MXPA99005408A - Process and apparatus for the partitioning and thermal treatment of heterogeneous feedstock - Google Patents

Abstract

A novel process and apparatus for the thermal partitioning of heterogeneous feedstock (11) for the production of a metal product, a glass ceramic product and a gaseous product. The process includes the capability for thermal treatment of hazardous waste as defined by the Environmental Protection Agency (EPA) which also contains radioactive isotopes in some cases (mixed waste as defined by the Department of Energy) and the production of stable long-lived products as a result of treatment. More specifically, this invention relates to a novel process and apparatus whereby an input feed stream (9) of a widely heterogeneous nature in the descriptors of physical form, combustibility, chemical content, and particle size and contaminated with varying concentrations of hazardous components and/or radioisotopes is treated in a direct current graphite electrode arc melter (4) with a contiguous thermal oxidizing reactor (5) for the production of a metal product, a basalt-like glass ceramic product and a fully combusted offgas. The apparatus described incorporates an offgas fast quench configuration (17) for the minimization of dioxin formation and subsequent ease of cleansing of the offgas stream.

Description

- - PROCESS AND APPARATUS FOR THE SEPARATION AND THERMAL TREATMENT OF HETEROGENEOUS FOOD MATERIALS FIELD OF THE INVENTION The present invention is generally related to the thermal processing of heterogeneous feedstocks and the production of a metallic product, a ceramic glass product and a gaseous product. The process includes the capacity for thermal treatment of hazardous waste as defined by the Environmental Protection Agency (EPA) which also contains in some cases radioactive isotopes (mixed waste as defined by the Department of Energy) and the production of stable products of life long as a result of treatment. More specifically, this invention describes both novel devices and processes by means of which an input feed stream of a widely heterogeneous nature in the descriptors of physical form, combustibility, chemical content, and particle size and contaminated with varying concentrations of components hazardous or radioisotope is treated in a direct or alternating current graphite electrode arc melter with a contiguous oxidization reactor Ref.: 30548 thermal for the production of a metallic product, a basalt as a ceramic glass product and the combustion of malodorous gases. The described apparatus incorporates a fast extinguishing configuration of malodorous gases for the minimization of dioxin formation and for the subsequent tranquility of the purified from the malodorous gas stream.

BACKGROUND OF THE INVENTION The Joule heated melter has traditionally been used for the production of glass-based products. The graphite electrode arc melter has traditionally been used for the reduction of minerals to metals and for the production of value-added products from a controlled and well-defined input feed stream. The arch smelters have also been used for the production of value-added mineral wool from the input material well characterized and controlled. Plasma torch arc melters have traditionally been used for the production of precious metals such as titanium. The different types of smelters commonly used in industry can be classified as low temperature (900 ° C-1200 ° C) medium temperature (1200 ° C-1500 ° C) and high temperature (1500 ° C-2000 ° C), with its defined use for the desired product and the required process. Joule hot melters commonly used for glass production (which includes borosilicate glass for high levels of radioactive waste) fall within the range of low temperature melters. Medium temperature melters are required for the production of high temperature glass such as aluminosilicate glass and ceramic glass.

High temperature melters are required for the reduction of minerals to metals such as iron ore to iron and for the production of a basalt as the ceramic glass product without the addition of molten reagents to reduce the viscosity. Arc smelters use heat-dented when an electric arc passes through a gas. The gas is then ionized and forms a high temperature plasma. Plasma temperatures can exceed many thousands of degrees centigrade. High temperatures and intense Heating of the process materials, make this technology ideal for the processing of high temperature metals.

The investigations and developments by the government and the industry aim to apply the technology of the arc melter to the treatment of hazardous and / or radioactive wastes. The application of the traditional technology of the smelter and the equipment for the safe, efficient and economical treatment of heterogeneous hazardous and / or radioactive wastes the expansion of the allowable complement of the incoming feed stream, the expansion of the flexibility of the operating process, and the adjustment of the specifications for the output products and malodorous gases.

There are a number of tests or development programs to apply to the technology of the electric arc melter for the treatment of radioactive waste, mixed waste, municipal waste, and hazardous waste. In an arc melter, the waste materials are heated to volatilize, pyrolyze, and destroy organics, and (b) melt inorganic materials with molten slag or metallic phases. By controlling the stoichiometry of the reaction, mixing, and other optional parameters, the process can be used to chemically oxidize or reduce the waste components, or react the waste components to form new products.

PREVIOUS ART Read in US Patent 4,421,037 comments on an oven for waste treatment. Rackeley Et al in US Patent 5,052,312 discusses the use of a cyclone furnace for the incineration of hazardous wastes and the vitrification of ashes. Alvi, et al in US Patent 5,541,336 comments that the plasma arc is the decomposition of hazardous wastes into vitrified solids and non-hazardous gases.

BRIEF DESCRIPTION OF THE INVENTION The processes described and the devices allow the continuous or intermittent feeding of a stream of heterogeneous waste very different input, the thermal separation of the input feed into the inert and volatile fractions, the melting and oxidation or reduction of the inert fraction in a phase of ceramic glass (slag) consisting of oxidized metals and materials of low vapor pressure, smelting and reduction of inert fraction metals to a metallic phase. In addition, the flexibility of the operation and the processes allow controlling the volatilization of high vapor pressure materials and the separation forces of these materials to the ceramic glass phase.

The processes and appliances provide for the removal of the metallic and ceramic glass phases by casting techniques of high temperature molten metal and rapid cooling of malodorous gas from over 2000 ° F to about 150 ° F in a minimum period of time. In addition, the process provides the recovery of a ceramic glass product via product by controlled melting and cooling techniques via the addition of insulation or heating to control the structure of the crystalline phase of the cooled final product.

The types of wastes to which the treatment of the described invention is applied include wastes having very different compositions in terms of the dirty content, metallic content, fuel content, organic content and content of hazardous contaminant.

The product of ceramic glass produced exceeds the common requirements of the Characteristic Toxic Leaching Procedure (TCLP) as published in the Federal Register on March 29, 1989, and where a more narrowly defined product specification for improvement is found. This specification may include narrowly defined compositional range and physical properties.

The metallic product is also suitable for recovery as a piece of industrial metal from a non-radioactive input feed and as a recyclable metal within the nuclear industry the radioactive contamination of the input feed material.

The malodorous or exhaust gas is rapidly extinguished at Darir from the temperatures required to complete the combustion and oxidation (> 2000 ° F) is the minimum time to lower the accepted temperatures as the formation temperature for dioxins and furans thereby minimizing the production of dioxins. In addition cleaning the malodorous gases allows the separation of the particles of the malodorous gas to volatile metal fractions and salts.

A homogeneous or heterogeneous feed material is thermally treated to form a melting bath and a gas phase in an arc melter separated by: grinding (2) a feed material (1) at a particle size of one brine less than one half the melting diameter; which conveys the feed material horizontally to a fourth melter (4); separating the feed material to a molten metal, slag, and malodorous gas phases; oxidizing malodorous gas for more than two seconds at a temperature above 2000 ° F in a thermal oxidizer (5); which extinguishes the flow of the malodorous gas from the thermal oxidizer in a room rapidly extinguishing malodorous gas (17) at a temperature below 150 ° F in a minimum time; cleaning the malodorous gas; and eliminating the final melted products.

The nominal characterization of the feed material (11) is heterogeneous and the general chemical composition of the matrix material of the feed material varies between the following ranges: dirt 0-100%, metals 0-35%, fuels 0-90%, volatile organic materials 0-60%, chlorinated organic materials 0-60%, chlorine 0-20%, carbon 0-40%, nitrates 0-20% and hydroxides 0-100%.

The feed material (11) may contain organic and non-organic compounds and metals classified as hazardous or toxic according to the classification of the U.S. Environmental Protection Agency. The feed material (11) may contain radioactive isotopes that emit alpha, beta, or gamma radiations.

The feed material (11) is transported through a side wall of the melter (4) and the surface of the melting bath (1-. 15) can be regulated with a controlled depth of cold layer (13) for increase the separation of volatile materials to a phase of molten ceramic glass. A portion of the fourth melter can be operated with a cooled outer wall to freeze a layer of the molten product inside the wall to ensure a long operation period in the melter.

The ends of the arc melter electrode (21) can be raised in conjunction with the lifting of the surface of the melting bath (14, 15) in a portion of the fourth melter which has a nominal depth for a diameter ratio of less than one half, and the fourth (4) can be rapidly mobile as in a batch operation without some capacity of casting molten metal.

Oxygen can be injected into or near the surface of the melting bath (14, 15) to control the oxidation reduction reactions in and on the melting bath (14, 15) for the generation of a syngas for the processes of the material of power and cogeneration of combustible gas.

An auxiliary heat source (16) can be injected into the base of the thermal oxidizer (5) to maintain the temperature. An oxidation reaction reduction of the gas phase can be regulated and controlled by the generation of a syngas for the process of the feedk and the cogeneration of fuel gas. The air enriched with oxygen is injected into the base of the thermal oxidizer (5) to maintain the temperature and provide oxygen for the oxidation reactions, and for the generation of a syngas for the process of the feedk and the cogeneration of the fuel gas.

The clean particulate, the volatile metals, the salts and the maintenance material of the air pollution control system, such as the filters can be introduced into the back of the feed material (1) and processed through the system again. . A molten metal casting product and a casting system is operated in a manner to control the cooling flow of a molten ceramic glass when attempting a mold insulation or addition of heat for the purpose of controlling the amorphous / crystalline phase structure of the final products.

The liquid can be absorbed in the feed material (11) or injected on top of the surface of the cold layer (13) or the surface of a melting bath (14, 15).

A thermal partition arc melting apparatus according to the present invention includes: a fourth melter with a refractory lining (4) with a molten bath (14, 15) having a nominal depth for a quarter or a half diameter ratio and, which has multiple sides with exit holes (19, 20) for the cast metal and slag; the fourth caster with refractory lining further comprises electrode ports (10) with 30 ° ± 10 ° of the vertical, a supply part (9) with 90 ° of the vertical, and a central port for the malodorous gas placed vertically above the fourth smelter; an electricity-based heating source comprising graphite electrodes of parallel axial transfer (21) current and voltage transport systems operating with a submerged or short Joule heating arc resistance or a long radiant heating arc; an adjoining thermal oxidizing reactor (5) long enough to provide a gaseous residence time greater than two seconds, located vertically above the fourth melter, with an auxiliary heating source (16), located at the bottom of the thermal oxidizer, to maintain an operating temperature of 1800 ° F to 2200 ° F; an extinguishing chamber for the malodorous gas (17) directly attached to the upper part of the adjoining thermal oxidizer which extends in an inclined manner at 45 ° -60 ° from the horizontal; and a control system for air pollution (6).

The two graphite electrodes (21) have a nominal space of the service ends of the melting bath (14, 15). The graphite electrodes (21) have translational mechanisms capable of positioning the ends of the electrode in the directions X, Y and Z (12).

The heat source can be a common direct source comprising in addition to two graphite electrodes of translation of the common parallel axis (21) and voltage transport; a graphite electrode of a common alternative phase (21) and a voltage transport system with electrodes in multiples of two; or a common three-phase graphite electrode (21) and a voltage transport system with electrodes in multiples of three.

The apparatuses may further include a wet-dry control system of malodorous gas (6) for the purpose of collecting particulates, volatile metals and salts in an aqueous stream of dissolved and suspended sludge and a gas filtration system for filtration purposes end of the gas stream.

The apparatus may further include a dry-wet purifying system for malodorous gases (6) for the purpose of distributing particulates and volatile metals to a processable or recyclable secondary dry stream, the salts of an acid gas scrubber to an aqueous stream of sludge suspended dissolved and not dissolved, and a filtration system in order to make a filtration of the gaseous stream.

BRIEF DESCRIPTION OF THE APPROVED DRAWINGS Reference will be made to the appended drawings where as a reference throughout several FIGURES are denoted as elements and where: FIGURE 1 Schematically describes a flow chart for the process presented by the present invention. FIGURE 2 Describes a representation of the apparatus of the system for the thermal process of the heterogeneous feedstock and the production of a metallic product, a ceramic glass product, and a gaseous product according to this invention. FIGURE 3 Describes the primary source of preferred heat of supply according to this invention. FIGURE 4 Describes a representation of the apparatus of the system for the thermal process of heterogeneous feedstock and the production of a metallic product, a ceramic glass product, and a gaseous product for the treatment of hazardous or radioactive wastes according to this invention.

This invention and its various representations are described in greater detail in the following description.

DETAILED DESCRIPTION OF THE PRESENT INVENTION The present invention can process a wide variety of hazardous municipal waste, radioactive and mixtures (both radioactive and hazardous). The test conducted in the design of the present invention in this application patent shows that the present invention can process a range of the feedstock shown in Table 1. The chemical composition of many of these components and similar components shown in Tables 2, 3, and 4.

Table 1. Acceptable limits of variations of input feedstock Feed material components% by weight Oils 0-100 Metals 0-35 Fuels 0-90 Volatile organic 0-60 Organic Chlorinated 0-60 Chlorides 0-20 Carbon 0-40 Nitrate 0-20 Hydroxides 0-100 Table 2 A typical chemical composition of feed of the material treated for this invention. % by weight of waste components Carbon Hydrogen Oxygen Nitrogen; Sulfur Chloride Floride Inert Water No fuel Glass Rings Glass Rasching 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Other glasses 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Mátales Acero al carbón 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Stainless steel 0.00 0.00 0.00 b.oó 0.00 0.00 0.00 0.00 100.00 Aluminum 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Tantalio 10W 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Metal heterogeneous 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Lead o.oo 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 HVPM (Zn, Cd) 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 No fuel Heterogéneo Molde Cerámica 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 refractory brick 0.00 0.00 0.00 O.00 0.00 0.00 0.00 3.00 97.00 Concrete 0.00 0.00 0.00 0.00 0.00 0.00 0.00 8.72 91.28 Cemento Portland 0.00 0.00 0.00 0.00 0.00 0.00 0.00 5.00 95.00 Land debris 0.00 0.00 0.00 0.00 0.00 0.00 0.00 10.00 90.00 Wood 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 Oil 0.00 0.00 0.00 0.00 0.00 0.00 0.00 5.00 95.00 % by weight of component waste Component Carbon] Nitrogen Oxygen Nitrogen Sulfur Chloride Floride Inert Water Vermiculite 0.00 0.00 0.00 0.00 0.00 0.00 0.00 5.00 95.00 Sales Evapor. 0.85 0.13 0.00 o.oo 0.00 0.00 o.oo 0.13 98.88 Filters / Detachment Glass media filters 3.96 0.54 0.00 0.00 0.00 0.00 0.00 5.00. 90.50 Asbestos medium filters 3.96 0.54 0.00 0.00 0.00 0.00 0.00 5.00 90.50 Filtered ashes 0.00 0.00 0.00 o.oo 0.00 0.00 0.00 10.00 90.00 Magnesium (Detachment) 0.00 0.00 0.00 0.00 0.00 0.00 0.00 2.00 98.00 Inorganic sludges 1 Lodos-superiors Na O 0.00 0.00 0.00 0.00 0.00 0.00 0.00 60.00 40.00 Lodos-superior CaO 0.00 0.00 o.oo 0.00 0.00 0.00 0.00 60.00 40.00 1 Aqueous solution 0.00 0.00 0.00 0.00 0.00 0.00 0.00 100.00 0.0 Partially combustible Leaded rubber 33.16 4.47 1.01 0.28 0.51 0.00 0.00 0.00 60.56 Organic mud 26.69 3.65 0.00 0.00 0.00 39.69 0.00 0.00 29.97 Cemented resin 83.03 6.97 O.00 0.00 0.00 0.00 0.00 10 , 00 0.00 Resin not cemented 27.68 2.32 0.00 0.00 0.00 0.00 0.00 20.00 50.00 Asphalt 4.294 0.49 0.05 0.05 0.12 0.00 0.00 0.00 95.01 Benelex / Lead 33.20 3.53 25.19 0.00 0.03 0.00 0.00 3J5 34.70 0.41 0.06 0.42 0.00 o.oo 0.00 0.00 20.77 78.34 Plastics Fuels Poly 84.93 13.40 0.35 0.11 0.02 0.00 0.00 0.00 1.19 PVC 47.38 5.73 9.09 0.00 0.01 35.72 0.00 O.OO 2.07 % in weight of waste components Carbon Hydrogen Oxygen Nitrogen Sulfur Chloride Floride Water Inert Tefion 24.00 0.00 O.OO 0.00 0.00 0.00 76.00 0.00 0.00 Plexiglas 59.99 8.05 31.96 0.00 0.00 0.00 0.00 0.00 0.00 Rubber 76.23 10.28 2.32 0.65 1.18 0.00 0.00 0.00 9.34 Surgical gloves 76.23 10.28 2.32 0.65 1.18 0.00 0.00 0.00 9.34 Heterogeneous fuels -Graphite 99.19 0.70 0.00 0.00 0.01 0.00 0.00 0.00 0.10 Paper 49.54 5.27 37.59 0.00 0.05 0.00 0.00 5.00 2.55 Wood 46.94 5.00 35.61 0.00 0.05 0.00 0.00 10.00 2.42 Carton 49.54 5.27 37J9 0.00 0.05 0.00 0.00 5.00 2J5 OR Fabric '49.54 5.27 37.59 0.00 0.05 0.00 0.00 5.00 2.55 Table 3. Chemical composition of the inert fraction of the feed material treatable by this invention expressed as a fraction of the inert chemicals % by weight of the inert fraction Aluminum Boron Bario Calcium CaSO Cadmium Carbon Chromium Cob Non-combustible Glass Rings Rasching glass 0.00 12.80 0.00 5.00 0.00 0.00 0.00 0.00 0.00 1 Other glasses 0.00 5.00 0.00 5.00 0.00 0.00 0.00 0.00 0.00 f Kill them 1 Carbon steel 0.00 0.00 0.00 0.00 0.00 0.00 0.20 0.00 0.00 Stainless steel '0.00 0.00 0.00 0.00 0.00 0.00 0.03 19.00 0.00 Aluminum 98.90 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Tantalio 10W 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Metal heterogeneous 30.00 0.00 6.00 0.00 0.00 1.00 0.00 1.00 10.00 Lead 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.10 HVP (Zn, Cd) 0.00 o.oo 0.00 0.00 0.00 50.00 0.00 0.00 0.00. No fuel Heterogéneo Molde Cerámico 0.00 0.00 0.00 o.co 0.00 0.00 0.00 0.00 0.00 refractory brick 43.00 0.00 0.00 1.00 0.00 0.00 0.00 0.00 0.00 Concrete <; 1.08 o.oo 0.00 9.79 aoo 0.00 0.00 0.00 0.00 Cement Portland 6.91 0.00 0.00 62.92 0.00 0.00 0.00 0.00 0.00 Dispose of soil 12.70 0.00 0.00 3.70 o.oo 0.00 0.00 0.00 0.00 Wood 15.22 0.00 0.12 7.74 0.00 0.51 0.00 1.84 0.00 Oil • 28.86 O.00 0.00 2.35 0.00 0.00 0.00 0.00 0.00 % Wt of inert fraction Components Aluminum Boron Bario Calcium CaSO Cadmium Carbon Chrome Copper Vermiculite 19.95 0.00 0.00 0.00 0.00 0.00 0.00 5.00 95.00 Sales Evapor. 1.93 0.00 0.00 2.47 0.00 0.00 0.00 0.00 0.00 Filters Detachment Filters of glass medium 6.28 10.47 4.19 3.14 0.00 0.00 0.00 0.00 0.00 Filters of medium of Asbestos 0.00 0.00 0.00 0.00 0.00 0.00 O.OO '0.00 0.00 Filtered ashes 12.70 0.00 0.00 3.70 0.00 0.00. 0.00 0.00 0.00 Magnesium (Desprendimiento) 0.00 0.00 0.00 0.00 0.00 0.00 O.OO 0.00 0.00 Inorganic sludges Top sludges Na 0 8.34 0.00 0.00 4.80 0.00 0.00 0.00 0.10 0.17 Sludge-upper CaO 4.31 0.00 0.00 22.61 0.00 0.00 0.00 0.04 0.18 Aqueous solution i 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 iso Partially combustible Leaded rubber 0.07 0.00 0.00 1.39 0.00 0.00 aoo 0.00 0.09 Organic mud 0.00 0.00 0.00 37.89 0.00 0.00 0.00 .oo 0.00 Cemented resin, 0.00 0.00 0.00 0.00 0.00 o.oo 0.00 0.00 0.00 Cementless resin 6.91 0.00 0.00 64.00 0.00 0.00 0.00 0.00 0.00 Asphalt 0.13 0.00 0.00 05 0.00 0.00 0.00 0.00 0.00 Benelex / Plomo 0.31 0.00 0.00 1.56 0.00 0.00 0.00 0.00 0.00 0.00 0.06 0.00 0.00 0.31 99.00 0.00 0.00 0.00 0.00 Plastic Poly Fuels 0.10 o.oo 0.00 99.70 0.00 0.00 0.00 0.00 0.00 PVC 0.20 0.00 22.16 0.90 0.00 61.94 0.00 0.00 0.00 % by weight < le fraction Inert Component Aluminum Boro Bario Calcio CaSO Cadmium Carbon Cromo Copper Teflon 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Plexigl s 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 rubber Rubber 1.00 0.00 0.00 20.70 o.oo 0.00 0.00 0.00 0.00 Surgical gloves 1.00 0.00 0.00 20.70 0.00 0.00 0.00 o.oo. 0.00 Heterogeneous fuels -Grafito 15.00 0.00 0.00 7.10 0.00 0.00 0.00 0.00 0.00 Paper, 6.31 0.00 0.00 31.79 0.00 0.00 0.00 0.00. 0.00 Wood 6.31 0.00 0.00 31.79 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 6.7 0.00 0.00 31.79 0.00 0.00 0.00 0.00 Fabric 6.31 0.00 0.00 31.79 0.00 0.00 0.00 0.00 0.00 I? i Table 3. (Continued)% by weight of inert fraction Component Gallium Iron Lead Magnesium Manganese Nickel Phosphide Potassium KNQ No fuel 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Glass 0.00 0.00 Rings Glass rasching o.oo 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Other glasses Mátales Carbon steel 0.00 99.10 0.00 0.00 0.45 0.00 0.00 0.00 0.00 I Stainless steel 0.00 71.97 0.00 0.00 0.00 9.00 0.00 0.00 0.00 1 Aluminum 0.00 0.00 0.00 0.70 0.00 0.00 0.00 0.00 0.00 Tantalio 10W 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Heterogeneous metal 0.00 50.00 1.00 0.00 0.00 0.00 0.00 0.00 Plfimri 0.00 0.00 99.90 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 HVPM (Zn, Cd) 0.00 0.00 0.00 0.00 0.00 (or fuel Heterogeneous Ceramic Mold 0.00 o.oo 0.00 61.64 0.00 0.00 0.00 0.00 0.00 refractory brick 0.00 1.00 0.00 1.00 0.00 0.00 0.00 0.00 0.00 Concrete 0.00 0.45 0.00 0.40 0.00 0.00 0.00 0.00 0.00 Cement Portland 0.00 2.91 0.00 2.54 o.oo 0.00 0.00 0.00 0.00 Disposal of earth 0.00 5.10 o.oo 2.90 o.oo 0.00 0.00 3.10 0.00 Wood 0.00 28.30 7.81 5.37 0.15 1.13 0.10 0.38 0.04 Oil 0.00 434 0.00 5.02 0.00 0.00 0.00 OJO 0.00 Vermiculita 0.00 41.30 0.00 17.98 0.00 0.00 0.00 0.00 0.00 % wt of inert fraction Component Gallium Iron Lead Magnesium Manganese Niauel Phosphorus Potassium KNQ 0. 66 0.00 0.00 0.30 28.49 Sales Evapor. 0.00 0.45 0.QQ 0.00 Filters Detachment Filters of glass medium 0.00 0.10 0.00 1.05 0.00 0.00 0.00 2.09 0.00 0.00 0.00 0.00 21.16 0.00 0.00 0.00 0.00 0.00 Asbestos medium filters 5.10 0.00 2 0.00 0.00 0.00 3.10 0.00 0.00. 90 Filtered ashes Magnesium (Desprendimiento) 0.00 0.00 0.00 100.00 0.00 0.00 0.00 0.00 0.00 Inorganic sludges Top sludges Na O 5.51 6.52 0.64 5.20 0.00 0.00 0.00 4.46 0.00 1 t \ 3 Sludge-upper CaO 0.08 5.84 0.31 10.55 0.00 0.00 0.00 3.74 O.OO, 1 Aqueous solution 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Partially combustible Leaded rubber 0.00 0.07 93.20 0.42 0.00 0.00 0.09 0.00 0.00 Organic mud 0.00 7.40 0.00 0.14 0.00 0.00 0.00 0.56 0.00 Cemented resin 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Resin not cemented 0.00 2.91 0.00 2.54 0.00 0.00 0.00 0.00 0.00 Asphalt 0.00 0.69 0, 00 0.17 0.00 0.13 0.00 0.00 0.00 Benelex / Lead 0.00 0.23 95.08 0.24 0.09 0.00 0.00 0.00 0.00 0.00 0.04 0.00 0.05 0.02 0.00 0.00 0.00 o.oo Plastic Poly Fuels 0.00 0.00 0.00 0.20 0.00 0.00 0.00 0.00 0.00 PVC 0.00 0.20 0.00 0.40 0.80 0.00 6.20 0.00 0.00 Teflon 0.00 0.00 0.00 .00 0.00 0.00 0.00 0.00 0.00 % Wt of fraction of inert Galium Fierro Lead Maßnesio Manganese Niquel Phosphorus Potassium KNQ Plexiglás 0.00 0.00 0.00 0.00 0.00 0.00 0.00.o.oo 0.00 0.00 rubber "\ Rubber I 0.00 1.00 0.10 6.20 0.00 0.00 1.30 0.00 0.00, Gloves for surgeon 0.00 1.00 0.10 6.20 0.00 0.00 1.30 0.00 0.00 Heterogeneous fuels -Graphite 0.00 17.30 0.00 2.30 0.00 0.00 o.os 2.30 0.00 i Paper 0.00 4.58 0.00 4.97 1.84 0.00 0.00 0.00 0.00, Wood 0.00 4.58 0.00 4.97 1.84 0.00 0.00 0.00 0.00 0.00 Carton 0.00 4.58 0.00 4.97 1.84 0.00 0.00 0.00 0.00 I Fabric 0.00 4.58 0.00 4.97 1.84 0.00 0.00 0.00 0.00 t-0 i Table 3 (continued)% by weight of inert fraction Silicon Sodium NaNO Tantalium Tin Titanium Tungsten Vanadium Zinc Non-combustible Glass Rings Glass rasching 62.20 20.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Other glasses 70.00 20.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Mátal Carbon steel 0.25 0.00 o.oo 0.00 0.00 0.00 0.00 0.00 0.00 Stainless steel 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Aluminum 1 0.40 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Tantalio 10W 0.00 0.00 0.00 0.00 0.00 10.00 0.00 0.00 0.00 Metal heterogeneous 0.00 0.00 o.oo 0.00 1.00 0.00 0.00 0.00 2.00 Plomo 0.00 0.00 .oo 0.00 0.00 0.00 0.00 o.oo 0.00 HVPM (Zn, Cd) 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 50.00 Non-combustible Heterogeneous and Ceramic Mold 38.36 0.00 0.00 0.00 0.00 0.00 0.00 0.0 '0.00 refractory brick 52.00 0.00 0.00 0.00 0.00 2.O0 0.00 0.00 0.00 Concrete 87.85 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Cement Portland 21.92 0.00 o.oo 0.00 0.00 0.00 0.00 0.00 0.00 Disposal of land 70.70 1 , 80 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Madera p Ac.ebiit? E 23.13 1.33 0.08 0.00 0.17 0.18 0.00 0.00 3.58 Vermiculita 60.68 0.00 o.oo 0.00 0.00 0.00 0.00 0.00 20.77 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 % by weight the fraction of inerts Component Silicon Sodium NaNO Tantalum Tin Titanium Tungsten Vanadium Zinc Sales Evapor. 8.54 0.17 56.99 0.00 0.00; oo 0.00 0.00 0.00 Filters / Detachment Glass media filters 59.32 10.99 0.00 0.00 0.00 0.00 0.00 0.00 2.36 Asbestos filter media 78.84 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Filtered ashes 70.70 1.80 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Magnesium (Desprendimiento) 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Inorganic sludges Top sludges Na O 36.09 28.14 0.00 0.00 0.00 0.02 0.00 0.00 0.01 Sludge-upper CaO 46.32 5.59 0.00 0.00 0.00 0.42 0.00 0.00 0.01 Solution aqueous 0.00 0.00 0.00 .00 0.00 0.00 0.00 0.00 0.0 I Fuel partially t CD Leaded rubber I 0.28 0.09 0.00 0.00 0.00 0.0014 0.00 0.00 4.17 • Organic mud 53.95 0.00 0.00 0.00 0.00 0.06 0.00 0.00 0.00 Cemented Resin 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Resin not cemented 21.92 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Asphalt Benelex Lead 95.37 0.85 0.00 0.00 0.00 0.00 0.00 0.00 0.83 0.83 0.00 0.00 0.00 0.02 0.00 0.00 0.00 0.15 0.15 0.00 0.00 0.00 0.81 0.00 0.00 0.00 Plastic Poly PVC Fuels 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 Teflon 0.20 0.00 0.00 0.00 0.00 0.80 0.00 0.00 6.20 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 % by weight the fraction of inert! Component, Silicon Sodium NaNQ Tantalio Tin Titanium Tungsten Vanadium i Zinc Plexiglás 0.00 0.00 0.00 0.00 0.00 0.00 0.00 0.00 o.oo oil Rubber 4.20 1.30 0.00 0.00 0.00 2.10 0.00 0.00 62.10 Gloves for surgeon 4.20 1.30 0.00 0.00 0.00 2.10 0.00 0.00 62.10 Heterogeneous fuels -Grafito 45.50 0.80 0.00 0.00 0.00 1.60 0, 00 0.00 0.00 Paper 16.88 16.80 0.00 0.00 0.00 0.39 0.00 0.00 o.oo Wood i 16.88 16.80 0.00 0.00 0.00 0.39 0.00 0.00 0.00 Carton to 16.88 16.80 0.00 0.00 0.00 0.39 0.00 0.00 0.00 ... 1. Fabric i. • 16.88 16.80 • 0; 00 0.00 0.00 0.39 • 0.00 0.00 0.00 I % Wt of inert fraction SO, CQJ ci Non-combustible Glass Rings Glass rasching 0.00 0.00 0.00 Other glasses 0.00 0.00 0.00 Mátals Carbon steel 0.00 0.00 0.00 Stainless steel 0.0G 0.00 0.00 Aluminum 0.00 0.00 0.00 I Tantalio 10W i 0.00 0.00 0.00? or Heterogeneous metal j 0.00 0.00 0.00 i Lead 0.00 0.00 0.00 HVPM (Zn, Cd) i 0.00 0.00 0.00 Heterogeneous fuel 1 Ceramic mold j 0.00 0.00 0.00 refractory brick 0.00 0.00 0.00 Concrete '0.27 0.17 0.00 Portland cement 1.72 1.08 O.OO Land debris 0.00 0.00 0.00 Wood i 0.33 0.79 0.01 Oil 0.00 0.00 0.00 Vermiculite 0.00 0.00 0.00 % Wt of inert fraction Component SOi COi Cl Sales Evapor. 0.00 0.00 0.00 Filters / Detachment Filters of glass medium 0.00 0.00 o.oo Filters of Asbestos medium 0.00 0.00 0.00 Filtered ashes 0.00 0.00 0.00 Magnesium (Release) 0.00 0.00 0.00 Inorganic sludges Top sludges Na O 0.00 0.00 - 0.00 I ? Lodos-superior CaO 0.00 0.00 0.00 i-1 Aqueous solution 0.00 0.00 0.00 Partial fuel Leaded rubber 0.00 0.00 0.00 Organic mud 0.00 0.00 0.00 Cemented resin 0.00 0.00 0.00 Cementless resin 1.72 0.00 0.00 Asphalt 1. 51 0.00 0.00 Benelex PIomo 0.23 0.58 0.01 0.04 0.11 0.06 Plastic Fuels Poly 0.00 0.00 0.00 PVC 0.00 0.00 0.00 Teflon 0.00 0.00 0.00 % in weigh; of inert fraction Component SO CO} Cl Plexiglás 0.00 0.00 0.00 rubber Rubber 0.00 0.00 0.00 Surgeon gloves 0.00 0.00 0.00 Heterogeneous fuels -Graphyte 8.10 0.00 .OO Paper 4.62 11.69 0.13 Wood 4.62 11.69 0.13 I Cardboard 4.62 11.69 0.13? Fabric 4.62 11.69 0.13 NO i Table 4. Estimated compositions of the additives used to prepare municipal waste mixtures a on nuac n The present invention can process wastes to (a) reduce the volume and mass output by evaporating moisture, thermally decomposing carbonates, and pyrolyzing organic materials, (b) destroying hazardous and non-hazardous organic materials, (c) melting organic oxides to form a homogeneous slag, easy to characterize and recyclable / dispose (stone-like ceramic glass waste forms), (d) separate metals in a melt, from the cast metal phase, and (e) decontaminate the metal phase of radionuclides (if presents). The resulting products are very homogeneous and easy to characterize, compared to the variety of heterogeneous metals which can be fed to the melter. The fourth melter 4 can receive waste that varies greatly in physical and chemical content. The composition of the slag is inherently less variable due to (a) less volatility of the organic materials of many waste materials, and (b) mixing effects of variation of the inorganic feed in the slag pool. Occasionally, depending on the composition of the feed, the desired operating conditions, and the metallic products or slag, the additives are used to modify the ceramic glass waste of similar stones or metal products.

A schematic example of the process presented by the present patents is shown in Figure 1. The particle size of the material of the feed 1 may be in the submicron range or above one half the melting diameter. The feeding materials and the containers of the feeding materials are fed through a hopper of the crusher 8 and reducing the size in the handling of waste and the feeding system operating at low speed, a high voltage crusher 2. This type of crusher, commercially available and included as a component of the present invention, can process most types of waste including heterogeneous, inorganic fuels including brick and concrete, and metals thicker than 1/4 inch. The shredder 2 is capable of shredding the contents of waste containers and / or waste cylinders, boxes and other containers.

The waste is crushed in a hopper which also serves as a feed hopper for a commercial feeder 3. The feeder 3 can safely transport the crushed feed material (feed material) through a feed port in the side wall of the feed. fourth melter 4.

A thermal narrow coupled oxidizer 5 effectively oxidizes entrained and gaseous organic materials that are emitted from the molten and fed materials. The malodorous gas with volatilized and entrained particles are purified and treated in a malodorous gas treatment system 6 to control the emissions. The output products 7 which may include a metallic shape and a ceramic glaze shape are removed and processed into value-added products.

The present invention can process liquid waste, sludge, slurry, or gases. Liquids, sludge, and slurries can be fed into the smelter through injectors or nozzles, absorbed in desiccant absorbers, or delivered in small intact containers. The present invention is also capable of process a feed material 11 that contains radioactive isotopes that emit alpha, beta or gamma radiation.

The present invention can be found or surpassed by the Resource Recovery and Conservation Act (RCRA) the best demonstrated technology available (BDAT) treatment requirements for essentially any hazardous organic contaminant and can produce a ceramic glass very resistant to the leaching of similar stones or a value-added product that can immobilize oxides of toxic metals and radionuclides according to regulatory limits.

A more detailed illustration of the process of the present invention and the apparatuses are shown in FIGURES 2, 3 and 4. Processes occurring in the fourth melter 4 include rapid heat transfer, chemical reactions, and physical transformations from solids to liquids. and gases. The feed material 11 entering the fourth melter 4 is heated and absorbed in the melter through a thin layer 13 due to (a) the radiant heat transfer from the arc and the water bath. melting, (b) conductive and convective heat transfer and mixing in the melting bath and (c) heating resistance (Joule heating) in the melt. As the feed material heats (a) moisture and water of evaporated hydration, (b) organic materials, nitrates, carbonates, sulfates and other materials thermally decompose, pyrolyze and oxidize to form primarily gases and oxides that are soluble in the melt (c) molten slag inorganic materials 14, and (14) metals in the feed material 11 either oxidize when there is sufficient available oxygen from the gaseous oxidant solid and combine with the slag 14 or molten and submerged through the slag, due to a high density of the metal and to form a melting bath 15. Some cements such as plutonium are highly oxidizable, but not volatile, and tend to concentrate in the molten slag 14 as desired, leaving the malodorous gas and the metallic products with one- reduced pollution. Some volatile species such as chlorides, sulfates, and some metals (such as mercury, lead, cadmium, and arsenic) are partially. or more completely volatilized. With this you can allow concentration - of these species in the malodorous gas for purification, if desired, or the operating conditions of the present invention can be adjusted to more effectively retain some of these species in the melt by creating a continuously consumable filter (cold layer). with which the residence time of a volatile material in the melt is increased and in this way increase the chemical reactions and the incorporation in the slag. The surface in the melting bath (14, 15) is regulated with a depth controller of the cold layer (13) to intensify the separation of the volatile material to the melt of the ceramic glass phase. The liquid can be absorbed into the feed material (11) or injected onto the cold layer (13) or on the surface of the melting bath.

The fourth melter 4 can be operated with a wall / bottom outdoor cooler to freeze a layer of the melted product on the side / bottom side to ensure a long melt operation time. The fourth refractory lining melter 4 comprises an electrode 10 at 30 ° ± 10 ° from the vertical, a feed port 9 at 90 ° from the vertical, and a part of the central malodorous gas. placed vertically above the fourth melter. In this present invention, the oxygen is injected into a puddle melted through an oxygen carrying 22 or near the surface of the melting bath through an oxygen carrying 25 to control the oxidation reduction reactions in and on the bath of fusion.

An adjoining thermal oxidizer 5 long enough to provide a gaseous residence time greater than 2 seconds is located vertically above the fourth melter 4. In the present invention, an auxiliary heating source 16 is injected into the base of the thermal oxidizer 5 to maintain a Operating temperature from 1800 ° F to 2200 ° F. In addition, the oxygen enriched air is injected through an oxygen carrying 27 at the base of the thermal oxidizer 5 to help maintain the desired temperature and provide additional oxygen for the oxidation reactions and for the generation of a syngas for the process of the feedstock and the cogeneration of fuel gas. Other operating conditions can be varied to optimize or reduce the amount of metallic product 15 or change the chemistry of the slag 14.

The present invention includes a casting and casting system of molten metal which can be operated in a manner to control the flow of the coolant from the molten ceramic glass by providing a mold insulation or the addition of heat for the purpose of controlling the structure of the mold. the amorphous / crystalline phase of the final cooled product. The present invention incorporates a fourth melter with refractory lining 4 and with a fusing bath 14, 15 having a nominal depth for a diameter ratio in the range of a quarter to a half and includes multiple sides with outlet holes for casting the molten metal and slag. A portion of the slag 14 is located at a desired depth of the melted surface equal to one half of the molten radius and a portion of the metal 20 is located at the bottom of the melt zone to allow intermittent or continuous spraying of any of the the materials. Alternatively a portion of the fourth melter 4 and containing the melted products can be rapidly movable as in a batch operation without any capacity or casting need.

The malodorous gas with volatilized and entrained particles is purified and treated in a malodorous gas treatment system 6 to efficiently control the emissions of organic materials, particles, acid gases, toxic metals or other unwanted emissions. In the present invention the purified particulate, the volatile metals, salts and the maintenance material of the air pollution control system as filters can be introduced into the back of the feed material 1 and processed through the system again. The only thermal narrow coupled oxidizer 5 is designed to efficiently oxidize entrained gaseous and organic materials that develop from the melt and from the feedstocks. The thermal oxidizer 5 is specifically designed to perform the oxidation of the gas which contains long amounts of entrained particles without slag or impurity problematic particle tightly coupling the thermal oxidizer 5 vertically to the fourth melter 4. This capacity is very important for the treatment of radioactive waste and dangerous, when a worker enters for maintenance reasons is limited or prevented. A single arrangement of a fourth malodorous gas extinguisher 17 for thermal oxidizer 5 allows almost instantaneous reduction of gas temperature from greater than 2000 ° F to less than 150 ° F in a same space. The fourth malodorous gas extinguisher 17 is directly attached to the upper part of the adjoining thermal oxidizer 5 extended in an inclined fashion at 45-60 degrees from the horizontal. The fourth melter 17 to the configuration of the thermal oxidizer 5 reduces the potential common plugging of the malodorous gas duct in a cross-arrangement of the horizontal duct and also minimizes the potential for dioxin formation due to the very short residence time of the gas in the range of formation / synthesis temperature of dioxin (about 450 ° F -750 ° F).

An alternate option included in the present invention is to produce a synthesis gas or a fuel gas with a low BTU of the malodorous gas melter. The oxidation reactions reduction of the gas phase can be regulated and controlled to maximize the generation of a syngas for the process of feedstock or for the cogeneration of fuel gas. In this option, the thermal oxidizer 5 is replaced by a reaction room 5 which allows the addition of steam or other reagents to react with the malodorous gas melter to form hydrogen, carbon monoxide, methane gas, or other gases. The particulate in the malodorous gas is filtered either countercurrently in waters under the reaction room 5. In this way the oxygen is injected into or near the surface of the melting bath to control the reactions of oxide reduction in and on the bath of fusion for the generation of a syngas for the process of the feeding material and the cogeneration of combustible gas.

The present invention has a treatment system 6 for malodorous gases 6 with options for removal of acidic particles and gases that includes (a) the removal of wet particles and acid gases, followed by an overheating and removal of traces of organic, toxic metal traces , and traces of submicron particles, or (b) the removal of dry particles, in a powder precipitator or a high temperature filter, followed by the wet removal of acid gas, reheated gas and removal of organic traces, toxic metallic traces, and traces of submicron particles The recovery of heat through of an air gas heat exchanger, water heating, or steam generation are some additional options.

The dry malodorous gas treatment system-dry 6 is designed specifically for radioactive waste applications, and is very reliable and compact. An individual secondary stream of waste consisting of cleaning waters is produced, with traceable trace amounts, HEPA depleted filters, and possibly spent carbon absorbers or other organic traces and metal absorbers. Cleansing waters contain dissolved salts of absorbed chlorides, sulfates and hydrofluoric acid gases, other dissolved species absorbed from malodorous gas such as nitric acid, carbonic acid, and suspended undissolved solid particles.

The dry-wet malodorous gas treatment system 6 is designed to allow an automatic separation of a secondary dry particulate waste stream separated from an aqueous wet cleaning solution.

It is desirable that the particle can be (a) used as a value-added product as a feed material for metal recovery operations, (b) recycled for the melter or (c) stabilized from the process that does not readily tolerate chlorides or other cleaning species. Filtering the particle away from the acid gas liquid reduces the amounts, any, of the chlorides that are undesirable in downstream or recycled particulate processing.

Other malodorous gas treatment systems 6 that can also be incorporated based on regulatory requirements or others include a dry or semi-dry cleaner for the control of acid gases, followed by dry particulate filtration.

The present invention uses a direct current electricity-based heating source comprising two graphite electrodes of axial translation (as arrow 18) 21 which penetrates at an angle to the axis of the fourth melter 4. Two alternatives for the current and the voltage transport systems are the graphite electrodes of an alternating current phase 21 in multiples of two and graphite electrodes of three phases of alternating current 21 in multiples of three. The graphite electrodes 21 are placed with the nominal space of the ends of one half of the diameter of the melting bath and can be operated either on a short arc Joule heating resistor in a submerged mode or a long arc of radiant heating. The graphite electrodes 21 are equipped with translational mechanisms capable of positioning the electrode ends are equipped with the ends of the electrode in the x directions, y and Z 12. The ends of the graphite electrodes 21 can be adjusted separately to consider a change in the level of the molten surface or the consumption ratio of the electrode 8. The ends of the electrode of the arc melter can be lifted together with the lifting of the surface of the melting bath in a portion of the fourth melter which has a nominal depth for the proportion of the diameter of less than half, and the fourth is rapidly movable as in a batch operation without any casting capacity.

This invention has benefits for the thermal (processed) separation of heterogeneous feedstocks. The process of the invention and the apparatuses are extended for the treatment of hazardous industrial waste, medical waste and radioactive waste (mixed). The invention can also be extended to the thermal treatment of municipal solid waste or sludge.

The output products 7 (fig 1) are a metal in a form suitable for recycling, a ceramic glass stably in nature with a high resistance to leaching, with malodorous gas completely burned in a suitable manner for a final purification, or a gaseous rich in fuel in a suitable way for the process of feeding material or cogeneration. An additional advantage in the production of solid products is a significant reduction in volume compared to the input of the feedstock.

Refers exclusively to FIGURE 4, when the radioactive or hazardous material is processed an additional isolation gate 24 and an airlock 23 is added to the feed crusher tank 8 to ensure the complete contaminant.

From the foregoing description, it will be apparent that the present invention provides a design for the process and apparatuses for separation will be evident that the present invention provides a design for the process and apparatuses for separation and thermal treatment of the heterogeneous feedstock. Various changes can be made in the above descriptions and methods of operation without departing from the essence or scope of the following claims, it is understood that all the matter contained in the above description or shown in the appended drawings can be interpreted as illustrative and not in the sense of limitation.

Variations or modifications for the design and construction of this invention, within the scope of the appended claims, may occur for those with skills in the field in reviewing what is described herein (especially for those using computer auxiliary design systems). Such variations or modifications, if within the essence of this invention, they are intended to be made within the scope of any claim to issue a patent protection of this invention.

Claims (23)

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1. REIVINDICATION 5 1. A process in which a homogeneous or heterogeneous feed material is thermally treated to form a melting bath and a gas phase in a separation arc melter characterized in that it comprises: a. grinding a feed material (1) at a submicron particle size to less than one half the diameter of the melter; b. "transporting the feed material horizontally in a fourth melter, c) separating the feed material in a molten metal, slag and phases of malodorous gas; d-oxidizing the odorless for more than two seconds at a time; temperature above 2000 ° F in a thermal oxidizer: e.to extinguish the flow of malodorous gas from the thermal oxidizer in a room rapidly extinguishing malodorous gas at a temperature of less than 150 ° F in a minimum time, f.purifying malodorous gas. and, 9- remove the final molten products
2. 2. The process according to claim 1, characterized in that the nominal characterization of the feedstock is heterogeneous and the general chemical composition of the matrix of the feedstock varies between the following ranges: dirt 0-100%, metals 0-35%, fuels 0-90%, volatile organic 0-60%, chlorinated organic 0-60%, chlor0-20%, carbon 0-40%, nitrates 0-20% and hydroxides 0-100%.
3. 3. The process according to claim 1 characterized in that the feedstock contains organic and non-organic compounds and metals classified as hazardous or toxic according to the classification of the US Environmental Protection Agency.
4. 4. The process according to claim 1 characterized in that the feedstock contains radioactive isotopes that emit alpha, beta or gamma radiation.
5. 5. The process according to claim 1 characterized in that the feed material is transported through the side side of the melter.
6. 6. The process according to claim 1 characterized in that the surface of the melting bath is regulated with a fdepth depth controller (13) to increase the separation of volatile materials to a phase of molten ceramic glass.
7. 7. The process according to claim 1 characterized in that the portion of the fourth melter can be operated with a cooling in. the outer wall to freeze a layer of the molten product on the inner wall to ensure long operation of the melter.
8. 8. The process according to claim 1 characterized in that the ends of the electrode of the arc melter (21) can be lifted together with the lifting of the surface of the melting bath (14, 15) in a portion of the fourth smelter having a nominal depth for a diameter ratio of less than half, and the fourth (4) being rapidly movable as in a batch operation without any casting capacity.
9. 9. The process according to claim 1 characterized in that the oxygen is injected at or near the surface of the melting bath (14, 15) to control the oxidation reduction reactions in and on the melting bath (14, 15), to the generation of a syngas for the process of the feeding material and the cogeneration of combustible gas.
10. 10. The process according to claim 1 characterized in that an auxiliary heat source (16) is injected into the base of the thermal oxidizer (5) to maintain the temperature.
11. 11. The process according to claim 1 characterized in that the air enriched with oxygen is injected into the base of the thermal oxidizer (5) to maintain the temperature and provide oxygen for the oxidation reactions, for the generation of a syngas for the process of the material of power and cogeneration of fuel gas.
12. 12. The process according to claim 1 characterized in that the purified particle, the metals Volatile, salts and maintenance material of the air pollution control system such as filters can be introduced into the back of the feed material (1) and processed through the system again.
13. 13. The process according to claim 1 characterized in that the oxidation reaction reduction of the gas phase can be regulated and controlled for the generation of a syngas for processes of the feedstock and for the cogeneration of fuel gas.
14. 14. The process according to claim 1, characterized in that a molten molten metal casting product and a casting system is operated in order to control the coolant ratio of a molten ceramic glass when attempting a mold insulation or adding heat for the purpose of controlling a phase of amorphous / crystalline structure of the final products.
15. 15. The process according to claim 1, characterized in that the liquid can be absorbed in the feed material (11) or injected in the upper part of a cold layer (13) or in the surface of the melting bath (14, 15)
16. 16. A thermal partition arc melter characterized in that it comprises: to. A fourth melter with refractory lining (4) with a melt bath (14, 15) having a nominal depth for the ratio of the diameter of a fourth casting melt and slag; b. The fourth melter with refractory lining furthermore electrode parts comprising (10) at 30 ° ± 10 ° from the vertical, a supply part (9) at 90 ° from the vertical, and a port of the central malodorous gas placed vertically above of the fourth smelter; c. An electrically-based heating source comprising a graphite electrode of parallel axial translation (21) with current systems and voltage transport operating on a short or submerged arc Joule heating resistance or long arc radiant heating; d. An adjoining thermal oxidizing reactor (5) long enough to provide a residence time of more than two seconds, placed vertically above the fourth melter, with an auxiliary heating source (16) placed in the thermal oxidization; to maintain an operating temperature of 1800 ° F to 2200 ° F. and. A fourth malodorous gas extinguisher (17) directly attached to the upper part of the contiguous thermal oxidizer extended inclined at 45-60 ° from the horizontal; Y, f) An air pollution control system (6)
17. 17. The apparatuses according to claim 16 characterized in that the two graphite electrodes (21) have a nominal spacing of the ends of the electrode of one half of the melting bath (14, 15) of the nominal service diameter.
18. 18. The apparatuses according to claim 17 characterized in that the graphite electrodes (21) have translation mechanisms capable of positioning the ends of the electrode in the directions x, y and z (12).
19. 19. The apparatuses according to claim 16, characterized in that the heat source is a direct current source comprising, in addition to two translational graphite electrodes, the parallel axis (21) with current and voltage transport systems.
20. 20. The apparatuses according to claim 16, characterized in that the heat source is a graphite electrode of an alternating phase (21), a voltage current and transport system with electrodes in multiples of two.
21. 21. Apparatus according to claim 16 characterized in that the source of heat is a graphite electrode of an alternate phase (21) a system Current and voltage transport with electrodes in multiples of three.
22. 22. Apparatus according to claim 16, characterized in that they also comprise a control system for wet-dry malodorous gas (6) for the purpose of collecting volatile metal particles and salts in an aqueous stream of dissolved and suspended sludge and a filtration system of gases for the purpose of a final filtration of the gas stream.
23. 23. Apparatus according to claim 16 characterized in that they further comprise a system for purifying a dry-wet malodorous gas (6) for the purpose of separating particles and volatile metals into a processable or recyclable dry secondary stream, salts of a gas cleaner acid to a stream of dissolved or undissolved suspended muddy material, and a gas filtration system for a final filtration of the gas stream. SUMMARY OF THE INVENTION Processes and novel devices for the thermal separation of feed materials (11) for the production of a metallic product, a ceramic glass and a gaseous product. The process includes the capability of a hazardous waste thermal treatment as defined by the Environmental Protection Agency (EPA) that also contains in some cases radioactive isotopes (mixed waste as defined by the Department of Energy) and the production of hazardous waste products. long life as a result of treatment. More specifically, this invention describes both apparatuses and new processes by means of which an input feed stream (9) of widely heterogeneous nature in the description of physical form, combustibility, chemical content, and particle size and contamination with varying concentrations of components and / or radioisotopes is treated in a direct or alternating-current graphite electrode steel melter (4) with an adjoining thermal oxidizing reactor (5) for production for the production of a metallic product, a basalt as a ceramic glass product and the combustion of gases malodorous The disclosed apparatus incorporates a fast extinguishing configuration of malodorous gases. The described apparatus incorporates a fast extinguishing configuration of malodorous gases for the minimization of dioxin formation and the subsequent tranquility of the purified from the malodorous gas stream.