JPH04500718A - Method and apparatus for forming non-hazardous aggregates using hazardous waste - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] Method and apparatus for forming non-hazardous aggregates using hazardous waste Background of the invention The present invention is for forming non-hazardous aggregates from hazardous waste by thermally induced oxidation. METHODS AND APPARATUS.

Many industrial processes require storage or processing of certain materials that cannot be legally disposed of. Generates unusable by-products and waste materials. In the past, such items were found in containment vessels. Efforts to discard quality may be due to a lack of care in the manufacture of such containment vessels or The deterioration of these containers has resulted in leakage or spillage of hazardous waste. I knew that. Other means of hazardous waste disposal include introducing such materials into wells. There is injection, but these substances are injected into the may not remain stationary within the geological formations that naturally flow into the aquifers. .

Using such benefits in addition to the technical issues associated with such disposal methods Potential liability remains for any person. Several years after the material has been deposited at the disposal site, the liability The request for a This is based on the recognition that the disposal site is solely responsible for the failure to prevent waste from scattering. This may occur due to If such a problem eliminates its harmful nature, to produce products suitable for sale to and use by the general public. It sparked a search for ways to use hazardous waste in manufacturing processes. trial One of the methods seen is passing through various types of heaters under oxidizing conditions. It was the oxidation of substances. One such variation of such processing is The form uses a countercurrent rotating kiln to induce combustion of combustible components within the hazardous waste and Non-combustible materials can be sold as valuable and useful products. It is to make it into aggregate.

Efforts at individual methods of waste use will require appropriate EPA regulations related to waste disposal. We have been partially successful in producing products that will pass. However, these The process has important drawbacks. Use of hazardous waste in rotary kilns or the like The most important drawbacks associated with This is the generation of additional non-combustible materials that must be disposed of. Therefore, and Even if the amount of hazardous waste is greatly reduced by this treatment, The problem of disposing of a portion of the material that has been treated as such remains. Even the most common This process generates large amounts of contaminated scrubber water that must be treated and disposed of. generate.

Therefore, one of the objectives of the present invention is to use recyclable materials in the manufacturing process. Provide methods and equipment for the use of hazardous waste materials to improve the production of such processing. Only the product can be made harmless and be used by the general public regardless of the nature of the input material processed. and be sold for use.

Another object of the present invention is to remove harmful solid substances from harmless non-active bones that can be sold without limitation. It is to convert it into material.

Another object of the invention is to use hazardous waste liquids as fuel and fuel supplements such as natural gas or stone. Any ° solids that form as a result of using charcoal instead of charcoal are related to the harmful properties of the large blade material. by making it available in such an economical way that it can be sold to the general public without be.

An additional object of the invention is that the system can be operated without significant risk to personnel operating the system. A system for the utilization of large-scale hazardous waste materials that can be operated economically The goal is to provide the following. These and other objects of the invention are hereby incorporated by reference. more fully described herein, or may be apparent from practice of the invention.

Summary of the invention To achieve these and other objectives of the invention, converting hazardous waste into non-hazardous aggregates provide processing to do so. This process consists of large solid waste and solid waste particles. locating a source of body waste material. These substances are classified into large solids. The body waste is directed into a rotary kiln having an inlet section, a combustion section and an outlet section. in the kiln The operating conditions are that large solid waste is mixed with solid granular primary aggregate, tarinka and gaseous combustion. controlled to form by-products. Most volatile combustibles in large solid wastes The chemical substances are volatilized at the entrance of the kiln. The gaseous by-products from the kiln are sucked out from there. Exhausted by ventilation. Waste particles separated from solid waste are combustible Along with quality, it is induced by oxidative means. Combustion in oxidizing means makes waste particles non-combustible causing it to be converted into particulates, molten slag and waste gases. The temperature of the oxidizing means Preferably, the temperature is controlled within the range of 1800°F to 3000'F. No Combustible particulates and waste gases are sucked out and vented therefrom. Nonflammable fine particles The combustion products, gaseous by-products and waste gases are cooled and non-flammable particulates are removed from the combustion products and waste gases. Separated from waste gas. Solid granular primary aggregate and non-combustible fine particles are reintroduced to oxidation means. entered. The heat from the oxidizing means melts the non-flammable particulates and 1 Next conveyed onto the aggregate. The molten slag is cooled to form a harmless slag (slBged). ) Becomes aggregate. Oxidation occurs when the primary aggregate and non-combustible particulates are introduced into the oxidation means. Preferably, the means are introduced in separate batches. Furthermore, these substances are oxidized. When introduced into the stage they are introduced in the form of a pilz and free from the oxidizing means. Preferably, the heat is conducted onto the deposition surface. Furthermore, the rotary kiln starts at 1600°F. Preferably, it is operated at an average internal temperature in the range of up to 2300°F.

A preferred device for implementing the method of the present invention for converting hazardous waste into non-hazardous aggregates is It has a rotating kiln with an inlet section and an outlet end. The oxidation means are located adjacent to the inlet section of the kiln. ing. Sources of solid waste material, including large solid waste and waste particulates, are also distributed. be placed. Includes means for directing large solid waste to the inlet section of the rotary kiln As such, a means is included to separate large solid waste from waste particles. difference In addition, this equipment converts large solid waste into solid granular primary aggregate, clinker and volatilization in the kiln. It also includes means for inducing combustion that converts into gaseous gases and gaseous combustion by-products. Ru. Means are used to separate clinker from solid granular primary aggregate. Furthermore, this The apparatus comprises means for discharging gaseous combustion by-products from the kiln and from the oxidizing means. ing. Means oxidize waste particulates, volatile gases and gaseous combustion by-products in oxidation means Induce combustion to convert materials into non-flammable particulates, molten sludge and waste gases It includes things. The cooling means cools nonflammable particles in the waste gas, and the separation means Separate non-flammable particulates and waste gas. This equipment also allows for fully molten mixtures. In order to increase the Equipped with means for redirection. This means sufficiently cools the molten mixture. It has a means for producing harmless slag-like aggregate. Preferably the oxidation means is a rotary kiln. a plurality of refractory lined containers in communication with the inlet portion of the container.

The invention will now be disclosed in the preferred embodiment section.

Brief description of the drawing The drawings, which form a part of the specification, depict embodiments of the invention.

FIG. 1 is a schematic diagram of an embodiment of the present invention.

2 is a schematic partial cross-sectional view of the oxidizing means of the embodiment of FIG. 1; FIG.

Figure 3 shows the accumulation induced by the oxidation means of the embodiments of Figures 1 and 2. 1 is a schematic illustration of an example for a particulate material; FIG.

Description of preferred embodiments An embodiment of the invention is schematically depicted in FIG.

The present invention is a device for converting hazardous waste into non-hazardous aggregates and performing this function. This is the process of operating the equipment. Rotary kiln according to the invention having an inlet part and an outlet part is placed. Here, as specifically expressed and depicted in Fig. 1, the rotary kiln 1 0 has an inlet section 12 and an outlet section 14. At the inlet and outlet of the rotary kiln There is a combustion section 16 between the sections. In the illustrated embodiment, the boundaries of each part are common terminals. The three parts of the rotary kiln are for illustration only and cannot overlap. Ru. This means that some combustion may occur at the inlet section 12 or at the outlet section 14; However, it should be said that combustion primarily occurs in the combustion section 16 of the window 10.

The kiln schematically depicted in Figure 1 processes limestone or shells to make quicklime. This is a standard countercurrent rotary kiln built for the purpose of This is gold lined with firebrick It has an extragenital membrane. The synthetic components of refractory bricks are subjected to operating temperatures and passed through a rotary kiln. Determined by the material used. The rotary kiln is heated from 1600°F to 2300” In this example, designed to work in a temperature range, the 70% alumina refractory brick manufactured by N5lion*IRefrigctory in India Tiles have been used without premature deterioration of heat resistance. The rotary kiln is supported by ordinary bearings ( (not shown) and is supported by conventional kiln drive means (not shown). It is driven at a drive speed in the range of up to 75 RPBI.

As will now be discussed in more detail, the solids are guided to the inlet section 12 of the rotary kiln 10. It will be done. As the kiln rotates, material larger than about 50 microns exits through combustion zone 16. While moving towards the mouth portion 14, the smaller material is moved against the larger solid material. It is carried by the flowing gas flow. In the depicted embodiment, the rotary kiln 10 is A cooling chamber 18 is provided at the outlet portion. The cooling chamber is the part where solid materials are connected to the rotary kiln. Receive through. The chamber is the outlet section where the solid material comes out from the rotary kiln outlet, and the gutter 2 0 to receive larger solid materials transferred by rotation. Also inside the rotary kiln lO A fuel source 22 and an air source 24 are connected to the rotary kiln 10 to support the combustion of the There is. The fuel that can be used is combustible waste liquid, combustible liquid fuel or combustible natural gas. It can be a flammable liquid or gas containing gas. The temperature of oxygen or water in a compound and used to control combustion. The air and fuel mixture exits by rotating the kiln The inlet section 12 flows through the kiln IO in countercurrent to the larger solids being fed in the direction of the section. is guided into the rotary kiln 10 at the outlet section 14 with the gas flowing towards . As mentioned earlier, the smaller particles are forced into the gas flowing through the kiln. There it is separated from larger solids and discharged from the kiln. According to the invention, A device with oxidizing means is adjacent to the inlet section of the kiln. as embodied here The device includes a first oxidizer 26. As shown in FIG. 6 is adjacent to the inlet section 12 of the rotary kiln. The oxidizer 26 is the inlet part of the rotary kiln IO 12 and circulates the volatile gases evaporated from the materials introduced into the rotary kiln. It is received along with the combustion by-products from the combustion occurring in the rolling kiln. The source of waste material is wood. The material is directed into the inlet section 12 of the kiln 10, where a countercurrent flow of gas (solid waste material) and smaller particles (waste particulates). General information of the present invention The solid waste material includes large solid waste and waste particulates. present invention For the purpose of - Any waste particulate has a particle size smaller than 50 microns. It is defined as a material that has a This device can also be used to separate materials into special sizes. Non-combustible materials, volatile gases or combustion by-products that can be manipulated while passing through the rotary kiln the physical state of the larger material introduced into the kiln to be classified as providing the first oxidizer 26 with material that can be easily oxidized or melted in the oxidizer 26; is the purpose of separation.

The present invention provides for separating large solid waste from waste particles. There is a means. As embodied herein and depicted in Figure 1, this device is a waste source. a receiver for receiving material from 28 and directing waste derived fuel to inlet portion 12 of rotary kiln 10; It is equipped with 30 moving conveyors. Sorting large solid waste from waste particles This occurs throughout the rotary kiln 10. The solid waste is The waste particulates can also be sorted by size by means of oxidation. It should also be noted that it can be directly induced.

According to the present invention, this device is capable of converting large solid waste materials into solid granular primary aggregates, clay, etc. in a kiln. means for inducing combustion that converts the fuel into volatile gases and gaseous combustion by-products. Also includes. Inducing this combustion, as embodied here and depicted in FIG. The means is a fuel source 22. It is equipped with an oxygen source 24 and a rotary kiln IO.

As disclosed below, the operating conditions in the kiln are such that large solid waste is first passed through the rotary kiln. granular primary aggregate, volatile gases and gases by minimizing the amount of clinker produced by The goal is to convert the gas into sludge combustion by-products. The operation of rotary kiln lO is to It passes through the cooling chamber 18 to the outlet trough 20 towards the outlet section 14 of the rotary kiln.

As embodied here, the solid material in the outlet and trough 20 is sent to the kiln classifier 34. It will be done. Kiln classifier 34 is any conventional machine for separating large solid particles from fine solid particles. Any structural device is fine.

As embodied herein, any solid material with a diameter of 3/8 inch or larger is a primary aggregate. It is classified as something inferior to clinker. Clinker and particles are magnetically separated It is passed over the container 32.

The primary aggregate is passed over another magnetic separator 32A. Ferrous metals are removed and scrapped It is sent to a metal yard to be sold as steel.

According to the present invention, waste material particulates, volatile gases and gaseous combustion by-products are removed in the oxidation means. to induce combustion that converts the material into non-flammable particulates, molten slag and waste gases There are means provided. Inducing combustion within the oxidizing means as embodied here The means for doing so includes a source of oxidizer fuel 36 and a source of oxygen. This way Thus, the oxidizer 26 can be combustible or non-flammable from the rotary kiln IO. Waste particulates and volatile gases are removed from the rotary kiln lO by combustion by-products from the fuel source 36. and oxygen from an oxygen source 38 . In this embodiment, the first oxidizer 26 is Works in temperatures ranging from 1800°F to 3000°F. In an oxidizing environment, Combustible materials within the oxidizer 26 are converted to waste gas and non-combustible particulates. Nonflammable Particulates may or may not be fused depending on their composition.

As schematically shown in Figure 2, some of the non-flammable particulates are melted and liquid It is collected at the bottom of the first oxidizer 26 in the form of a ludge 40. In Figure 2, the liquid slurry Although the sludge is shown being discharged from the apparatus by a sludge boat 42, Such sludge ports are selectively located along the bottom of the first oxidizer 26. can be As shown in FIG. 2, the sludge boat 42 With a burner 44 arranged to maintain the material in the vicinity of the boat 42 in a molten state. associated with. Increasing the temperature at various locations within the oxidizer 26 For this purpose, the device selectively directs a burner directly into the first oxidizer 26. As depicted in FIG. It is a refractory lined container in communication with the inlet section 12 of the O. The first example of this example The oxidizer has a rectangular cross section and includes a metal shell 46 with an internal refractory lining.

The refractory lining of the depicted embodiment includes a refractory brick 48 and a monolithic refractory lining 50. do. In the example depicted, the refractory brick is N5 from Oakland, California. It is 70% alumina manufactured by Lioul Rzfrtchlor7. Inside the integral structure The wire is J*dtPxk manufactured by A, P, Gtum of Mexico City, Missouri. . The refractory brick at the bottom of the first oxidizer 26 in the embodiment is a wall part of the first oxidizer 26. It is much thicker than firebrick. This passes through the interior portion 52 of the oxidizer 26. oxidizer caused by a flowing liquid sludge 40 that transfers heat from hot gases. Based on the operating temperature in that area. Another preferred embodiment of the first oxidizer is a water It has a cold ceiling, water-cooled metal walls, and a fireproof floor. Such a structure allows for higher operating temperatures. enable.

In the embodiment of FIG. 2, the hot gas is connected to the first oxidizer 26 to the second oxidizer 56. It is bent 90 degrees toward the conduit 54. The structure of the second oxidizer 56 is similar to that of the first oxidizer. It is similar in some respects to that of However, in the example shown, The second oxidizer 26 is cylindrical with an interior 58 that is also cylindrical.

Gas and particulates are passed from the first oxidizer 26 through a conduit 54 to a second oxidizer 56. Towards and passing through. The construction of conduit 54 and second oxidizer 26 is such that they are within the refractory range. The structure of the first oxidizer of the embodiment depicted in that it consists of stretched steel; Similar. The refractory material used in conduit 54 is JxdsPxk, and the second The refractory material used in the oxidizer 56 is JldrPtk. First oxidizer 26 Similarly, the second oxidizer 56 also includes multiple layers of refractory bricks in its bottom portion. Prepare. The functionality of this multilayer refractory material has been discussed above.

In the depicted embodiment, all of the waste material combustion occurs within the first oxidizer 26. It's not like that. A significant portion also occurs in the second oxidizer 56. therefore In operation of the embodiment of FIG. 52 through conduit 54 into an interior portion 58 of second oxidizer 56 .

In a preferred embodiment, the liquid is now in the first position as embodied by liquid inlet 60. 2 into the oxidizer 56. The liquid source for the liquid inlet 60 in this embodiment is A sump system (not shown) is provided that surrounds the entire device. Waste derived combustion Any liquid containing rainwater, rainwater or contaminated rainwater shall be controlled by the sump system. and is injected into the second oxidizer 56 through the liquid inlet 6o. However, The entire device is designed to dissipate waste derived fuel and contaminated water surrounding the device. Have the means for personal use. A person skilled in the art to which the present invention pertains will understand such a system. Drainage device and sump such that the invention can be operated without specific description of the stem The system can be easily designed.

According to the invention, means are provided for cooling non-flammable particulates and waste gas. ing. As schematically embodied and depicted in FIG. 1 herein, cooling vessel 62 is equipped.

The cooling container 62 is equipped with a water inlet 64 . In this embodiment, the water inlet 64 is located therein. , has a nozzle (not shown) that introduces water and air faster than the speed of sound.

The spray nozzle used in this example is SCCN manufactured by 5onic, New Chassis. It is "5onic" of R-03-F-02 model. In communication with the water inlet is the water source 66. In this embodiment, the water source 66 is supplied with waste-free water. Ru. Its function is to remove approximately 350 waste gases and non-flammable particulates from the water source 66. The purpose of this is to cool the gas to a temperature between and particulate matter can be separated by conventional separation means described below. Ru.

Alkaline liquid as a spray, as schematically embodied and depicted in FIG. in communication with a spray nozzle 70 that introduces the body into a dry spray reaction vessel 62. There are sources of alkaline substances. Its alkaline substance spray injection function is to neutralize any acids in the waste gas.

According to the invention, the apparatus collects gaseous combustion by-products from the kiln and waste gas from the oxidizer means. shall be provided with means for passing the water. As embodied here, there is a second oxidation A connector 72 is provided that communicates between the vessel 56 and the dry spray reactor 62. ing. This connector has a similar construction to the second oxidizer, i.e. it has a fireproof lining. It has a structure consisting of a metal shell. Similarly, the dry spray reactor 62 is also fireproof. It is a stretched metal container.

The effects of differential thermal expansion must be considered when making connections between the various elements of the invention. . Because the material in oxidizers 26 and 56, conduit 54 and connector 72 This is because the temperature is very high. Additionally, meaningful temperature differences in different parts of the device Because of the existence of must be carried out.

As described below, the system is operated at subatmospheric pressure. Therefore the device Any leakage at the connections between parts of the oxidizer will adversely affect the combustion of the material in the oxidizer. As long as it is not exceeded to the extent that it causes an adverse effect, it will not be detrimental to the performance of the equipment. This cornerstone The requirements are less important in other parts of the equipment that operate at lower temperatures.

According to the invention, the device comprises means for separating non-flammable particulates and waste gas. do. As embodied here and schematically depicted in FIG. two filter systems each having a filter 74 and a fan 76. Be equipped. Waste gases and particulates are preferably kept above 350°F <400°F. Since it is introduced into the filter at a lower temperature, it can be ) filter can be used. The operation in this example is performed using ordinary Teflon fibres. It has been determined that a filter element can be used in connection with this operation.

The waste gas is separated from non-flammable particulates, and the waste gas is separated from the waste gas composition and It passes through a monitor means 78 that monitors the temperature. And the waste gas goes through the chimney 80. is passed through to the atmosphere.

Fans 76 are provided throughout the apparatus for sucking volatile gases and combustion by-products from the rotary kiln. Stand up and perform suction. Combustion by-products from rotary kilns, combustion by-products from oxidizers and All gas passing through the stem passes through fan 76, so the entire system is at atmospheric pressure. It works as below. Particles accumulated in filter 74 are pumped by pump means 82. It is passed to the mulrator 84. Similarly, the primary aggregate passes through pump 86 to the data 84. A preferred embodiment of accumulator 84 is depicted in FIG. Photographed.

According to the present invention, solid particulate primary aggregate is introduced into the device and non-combustible particulates are re-induced. Means is provided for bringing the mixture into a sufficiently molten mixture. This is embodied here and the first As depicted in Figures 1 and 2, the equipment oxidizer means, in particular means leading to the second oxidizer 56.

As depicted in FIG. 3, accumulator 84 receives particulates from pump 82. A first inlet 88 is provided which is arranged to accommodate the inlet. Accumulator 84 Additionally, a second inlet 9 is arranged to receive the primary aggregate through the pump 86. 0.

a first for detecting a desired maximum level of particulate matter within accumulator 84; Sensor 92 is associated with the preferred embodiment of accumulator 84. second cell The sensor 94 detects the level of particulate matter within the accumulator 84 and controls the sensor control mechanism. The valve 98 is operated by the valve control means 100. NOTE DURING EQUIPMENT OPERATION Inlets 88 and 90 introduce particulate material into accumulator 84 where the particulate matter is The substance accumulates to a predetermined level such that the upper sensor 92 is activated. , opening the valve 98 by the control sensor control means 96 and the valve control 100; Particulate matter is thereby passed through conduit 102 to a second oxidation stage as shown in FIG. can be sent into the container 56. Level of particulate material in accumulator 84 If the signal reaches the level of the lower sensor 94, then the sensor control and valve control 1 00 closes valve 98, thereby blocking the flow of particulate matter through conduit 102. .

Conduit 102 was shown to direct solid particulate material into second oxidizer 56. However, solid particulate matter may be present in the first oxidizer 26 or in both the first and second oxidizers. You can also be guided to As shown in FIG. The solid particulate matter directed into the second oxidizer 56 enters the central portion 58 of the second oxidizer 56. and fall, and form a deposit on the bottom. Is the gas passing through the second oxidizer 56? The heat from The molten particulate matter is transferred to the surface of the deposit. Isn't the substance melted in it? from the pile 104 which also carries particulate matter, and from the slug boat 42. It joins the melting step 40.

According to the invention, the device cools a nearly molten mixture to form a non-hazardous aggregate. have the means to do so. As embodied herein, the apparatus is schematically depicted in FIG. The illustrated cooling means 106 is provided. In a preferred embodiment, the cooling means is substantially molten. The mixture simply has water drained into it. Is the cooling method a molten mixture? removes heat and forms non-toxic aggregate.

The operation of the equipment described above now eliminates hazardous waste in the manufacturing process to form non-hazardous aggregates. Methods for use will be described. According to the invention, the first step The step provides a source of solid waste material consisting of large solid waste and waste particulates. It is to provide. In embodiments of the invention, waste may be delivered to the device in various forms.

Wastes include contaminated topsoil, contaminated construction debris, and semi-solid waste from wastewater treatment operations. Mud, metal drums of liquid waste, fiber drums containing liquids or solids (usually It is in the form of a granular solid, such as love back (called Ixb psck). be able to. When the waste material is sludge containing liquid, the waste is first The liquid is separated and stored separately from the solid residue in the apparatus of the present invention. will be introduced in When the waste is in a 55-gallon metal drum, the The rum cans are chopped up and introduced into a rotary kiln as a large solid waste piece. , thereby eliminating the need for drum cleaning or inspection. Also, large knives It is also necessary to chop the material multiple times to obtain a large blade material that is effectively consumed in the process. may be required.

In controlling the process and the operating temperatures of the various components that carry out the process, It is advantageous to know certain properties of the blade material so that waste materials and The feed rate of the material and other large blade materials can be controlled to obtain the desired operating conditions.

Preferably, the waste material reaches a description that will include BTU and water content. death However, the BTU content and other characteristics of the large blade material can be adjusted to make the device easier to operate. There is a need to inspect. While a load of waste material can have one value of total BTU , the waste is often non-homogeneous and therefore equipment operation and process control are complete oxidation of the combustible components of the waste and the desired non-hazardous aggregates. It is worth noting that the operating parameters should not deviate from the need to generate Ru.

In addition to BTU and water content, acid content, ash content and halogen concentration are It is also advantageous to know. The acid content of the waste should be determined by the operator based on process operation and How much alkaline agent is consumed in the process, which has a strong impact on both its economic efficiency provide a means of assessing whether The amount of ash in the waste depends on how much aggregate is produced. determine whether Halogen content affects process operation and Preferably, this ranges from 10 to 15%. To obtain the desired operating conditions Using these properties of waste, water, auxiliary fuel, oxygen, alkaline agents, desirable aggregates by proper control of the input of coolants and the like. can be manufactured economically.

According to the invention, the process comprises the step of separating large solid waste from fine particles. , as mentioned above, this separation occurs in the rotary kiln 10 or is suitably sized. This can be achieved by simply directing the collected waste to different locations on the device. Wear. For example, if the waste particles are contaminated topsoil, they are can be guided directly to the stage.

According to the invention, the process includes a large solid waste input section, a combustion section and an exit section. a rotary kiln in which there is a rotary kiln. The operating conditions in the kiln are large solids The waste is burned to produce solid granular primary aggregate, clinker and volatilization at the input of the kiln. gaseous combustion with the majority of volatile combustible materials in large solid wastes is combusted to form a product. The rotary kiln is approximately 1600°F to 2300°F. Preferably, it is operated at an average internal temperature within the range of °F.

There are significant temperature gradients within the kiln along its length and in the radial direction. It should be noted that Therefore, the kiln section is heated from 1600°F to 2300° may significantly deviate from the F range.

Large solid wastes are guided into the rotary kiln, the speed of which depends on the BTUiit. However, it is usually about 20 tons per hour. The kiln is within the range of 1 to 75 RPII. Since it is rotated at a speed, the total residence time of the solid material present in the kiln at the outlet section 14 is It is in the range of about 90 to 120 minutes.

With these operating parameters the rotary kiln can be classified as a clinker. producing a solid output consisting primarily of solid granular primary aggregate with a quantity of material. Main departure For manufacturing purposes, clinker is usually an unreacted building block passed through a rotary kiln, for example. Like tiles or agglomerates of low-melting-point substances that are melted and aggregated at relatively low temperatures in a rotating kiln. It is a solid of large size. The operating conditions of the rotary kiln are designed to facilitate two conditions. controlled by.

One is to convert most of the large solid waste into solid granular primary aggregate; and two. The first is to eliminate most of the volatile combustible materials in the large solid waste in the input section of the rotary kiln. It is to evaporate. The primary aggregate is melted as will be discussed below. It is recycled into the process and directed to a melting step within an oxidizing means. Ste The cup is formed into non-toxic aggregate so that as much of the treated material as possible can form into the shape. It is desirable to be converted. The substances that form the clinker output from the kiln have been tested It is determined whether there are any hazardous substances that can be leached from it. leaching Any material that grows potentially harmful substances is redirected into the rotary kiln at the input section. Ru. The operation and process of this equipment results in a rotating material classified as clinker material. Produces a very small output from the kiln.

A secondary objective when operating a rotary kiln is to eliminate volatile combustible materials within the input section of the rotary kiln. The goal is to volatilize most of it. This passes through the rotary kiln and the combustion part 1 of the rotary kiln Reduce the amount of BTU of solid material going into 6. If the combustion part 1 of the rotary kiln lO If the BTUfi of the solid part is too high, reaching 6, uncontrolled combustion will occur. Can occur within the combustion section of a kiln. Therefore, the operating conditions for a rotary kiln are very sufficient input to volatilize most of the volatile components in the large solid waste. Temperature at the power point should be provided.

As shown schematically in FIG. Sent to 34th. The classifier 34 separates large solid particles from solid fine particles. Any conventional mechanism may be used. As embodied here, 3/8 inch Any solid material with a larger diameter than anything smaller is a primary aggregate. It is classified as a tarinka. The tarinka and particles pass over the magnetic separator 32. Ru. The primary aggregate passes over another magnetic separator 32A. The ferrous metal is separated and Sent to a metal yard to be sold as crap steel.

According to the invention, the gaseous combustion by-products from the kiln are transported therefrom by suction draft. It will be done. As mentioned above, the fan 76 maintains the entire system below atmospheric pressure; and draw gas from the rotary kiln as well as from the oxidizer throughout the apparatus.

According to the invention, the process includes directing the waste particulates to an oxidizing means. Here As embodied, the waste particulates from the rotary kiln 10 are entrained in the gas stream and oxidized. It is carried into the container 26.

According to the invention, combustible substances are directed into the oxidizing means.

As embodied herein, there is a source of liquid fuel 36 coupled to the first oxidizer 26. do. fuel, waste particulates, volatile side gases from solid waste materials in the kiln, and oxygen. All injection inputs should be in the range of approximately 1800°F to 3000°F Used to control the temperature within the first oxidizer. Its temperature is determined by any induced compensation. It is determined by the BTUfi of the large blade material which also includes the auxiliary fuel. supplement from fuel source 36. Preferably, the co-fuel comprises combustible liquid waste material. The flammable liquid waste material It is further preferred to include a liquid that is an organic solvent, drilling mud waste, or paint. Yes.

According to the present invention, the process involves inducing combustion in the oxidizing means to transform waste particles into non-flammable particles. , a melting step and a step of converting to waste gas. embodied here As shown, the oxidizer means includes two oxidizers, a first oxidizer 26 and a second oxidizer. A container 56 is provided. In the first oxidizer 26, most of the combustible material is oxidized. Forms gaseous combustion by-products. These pass through the interior 52 of the first oxidizer 26 and It is pumped through tube 54 into the interior 58 of second oxidizer 56 . Operating temperature is 18 00° to 3000° is preferred and some of the solid material is melted. this substance is added to the bottom portion of the first oxidizer as a liquid step 40 as shown in FIG. The water is collected and flows towards the step boat 42. solid particles not yet melted The gaseous combustion by-products pass through conduit 44 into the interior of oxidizer 56; Here a portion thereof can be melted in the second oxidizer 56 or It is also possible that the solid particulate waste passes through the equipment untreated.

According to the invention, solid particulate primary aggregate and non-combustible particulates are introduced into the oxidizing means. It will be done. As embodied here and clearly depicted in FIG. The aggregate and solid particulates are directed into the interior of the second oxidizer 56. Primary aggregate and Preferably, the solid particulates are introduced into separate chunks. This into the oxidizer The continuous induction of these materials is due to the accumulation of particulate matter within the oxidizer, which prevents surface melting. cooling the surface. This inhibits oxidizer-induced particulate matter melting and thereby inhibiting the formation of a melting step that would form a non-hazardous aggregate.

As shown schematically in FIG. Preferably, the second oxidizer is directed to the second oxidizer to form a deposit within the oxidizer. acid The heat from the oxidation means is transferred onto the surface of the deposit, on which surface it has a relatively low melting point. The material melts and flows down to the bottom of the oxidizer and towards conduit 54 where it is The molten material exits the step boat 42. The process involves increasing the temperature of the second oxidizer It is possible to generate slag-like aggregate or non-combustible fine particles with a melting point higher than that of can. Therefore, such particulate material is not melted. But it is the second into the molten material formed in the oxidizer and into the step. , forming a molten mixture. by melting the surface of the deposit, and The molten material and solid particulate material flowed therein flow towards conduit 44 This exposes new surfaces on the particulate material and It is then melted and flows out of the device through the step port. shown here Although the examples show the introduction of primary aggregate and non-combustible particulate matter into the second oxidizer. , the process also operates if a portion of the material is directed to the first oxidizer. It is possible. In addition, primary aggregates can be added to both oxidizers, or fine particles can be added to both oxidizers individually. It is also possible to inject into It is preferred to combine and redirect them into the process as a combination.

The embodiment of FIG. 2 also shows an apparatus for injecting oxygen into the first oxidizer.

The process is also operable to inject oxygen into the second oxidizer. Preferred operation of the device During operation, the average temperature within the first oxidizer is approximately 3000°F. first oxidizer and The temperature in the conduit between the second oxidizer is 2800°F; is approximately 2800″F. The second oxidizer is also designed to receive a relatively small amount of liquid. so that any combustible hazardous waste in the liquid is oxidized in the oxidation means. It is preferable that the As embodied here, the injection port 60 is provided with This is the second oxidizer. At the operating temperature of the second oxidizer the water is evaporated and Solids may be combusted by a hot gas stream, melted, or treated with other non-flammable materials. Either it is sent along with the particles to the downhill part of the device.

Waste gases and gaseous combustion by-products and non-flammable particulates from the oxidizing means are removed by water injection. More preferably, the liquid is cooled to form a cooled effluent. It is embodied here and As schematically depicted in FIG. Means for injecting water into the Leh reactor 62 is provided. The water is about 400°F. forming a cooling effluent having a temperature lower than 350'F and preferably higher than 350'F. preferable. It is further preferred that any acid in the cooled effluent is neutralized. child As embodied herein and schematically depicted in FIG. means for introducing a neutralized effluent containing non-combustible particulates and waste gases. have The waste gas is preferably separated from non-flammable particulates by dry filtration. stomach. This step allows non-flammable particulates and waste gases to pass through a regular baghouse. This is achieved by A fan connected to a baghouse, i.e. this example Since the first fan 76 draws suction throughout the device, the device is below atmospheric pressure. Operated at low pressure.

According to the present invention, the process includes a melting step and cooling of the mixture with solid particles to form non-toxic aggregates. comprising steps for forming a.

In a preferred embodiment, the mixture of melting step and solid particles is placed in a water-filled container. Guided by Beya. Here the cooling effect of water cools the mixture, making it solid, harmless and non-toxic. A leachable aggregate is formed. The water used to cool the molten material there is discarded. For treatment with water into the second oxidizer or into the cooler 62 as cooling water be redirected to.

Operation of the apparatus of the invention results in the production of four emissions: Ferrous metal without harmful substances; if it contains harmful substances, they are bound in the clinker structure Either the clinker is removed or re-introduced into the process until the clinker composition becomes harmless. Clinker passing through a rolling kiln. And the third emission is the gaseous emission from the chimney 80. It is mainly carbon dioxide and water. The preferred embodiment is a hazardous waste incinerator. air quality certification even though it is not classified and is not required for hazardous waste incineration. is based on the same considerations as applied to Part “B” of hazardous waste incinerators.

The present invention meets these criteria without difficulty. More convincing air quality specifications In addition to eliminating heavy metals that would be harmful if separated from the aggregate. The aggregate produced from this process contains heavy metals trapped within the glassy aggregate. Converts matter into a given shape. In particular, arsenic, barium, cadmium, chromium levels of aluminum, lead, mercury, selenium, and silver are all well below specified limits.

In addition, insecticide herbicide compounds, acid phenolic compounds, neutral base compounds, and others The concentration of volatile compounds is well below the specified limits. Therefore, there is a large blade material. Even if they contain harmful substances, they may be oxidized by oxidation treatment or The process produces non-hazardous emissions.

The invention has been described by means of preferred embodiments. However, the present invention is not limited thereto. Not possible. The scope of the invention is defined by the appended claims and their equivalents. determined only.

To Shishi FIG, 3゜ Submission of translation of written amendment (Article 184-7, Paragraph 1 of the Patent Law) Plain! March 14th, 3rd year

Claims (59)

[Claims] 1. A method for forming non-hazardous aggregates using hazardous waste, providing a source of solid waste material comprising large solid waste and waste particulates; , Inducting the large solid waste into a rotary kiln having an input section, a combustion section, and an exit section. to guide and separating the large solid waste from the waste particulates; The large solid waste is burned to produce solid granular primary aggregate and clinker and gaseous combustion byproducts. controlling operating conditions in the kiln to form a product; Most of the volatile combustibles in the large solid waste are volatilized in the input section. Toto, removing the gaseous combustion by-products from the kiln by drafting; directing said waste particulates to said oxidizing means; and directing combustible substances to said oxidizing means. and inducing combustion within said oxidizing means to transform said waste particulates into non-flammable particulates. converting particles into molten slag and waste gas and controlling the temperature within said oxidizing means. controlling the non-flammable particulates and the waste gas from the oxidizing means; displacing the non-flammable particulates and the gaseous combustion by-products by ventilation; and cooling the waste gas; separating the non-combustible particulates from the gaseous combustion by-products and waste gas; directing the solid particulate primary aggregate into the oxidizing means and re-inducting the non-combustible particulates; to guide and Heat from the oxidizing means is transferred onto the non-flammable fine particles and the primary aggregate to melt the forming a mixture of rags and solid particles; cooling the mixture of molten slag and solid particles to form the non-hazardous aggregate; and a method of comprising. 2. The primary aggregate and the noncombustible fine particles are introduced into the oxidizing means in separate chunks. 2. A method according to claim 1, wherein said method comprises: 3. Said portions of primary aggregate and non-combustible particulates form deposits within said oxidizing means. The method according to claim 2. 4. 4. A method according to claim 3, wherein heat from said oxidizing means is conducted to the surface of said deposit. 5. the deposit has a sloped external surface, the surface being propagated onto the surface; 5. A method as claimed in claim 4, including heat from said oxidizing means. 6. The sloped exterior surface is melted and the molten material on the surface is transferred to the surface. 5. Flowing from a surface exposing a new surface of unmelted material on said deposit. Method described. 7. The rotary kiln operates at an average internal temperature within the range of about 1600 to 2300°F. 2. The method according to claim 1, wherein 8. The operating parameters of the rotary kiln are arranged such that mainly from the solid granular primary aggregate 2. The method of claim 1, wherein the method produces a solid state output consisting of: 9. The oxidizing means includes a plurality of oxidizers including at least first and second oxidizers. How to equip. 10. The first oxidizer includes additional potential in the form of the waste particulates and liquid fuel. receiving a combustible material and the gaseous combustion by-products from the kiln, the first oxidizer having about 10. The person of claim 9, which operates at an average internal temperature within the range of 1800 to 3000 degrees Fahrenheit. Law. 11. 11. The method of claim 10, wherein the liquid fuel comprises combustible liquid waste. 12. comprising the step of redirecting the nonflammable fine particles back to the first oxidizer. The method according to claim 3. 13. directing the solid granular primary aggregate to the first oxidizer. The method according to claim 9. 14. A second oxidizer receives combustion byproducts and non-flammable particulates from the first oxidizer. and said second oxidizer has an average internal temperature within the range of about 1800 to 2800°F. 10. The method of claim 9, further comprising: 15. comprising the step of redirecting the nonflammable fine particles back to the second oxidizer. 15. The method according to claim 14. 16. directing the solid granular primary aggregate to the second oxidizer. 15. The method according to claim 14. 17. The solid granular primary aggregate and the noncombustible fine particles are mixed, and the mixture is 15. The method of claim 14, comprising adding to the second oxidizer. 18. 10. The method according to claim 9, further comprising the step of injecting oxygen gas into the first oxidizer. the method of. 19. 10. The method according to claim 9, further comprising the step of injecting oxygen gas into the second oxidizer. the method of. 20. 10. The method of claim 9, further comprising the step of injecting waste liquid into the second oxidizer. the method of. 21. said waste gas from said oxidizing means, gaseous combustion by-products and non-flammable particulates; Claim wherein the oxidizing means is cooled by injection of moisture into the oxidizing means to form a cooled effluent. The method described in Section 1. 22. The cooled effluent is cooled to a temperature within the range of 350°F to 400°F. 22. The method according to claim 21. 23. 22. The method of claim 21, wherein the acid within the cooled effluent is neutralized. 24. The acid is neutralized by introducing an alkaline solution, forming non-flammable particles. 24. The method of claim 23, forming a neutralized effluent comprising waste gas. 25. The neutralized exhaust is separated into nonflammable particles and waste gas by dry filtration. 25. The method of claim 24, wherein the method is separated. 26. 26. The step of dry filtration is performed by a baghouse. the method of. 27. Claim 1 wherein said kiln and said oxidizing means are operated at a pressure below atmospheric pressure. Method described. 28. cooling the solid material exiting the outlet end of the kiln. 2. The method according to claim 1. 29. The non-combustible fine particles and the solid granular primary aggregate are in communication with the oxidizing means. 2. The method of claim 1, wherein the materials are collected in a container. 30. The noncombustible fine particles and the solid granular primary aggregate are and in response to said solid granular primary aggregate reaching a predetermined level within said container. 30. The method according to claim 29, wherein the oxidation means is located within the oxidation means. 31. A method for forming non-hazardous aggregates using hazardous waste, providing a source of solid waste material comprising large solid waste and waste particulates; , Inducting the large solid waste into a rotary kiln having an input section, a combustion section, and an exit section. to guide and separating the large solid waste from the waste particulates; The kiln is operated at an average internal temperature within the range of 1600° to 2300°F and below atmospheric pressure. Operating at lower pressures and the majority of volatile combustible materials in large solid wastes to volatilize the liquid at the input part of the rotary kiln, and to control the state inside the kiln to The body waste is combusted into solid granular primary aggregate, solid clinker and gaseous combustion by-products. Most of the solid material coming out of the outlet of the kiln is solid granular primary controlling the content of aggregate, said waste particulates and said gaseous combustion byproducts; a first oxidizer communicating product, auxiliary fuel and oxygen gas with an input portion of the rotary kiln; and the temperature in the first oxidizer is approximately 1800° to 3000°. inducing combustion within the range of F; melting in an oxidizer to form a molten slag; Gaseous combustion by-products and molten particulate matter from the first oxidizer are transferred to the first oxidizer. oxidizer, said second oxidizer being in communication with the oxidizer of operating at an average internal temperature within the range of from to 2800°F; Gaseous combustion products and unmelted particulate matter from the second oxidizer are transferred to the second oxidizer. through a cooling and neutralization vessel in communication with the oxidizer of No. 2; the gaseous combustion by-products and unmelted particulate matter from the second oxidizer; The temperature inside said container is increased to about 400° by injecting a liquid containing water into it. cooling to a temperature lower than F; The acid in the gaseous combustion by-products from the second oxidizer is removed from the alkaline liquid in the volume. Neutralize by injecting into the vessel, forming gaseous emissions and cooled particulate matter and dry filtering the neutralized gaseous effluent from the cooled particulate material. separating by passing; discharging said neutralized gaseous emissions; and discharging said cooled particulate matter and said combining and collecting primary aggregate; Periodically the combined and cooled granular material and primary aggregate are placed in a second oxidizer. inducing a deposition having a sloped exterior surface adjacent the bottom of the second oxidizer; forming and conducting heat from the first oxidizer to the sloped surface of the deposit. , and melting at least a portion of the substance therein; the molten material and any molten material flowed therein with the molten slag; forming a substantially molten mixture; removing the substantially molten mixture from the oxidizer; and removing the substantially molten mixture from the oxidizer. cooling the compound to form the non-hazardous, non-leachable aggregate. 32. 32. The method of claim 31, wherein the waste particulates comprise contaminated soil. 33. 32. The method of claim 31, wherein the supplemental fuel comprises combustible liquid waste material. 34. The flammable liquid waste materials include organic solvents, waste petroleum products, and drilling mud waste liquids. body and a liquid selected from the group consisting of paint and other organic and inorganic liquids. 34. The method of claim 33, comprising: 35. 32. The method of claim 31, comprising injecting a liquid into the second oxidizer. Method. 36. A device for converting hazardous waste into non-hazardous, non-leachable aggregates, a rotary kiln having an inlet section and an outlet end door; and oxidizing means adjacent to the inlet section of said kiln. and said source of solid waste material comprising large solid waste and waste particulates; means for separating the large solid waste from the waste particulates; means for directing the large solid waste to the inlet section of the rotary kiln; means for directing said waste prior to said oxidizing means; Combustion is induced in the kiln to clean the large solid waste with solid granular primary aggregate. means for converting mosquito into volatile gases and gaseous combustion by-products; means for separating the clinker from the solid particulate primary aggregate; Combustion is induced in the oxidizing means to separate the waste particulates, the volatile gas and the gas. for converting sludge combustion by-products into non-flammable particulates, molten slag and waste gas. means; and the gaseous combustion by-products from the kiln and the waste gas from the oxidation means. and a means for communicating with means for cooling the non-flammable particulates and the waste gas; means for separating the non-flammable particulates and the waste gas; The solid granular primary aggregate is introduced into the molten slag and the non-combustible fine particles are recycled. means for inducing to form a substantially molten mixture; cooling said nearly molten mixture to form said non-hazardous non-leachable aggregate; An apparatus comprising means. 37. The oxidizing means comprises a plurality of refractory-lined units communicating with the inlet portion of the rotary kiln. 37. The apparatus of claim 36, comprising a container. 38. The oxidation means includes the waste particulates, volatile gas from the kiln, and the kiln. and a first oxidizer arranged to receive the gaseous combustion by-products. The device according to claim 37. 39. the apparatus comprising means for injecting auxiliary fuel into the first oxidizer; 39. The apparatus of claim 38. 40. the apparatus comprising means for injecting oxygen gas into the first oxidizer; 39. The apparatus of claim 38. 41. Claim wherein the first oxidizer comprises a burner for heating the substance therein. The device according to item 38. 42. A method for guiding the non-combustible fine particles and the primary aggregate to the oxidizing means. 37. The apparatus of claim 36, comprising a stage. 43. The means for inducing the non-combustible fine particles and the primary aggregate comprises: A claim comprising an accumulator for receiving non-combustible particles and the primary aggregate. 43. The device according to claim 42. 44. The accumulator has the non-combustible particulates and the primary aggregate therein. Collect until the level of substance in the accumulator reaches a predetermined level valve means connected to said accumulator; the non-combustible characteristic particles and primary aggregates are allowed to pass into said oxidizing means. 44. The apparatus of claim 43, wherein the apparatus is arranged to enable. 45. guiding the non-flammable fine particles and the primary aggregate into the first oxidizer; 40. The apparatus of claim 39, comprising means for determining. 46. means for removing the molten slag from the first oxidizer. 39. The apparatus of claim 38. 47. 39. The method of claim 38, further comprising a second oxidizer in communication with the first oxidizer. equipment. 48. guiding the non-flammable fine particles and the primary aggregate into the second oxidizer; 48. The apparatus of claim 47, comprising means for determining. 49. 47. Claim 47, comprising means for injecting a liquid into said second oxidizer. The device described. 50. 48. The apparatus of claim 47, wherein the apparatus comprises a conduit between the first and second oxidizers. equipment. 51. said conduit comprising means for removing said molten slag from said oxidizing means; 51. The apparatus of claim 50, comprising: 52. 50. Claim 49, wherein said conduit comprises a burner for heating the substance therein. equipment. 53. The cooling means comprises a cooling container in communication with the oxidizing means and removes moisture. 37. The apparatus of claim 36, comprising means for injecting into said cooling vessel. 54. 54. The apparatus of claim 53, wherein the moisture is injected into the container at supersonic velocity. 55. Injecting an alkaline liquid into the cooling vessel to neutralize the acid in the waste gas. 54. The apparatus of claim 53, further comprising means for causing. 56. said means for separating non-combustible particulates and waste gas comprises a baghouse; 37. The apparatus of claim 36. 57. the gaseous combustion by-products from the kiln and the waste gas from the oxidizing means; said means for passing a gas, said means for inducing a subatmospheric pressure within said device; 37. The apparatus of claim 36, comprising a stage. 58. said pressure reducing means comprises at least one fan associated with said separating means; 58. The apparatus of claim 57, comprising: 59. said for separating said larger solid waste from said waste particulates; 37. The apparatus of claim 36, wherein the means comprises the rotary kiln.