treatment of the material. 2. A process according to claim 1, characterized by passing at least the lower temperature step of maintaining the pressure effect in contact with the walls of the reaction vessel with the expected shape and strength, and at least one high temperature step of supplying oxygen. 3. A process according to claim 1, wherein the low temperature stage is between 100 ° C and 600 ° C and the high temperature stage is above 1000 ° C. 4. A process as claimed in claim 1, wherein the unmixed and compacted mixture of waste particles decontaminated together with the liquid particles, while retaining its mixing and unifying structure and under pressure, is brought to a suitable temperature above 100 ° C. channel, the compact mix shifts across the channel extension with adequate strength to the channel walls, evaporating the original fluids, destroying the mechanical rebound forces and organic components of the individual components of the decontaminated waste mixture, and transferring the extruded solids into a high temperature conglomerate. a reactor capable of maintaining a temperature of at least 1000 ° C throughout its volume. 5. A process according to claims 1 and 4, characterized in that the solid conglomerate is exposed to heat radiation before it enters the high temperature reactor and, due to the internal pressure of the residual gas, disintegrates the conglomerate into constant shapes. 6. A process according to claim 1, wherein the high temperature reactor is formed of and retains a gas-permeable filler of solids scrap up to the height of the heated channel inlet, the fill level is maintained constant, and leaving the heated channel organic components of the solid on the outside, they pyrolitically decompose immediately and in a short period of time. 7. A process according to claims 1-6, wherein the pure carbon moiety in the filler is converted to carbon dioxide by metered oxygen delivery, so that the latter is reduced to carbon monoxide by passing through the filler containing pure carbon. 8. A process according to claims 1-7, wherein water vapor generated from the decontaminated waste liquid particles in the heated channel and subjected to high pressure exiting the channel is directed in a high temperature reactor over the filler surface and through thermally decomposed and pure carbonaceous solids. fractured fracture margins. 9. A process according to claims 1-8, characterized in that, in a quenching zone heated to at least 1000 ° C above the filler, all chlorinated hydrocarbon compounds (dioxins and furans) are destroyed and long chain hydrocarbon compounds formed during the thermal decomposition of organic compounds are cleaved. condensates such as resins and oils. 10. A process as claimed in claims 1-9, wherein the mixture formed in the high temperature reactor containing at least 1000 ° C of a harmful gas synthesis gas is immediately exited from the high temperature reactor with a jet of water until cooled down at 100 ° C. dust. 11. A process according to claims 1-7, characterized in that, at temperatures above 2000 ° C, the metallic and mineral constituents obtained by gasification of pure carbon with oxygen are melted and fractionated in known manner. 12. A process according to claims 1-11, wherein after gasification, the high temperature mineral alloys remain in the liquid phase in an oxidizing atmosphere until the alloy clears, is free of bubbles and is homogeneous. 13. A process according to claim 12, characterized in that the homogenized high temperature alloy is used to produce high quality industrial products by rolling, casting, blowing and / or blowing using at least part of its inherent energy. 14. A process according to claims 1-10, characterized in that the synthesized gas is used to heat a lower temperature stage channel, as well as to heat a high temperature reactor and / or alloy clarification and / or oxygen device. 15. Waste decontamination and recovery unit, comprising several tanks for the stepwise heating and treatment of waste, characterized in that at least one of the reaction capacities of the thematic treatment steps at at least one decoupling heat treatment and at least one oxygen treatment at temperatures above 1000 ° C. non-gateway and those reaction equipment, together with the decontaminant mixture injection device, are arranged in a single, one-way operating line such that the fixed thermal expansion point of the unit as a whole passes through the reaction vessel at the highest temperature of the heat treatment step. 16. Apparatus according to claim 15, characterized in that the reaction tank for oxygen treatment after decontamination is a horizontally located, externally heated, reciprocating furnace having a rectangular cross-section with a furnace width to furnace height ratio greater than 2 at a furnace ratio l ^j ] _irosn in _es k 15 λ / ^ furnace> in which ^ the cross-sectional area of the furnace yna recessed furnace. 17. Apparatus according to claim 15, characterized in that the sliding furnace has, at least on the loading side, support rollers which can move longitudinally when receiving the applied lateral forces. 18. Apparatus according to claim 15, characterized in that the loading side of the pushing furnace is fixedly connected to the outlet side of the compactor having a vertical compaction direction in the first step and a horizontal in the second step and that the waste compactor has a movable roller support. 19. Apparatus according to claim 15, characterized in that between the outlet side of the waste compactor and the loading opening of the recess furnace there is a retractable and retractable resisting wall for receiving horizontal compaction resistance forces. 20. Apparatus according to claim 15, characterized in that the horizontal compaction unit of the waste compactor is formed as a retractable plane, whereby the vertically and horizontally compressed waste packages forming a gas-tight stopper are pressed into the feed opening of the reciprocating furnace while being kept pushed. 21. Apparatus according to claim 15, characterized in that the outlet side of the push furnace is firmly connected to the entrance side of a vertically mounted shaft furnace, wherein the gaseous, liquid and solid products of the push furnace reaction are treated at a temperature above 1000 ° C by supplying oxygen. Apparatus according to claim 15, characterized in that, for a quicker change of the thermally loaded lower reaction vessel portion, the vertical shaft furnace for the high temperature treatment of the sliding furnace reaction products is divided approximately at the inlet height. 23. Apparatus according to claim 15, characterized in that a lower heat treatment reaction vessel is provided below the high temperature reaction tank, wherein the metal and mineral components of the mixture of heat treated waste melted in the high temperature zone can be further treated to supply oxygen and energy. 24. Apparatus according to claim 15, characterized in that the lower portion of the high temperature reaction vessel and the subsequent heat treatment reaction vessel can be lowered and transported in the direction of the base 90 °. 25. Apparatus according to claim 15, characterized in that the high-temperature reaction tank and the subsequent heat-treating reaction vessel for the molten metal and mineral components can, if necessary, be operated overcrowded. 26. Apparatus according to claim 15, characterized in that the high temperature treatment reaction vessel on the gas outlet side is firmly connected to a fast-acting gas cooler having a device for introducing cold water into the hot gas stream. 27. The device of claim 15, wherein the waste heat treatment reaction gas products passes the device at a pressure above atmospheric pressure and the device has a throttle device, such as a throttle valve, at the end of the pipeline. 5 28. The apparatus of claim 15, wherein a pressure barrier water barrier is coupled to the high temperature limiting reaction vessel. 29. Apparatus according to claim 15, characterized in that the waste grouping and loading devices are disposed above the loading side and the devices for purifying and utilizing the gas are arranged in a bite. FIG. 1 year o T3 P • Φ Φ + »a • rl CO CO a) 03 a oh • H co S S a) • H • rl a 03 β • H o nS · <υ Φ C! C * xJ ΣΖΖ ΗγΗ be • H SA O Ί-5 CXJ .—. o Ό Ή a d 0.0 >> + » o « t — 7 cj i-4 CO you Σ3 "" CMC3 $ = 5 £ toJ _r . ^ C 10 - C 3 CJCJCJCJC-l O o O O O S8®S S co o ^ cn Φ • H CZD O r4 C => + » « f—) C-J s o to = ± Cxi Minerals Metals CM taO • H fa -v m ώ S • H • H aJ (4 60 Φ • H 60 Φ O > 0Q a o S HI ΟΛ ώ • H • H d i-1 • rl d d Lt rH Φ d ϋ -P • rl Φ a a 03 o Ι-d & d a ι Λ 1 X • o • H I / b i> o o 1 rd A 1 O Ή Lt d oo o • ro b • d Minerals Fig.4 Metals 1 m £ • rl Lt ι ^φ Φ • H Al 1 ^r_1 d 1p d 1 * 4