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Title:
METHOD AND INSTALLATION FOR PROCESSING OF HAZARDOUS WASTE FROM RECYCLING LEAD-ACID BATTERIES
Document Type and Number:
WIPO Patent Application WO/2018/145172
Kind Code:
A1
Abstract:
The Invention will find application in the processing of hazardous waste, which contains lead compounds, polymers, metals and other waste. The method includes stages as follow: A first stage (A) where is conducted a pre-processing of hazardous waste by reducing the size of the waste, a neutralization with an alkaline solution, a chemical treatment for cleaning out of the pollutants, and drying. A second stage (B), where is conducted a sorting of the processed AGS and PC waste for landfilling, and polypropylene is released, as well as polyethylene separators with a silicon dioxide filler which are fed in third stage (C) for processing via gasification. This results in a gas phase and gives out amorphous silicon dioxide which is directed for its subsequent use. The gas phase is fed to a fourth stage (D), which is a combustion process at a temperature not lower than 900°C in a thermal oxidizer. After the combustion process, the hot gases are sent in energy module (E) for utilization.

Inventors:
ZHEKOV SERZHO SIMEONOV (BG)
SLAVOV SIMEON KOSTADINOV (BG)
BOBOKOV ATANAS STOILOV (BG)
BOBOKOV PLAMEN STOILOV (BG)
BOGDANOV VASIL TSVETKOV (BG)
Application Number:
PCT/BG2017/000030
Publication Date:
August 16, 2018
Filing Date:
December 08, 2017
Export Citation:
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Assignee:
ASTECH 2015 LTD (BG)
International Classes:
C01B33/12; C22B13/02; H01M10/54
Domestic Patent References:
WO2007026322A22007-03-08
Foreign References:
US7772452B22010-08-10
CN102208705B2013-06-19
US7772452B22010-08-10
Other References:
WEI ZHANG ET AL: "A critical review on secondary lead recycling technology and its prospect", RENEWABLE AND SUSTAINABLE ENERGY REVIEWS., vol. 61, 1 August 2016 (2016-08-01), US, pages 108 - 122, XP055460457, ISSN: 1364-0321, DOI: 10.1016/j.rser.2016.03.046
Attorney, Agent or Firm:
YANAKIEVA-ZLATAREVA, Maria Nikolova (BG)
Download PDF:
Claims:
CLAIMS

1. Method for processing of hazardous waste that contains lead compounds, polymers, metals, and other waste that includes a first stage for the separation of lead, follow-up chemical treatment for cleansing of pollutants, and drying characterized in that in the first stage (A) there is conducted a pre-processing of hazardous waste that takes place in four stages where in the first stage (Al) the size of the hazardous waste is reduced, and besides the lead there are also released magnetic metals, and the lead and magnetic metals are directed via separate outlets for subsequent use, while the remaining part of the hazardous waste in second stage (A2) is subjected to neutralization with an alkaline solution, and after the neutralization, in a third stage (A3), there is conducted the chemical treatment for cleaning out of the pollutants, and in a fourth stage (A4) is conducted the drying, after which, in the second stage (B), there is conducted a sorting of the waste processed in the first stage (A), while there are released acrylonitrile butadiene styrene and polyvinyl chloride which are sent for landfilling, and polypropylene is released, as well as polyethylene separators with a silicon dioxide filler, and a residue is released representing other materials, and then the released polyethylene separators with a silicon dioxide filler are fed in the third stage (C) for processing via gasification, and this results in a gas phase and gives out amorphous silicon dioxide, which amorphous silicon dioxide is directed for its subsequent use, while the gas phase is fed to a fourth stage (D), which is a combustion process at a temperature not lower than 900°C in a thermal oxidizer, and after the combustion process (D), the hot gases from the thermal oxidizer are sent for utilization of the thermal energy in energy module (E).

2. A method according to claim 1 characterized in that the reduction of the size of the hazardous waste in the first stage (Al) of the pre-processing (A) is conducted to a size in the range of 5 to 20 mm.

3. A method according to claim 1 or 2 characterized in that the drying (A4) is conducted mechanically.

4. A method according to claim 1 or 2 characterized in that the drying (A4) is conducted thermally.

5. A method according to claims 1 to 4 characterized in that the neutralization (A2) is done at maintaining a hydrogen potential pH = (11 - 13).

6. A method according to claims 1 to 5 characterized in that the third stage (C) - the gasification - is conducted within a temperature range of 200°C to 850°C in controlled consecutive ranges of a temperature between 200°C and 350°C, followed by a second range of temperature between 350°C and 450°C, by a third range of temperature between 650°C and 700°C, and by a fourth range of temperature between 750°C and 850°C.

7. A method according to claims 1 to 6 characterized in that in transferring it for subsequent use, the amorphous silicon dioxide is subjected to further processing consisting of cooling (CI), grinding (C2) and packing (C4).

8. A method according to claims 1 to 7 characterized in that in the neutralization (A2), and from the chemical treatment (A3) is derived sludge that is subjected to precipitation, washing and compacting, and the compacted sludge is then collected for a follow-up recycling, while the waste waters are directed for treatment.

9. Installation for the implementation of the method for processing of hazardous waste characterized in that it includes a pre-processing unit (A), followed through a feeder hopper (19), from a sorting unit (B), which sorting unit (B) is connected via a buffer feeder hopper (27) with a unit for processing of polyethylene separators with a silicon dioxide filler (C), and behind which there is located a gas phase processing unit (D) connected with energy module (E), while the pre-processing unit (A) includes an incoming feeder hopper (1) followed by a conveyer (2) to a universal shredder (3) with gravity feeding to a conveyor with magnetic drum (4) that has an outlet for magnetic metals, for recycling, to container (5), and a second outlet towards a lead-containing waste separator (6), which also has two outlets - for lead with a lead container (7) and an outlet for the remaining waste connected via an elevator (8) with a dump feeder hopper (9), and the dump feeder hopper (9) has an outlet to at least one neutralization machine (10) with a switch valve (101) to at least one gravity chute (102) where each gravity chute (102) is connected to a chemical treatment machine (11), and each chemical treatment machine (11) is connected to a screw conveyer (12) with a respective dryer (13) that is connected through a pneumatic transport system (14) to the feeder hopper (19) feeding the waste sorting system from the sorting unit (B), and consisting of three sorting machines (20, 21, 22) each of which has two outlets, and namely - a first sorting machine (20) with a first outlet for polymers connected with the second sorting machine (22) and with a second outlet for all the rest of the waste, connected to a third sorting machine (21) where the second sorting machine (22) has an outlet for particles of acrylonitrile butadiene styrene and polyvinyl chloride, for landfilling, to container (23), and a second outlet for particles of polypropylene, for recycling, to container (26), and the third sorting machine (21) has an outlet for polyethylene separators with a silicon dioxide filler to a pneumatic transport system (25), and with a second outlet for other waste, for landfilling, to container (24) where the pneumatic transport system (25) is connected to a buffer feeder hopper (27), which is gravitationally connected to a second pneumatic transport system (28), and via it with a gasifier (29) the last three of which are located in the unit for processing of polyethylene separators with a silicon dioxide filler (C), and the gasifier (29) is completed with an air blower (30), and an exhaust gas blower (31) leading to a thermal oxidizer (36) from the gas phase processing unit (D), which includes an after-burner (37), mounted in the thermal oxidizer (36), and supplied with a second air blower (38) that controls the feeding of air, where the thermal oxidizer (36) is connected via a gas pipe to a boiler- utilizer (39) of the energy module (E), which boiler-utilizer (39) is completed with a water steam manifold (40) connected with the gasifier (29), as well as with a system for preparation of solutions (18) from the pre-processing unit (A), while the energy module (E) includes also a wet scrubber (41), an exhaust gas blower (42), as well as a chimney (43) and a deaerator (44), that feeds the boiler-utilizer (39) with water, where all facilities releasing processed water are connected to a station for water preparation and treatment (45), which is connected via a feeding pipeline with the system for preparation of solutions (18), as well as with the wet scrubber (41) and with the deaerator (44).

10. Installation according to claim 9 characterized in that the dryer (13) is mechanical.

11. Installation according to claim 9 characterized in that the dryer (13) is thermal.

12. Installation according to each of the claims 9 to 11 characterized in that the waste sorting system (20, 21, and 22) is gravitational.

13. Installation according to each of the claims 9 to 11 characterized in that the waste sorting system (20, 21, and 22) is optical.

14. Installation according to each of the claims 9 to 13 characterized in that the unit for processing of polyethylene separators C includes, besides the gasifier (29), also a cooler (32) of amorphous silicon dioxide, behind which is located a mill (33) connected to a packing system (35).

15. Installation according to claim 14 characterized in that behind the mill 33 is mounted a grinding size classifier 34.

16. Installation according to each of the claims 9 to 15 characterized in that each of the neutralization machines (10) and the chemical treatment machines (11) have outlets connected with precipitators (15), while they on their part are connected with sludge compactors (16) with outlets to containers (17) for the sludge, and the precipitators (15), and the sludge compactors (16) are connected to a station for water preparation and treatment (45).

Description:
METHOD AND INSTALLATION FOR PROCESSING OF HAZARDOUS WASTE

FROM RECYCLING LEAD-ACID BATTERIES

TECHNICAL FIELD

The Invention will find application in the processing of hazardous waste resulting from the recycling of lead-acid batteries through fragmentation of the batteries and separation of the fragments via hydro-mechanical sorting into particles of plastics from boxes, metals, including lead compounds, electrolyte and hazardous waste. The hazardous waste that is normally landfilled is subjected to processing in accordance with this Invention. The hazardous waste contains lead compounds, polymers, metals and other waste.

BACKGROUND ART

A closest known solution is described in Patent US 7,772,452 B2. The known method consists of initial washing of the waste to separate lead compounds and other foreign bodies. After that the heavy plastics from the washing solution are separated, and the lead is recovered, while the washing solution is regenerated via processing with alkaline metal or alkaline-earth-metal sulphides or via processing with metals, that are less precious than the lead used in a cementation reaction, that replace the lead in the solution with cations of these metals. A rinsing and drying of the waste is performed. Following that, the fine plastics are removed via an air jet, and there is also performed a separation of PVC and polyethylene with a silicon dioxide filler via fragmentation in a rotor apparatus . Pyrolysis of polyethylene with silicon dioxide filler is then performed for 10 to 60 minutes at a controlled temperature between 300°C and 600°C, and the gases and steam are directed to a catalytic cracking reactor with an operating temperature between 550°C and 750° C, to diminish the molecular weight of the pyrolysis gases. Zeolite is used as a catalyst. From the cracking reactor, the gases are directed towards the combustion chamber where they are burnt consecutively and produce the heating energy for the whole process. After that treatment, in the furnace remains hard fraction that in essence consists of silicon dioxide and residual carbon - in an amount between 3-5% of the total quantity. The carbon residue is oxidized in a separate process that is carried out at a controlled temperature between 400°C and 600°C in the presence of an inert gas and oxygen. There is also carried out a second pyrolysis of the mixture of PVC and fabrics in the presence of alkaline substances, and oxidation is performed of the residue from the pyrolysis of the PVC and fabrics with the production of an inert ash. Also known is an installation for conducting the method under US 7,772,452 B2 that includes a separating unit consisting of a device extracting the polyethylene with a silicon dioxide filler, PVC and fabrics via an air jet to a cyclone separator hopper and a conveyor belt for remaining heavy plastics. The installation includes also a rotation apparatus for the extraction of polyethylene with silicon dioxide filler, followed by a unit for its pyrolysis that includes a device for the performance of pyrolysis with a rotating drum heated on the outside with hot inflammable gases at maintaining of an inert atmosphere and slight overpressure. The installation also includes a catalytic cracking reactor.

The shortcomings of the known solution consist in the fact that the processes are carried out with the use of inert gases, alkaline metals or alkaline-earth sulphides and catalysts, and this makes the processing significantly more expensive. The processing of the main hazardous waste is done in different processes, which also makes it more expensive.

DISCLOSURE OF INVENTION

The problem the present Invention faces is there to be created a method for the processing of hazardous waste from the recycling of batteries, as well as of an installation for its implementation via which the hazardous waste to be processed into products for subsequent use or recycling, while for landfilling to be left waste at an amount below 5% of the total.

The problem has been resolved via a method of processing of hazardous waste containing lead compounds, plastics, metals, and mixed waste that includes a first stage of extraction of lead, subsequent chemical treatment for the cleaning of pollutants and for drying. According to the Invention, during the first stage there is performed a pre- treatment of the hazardous waste carried out in four phases, in which in the first phase is reduced the size of the hazardous waste, and besides the lead, there are also separated magnetic metals, and the lead and the magnetic metals are then led out through separate outlets for subsequent use. The remaining part of the hazardous waste, in a second phase, are subjected to neutralization with an alkaline solution, and after the neutralization, in a third phase, there is carried out the chemical treatment for the cleaning of pollutants. Drying is performed at a next fourth phase. After it, in a second stage of the method, is performed a sorting of the processed in the first stage waste, and the acrylonitrile butadiene styrene and polyvinyl chloride are separated and sent for landfilling, while polypropylene is separated for recycling. There are also extracted polyethylene separators with silicon dioxide filler for processing, and there are also separated other materials. The separated polyethylene separators with silicon dioxide filler are fed in a third stage for processing via gasification, during which there results a gas phase and amorphous silicon dioxide. The amorphous silicon dioxide is sent for subsequent use, while the gas phase is fed into the fourth stage that constitutes a combustion process at a temperature not lower that 900°C in a thermal oxidizer. After the combustion process, the hot gases from the thermal oxidizer are fed for thermal energy utilization in an energy module.

The reduction of the size of the hazardous waste in the first stage of the pre-processing is done to a size within the range of 5 to 20 mm.

The drying is conducted mechanically or thermally.

Neutralization is performed by maintaining a hydrogen potential pH = (11 - 13).

It is recommended the third stage of the method - the gasification - to be conducted within a temperature range from 200°C to 850°C in controllable consecutive ranges of temperature - between 200°C and 350°C, followed by a second range of temperature between 350°C and 450°C, by a third range of temperature between 650°C and 700°C, and by a fourth range of temperature between 750°C and 850°C.

When feeding it for subsequent utilization, the amorphous silicon dioxide is subjected to additional processing consisting of cooling, grinding and packing.

In carrying out the stage of pre-processing, according to the Invention, because of the neutralization and the chemical treatment, a sludge is obtained, which is subjected to precipitation, flushing and compacting, and the compacted sludge is collected for subsequent recycling, while the waste waters are directed for treatment.

In accordance with the Invention, there has also been created an installation for the implementation of the method of processing of hazardous waste which includes a unit for pre-processing that is followed by a sorting unit via a feeder hopper. The sorting unit is connected through a feeder hopper with a unit for processing of polyethylene separators with a silicon dioxide filler behind which is located a unit for a gas phase processing connected to an energy module. The pre-processing unit includes an incoming feeder hopper followed by a conveyor to a universal shredder with a gravity feed to a conveyor with magnetic drum, with an outlet for magnetic metals, for recycling, to a container, and with a second outlet to a lead-containing waste separator. The lead-containing waste separator also has two outlets - for lead with a lead container, and an outlet for the remaining waste connected through an elevator with dump feeder hopper. The feeder hopper has an outlet to at least one neutralization machine with switch valve, and with at least one gravity chute. Each gravity chute is connected to a machine for chemical treatment. Each machine for chemical treatment is connected through a screw conveyor to a respective dryer that is connected via a pneumatic transport system to the feeder hopper that feeds a waste sorting system from the sorting unit. The waste sorting system consists of three sorting machines, each of which has two outlets. The first sorting machine has a first outlet for polymers (polypropylene P acrylonitrile butadiene styrene ABS, polyvinyl chloride PVC), connected with a second sorting machine; and a second outlet for all the rest of the waste, connected to a third sorting machine. The second sorting machine has an outlet for particles of acrylonitrile butadiene styrene and polyvinyl chloride, for landfilling, to container, and a second outlet for particles of polypropylene, for recycling, to container. The third sorting machine has an outlet for polyethylene separators with silicon dioxide filler to a pneumatic transport system, and with a second outlet for other waste (the remaining waste from the sorting process), for landfilling, to container for the waste. The pneumatic transport system is connected with the feeder hopper, which is connected gravitationally to a second pneumatic transport system, and through it to a gasifier, the last three of which are located in the unit for processing of polyethylene separators with silicon dioxide filler. The gasifier is completed with an air blower and an exhaust gas blower leading to a thermal oxidizer in the gas phase processing unit. The gas phase processing unit includes an after-burner mounted in the thermal oxidizer, equipped with a second air blower. The thermal oxidizer is connected via an exhaust gas duct to a boiler-utilizer of the energy module, which boiler-utilizer is completed with a water steam manifold connected to the gasifier, as well as to a system for preparation of solutions in the pre-processing unit. The energy module includes also a wet scrubber for exhaust gases, an exhaust gas blower, as well as a chimney, and a deaerator which feeds water to the boiler-utilizer. All processed water separating facilities are connected to a station for water preparation and treatment which is connected by a feeding pipeline to the system for preparation of solutions, as well as to the wet scrubber and to the deaerator. According to one of the versions of the Invention, the dryer is mechanical.

According to another version of the Invention, the dryer is thermal.

Optionally, the waste sorting system is gravitational or optical.

The installation, according to the Invention, connects the polyethylene separators processing unit to both the gasifier, and to a cooler for the amorphous silicon dioxide, behind which is located a mill connected to a packing system.

It is appropriate behind the mill there to be mounted a grinding size classifier. It is foreseen that all the neutralization machines and the chemical treatment machines to have outlets connected to precipitators, and they on their part to be connected to sludge compactors with outlets to containers for the sludge. At that, the precipitators and the sludge compactors are connected to the station for water preparation and treatment.

The advantages of the Invention lie in the simplified technological scheme in using energy effective technological processes, and there is created an opportunity for separating the waste that is to be subjected to recycling or subsequent use - lead and magnetic metals, polypropylene (PP), as well as amorphous silicon dioxide, which is a commercial product ready for incorporation in other industrial productions. There has been used a specific equipment for neutralization and chemical treatment with functionality relevant to the implemented processes. The amount of waste subject to landfilling is less than 5% of the total amount of the processed hazardous waste.

BRIEF DESCRIPTION OF DRAWINGS

Fig. 1 - A block diagram of the method implementing installation according to the Invention

Fig. 2 - This is a flow diagram of the method implementing installation according to the Invention.

MODE FOR CARRYING OUT THE INVENTION

The Hazardous Waste Processing Method by the recycling of lead-acid batteries that contain lead compounds, plastics, metals, and mixed waste includes an extraction of lead, a follow-up chemical treatment to clean up pollutants, and drying. According to the Invention, there have been provisioned several stages of processing, as in the first stage A in which a pre-processing of the hazardous waste is carried out. At the end of this stage, from the fed at its entrance hazardous waste that is of un-homogeneous content, polluted, and with different sizes, usually within the ranges from 5 ÷ 250 mm, the hazardous waste is cleaned to the highest possible degree, and it is brought to 5 ÷ 20mm. The magnetic metals and lead are separated from the total stream. Thus, the preliminary processing stage A includes stage Al of reduction of the size of hazardous waste (via cutting and fragmenting), followed by the extracting from them the lead and the magnetic metals by directing them via separate outlets for subsequent use. The reduction of the size can be carried out with the use of a universal shredder which cuts the soft waste and fragments the hard ones. During a second stage A2 of the pre-processing the portion of hazardous waste that has remained after the separation of the metals from the hazardous waste is subjected to a two-phase neutralization, and in the first phase is performed neutralization with an alkaline solution by maintaining a hydrogen potential pH = (11 to 13) and a temperature within the 75°C to 85°C range. In the second phase is performed a rinsing of the waste with hot demineralized water. The temperature in this phase is maintained within the 75°C to 85°C range. The second phase of neutralization usually takes some 5 to 10 minutes.

After the neutralization, there is carried out a third stage A3 of pre-processing consisting of chemical treatment to remove the pollutants.

The chemical treatment is intended to reduce to the greatest possible degree the precipitated pollutants (primarily lead compounds), and it is conducted in three phases that are usually carried out in one and the same machine. The first phase of chemical treatment consists of the processing of the neutralized waste in a 3% solution of ethylene diamine tetra acetate known under the commercial name of EDTA, at a temperature of 75°C to 85°C and in maintaining a hydrogen potential pH = (11-13). The process is with continues 50 to 70 minutes.

The second phase of the chemical treatment consists of rinsing with hot water at a temperature from 75°C to 85°C for 5-20 minutes.

The third phase of chemical treatment is rinsing with demineralized water supplemented with acetic acid to a pH = 5 for around 15-20 minutes with a subsequent rinsing with demineralized water until the conductivity of the waste water reaches < 100 μ5/οηι.

The three phases of chemical treatment result in waste water that is directed to a station for the preparation and treatment of water.

In the following fourth stage A4 the waste that underwent chemical treatment is subjected to drying.

The A4 drying after the chemical treatment is intended to reduce the humidity of the waste to the appropriate such for the conducting of stage two B. Normally, the drying can be done in a mechanical way, for example, as in using a centrifugal process. It is also possible to use a thermal process.

The second stage B of the method, according to the Invention, consists in sorting of waste by types that allow for a consequent recycling. In this second stage B, the processed in the first A stage waste, are sorting and at the outlet from the sorting there are released acrylonitrile butadiene styrene (ABS) and polyvinyl chloride (PVC), and it is directed for landfilling as chemically neutralized and washed waste. Polypropylene (PP) is also released for recycling. In the sorting there are also released polyethylene separators with silicon dioxide filler, which are processed in a following stage of the method. There also remain other materials such as labels, microfiber glass separators (AGM), and others. The remaining materials are usually led out for landfilling or subjected to additional processing . The sorting can be done with standard production equipment - gravitational or optical. The polyethylene separators with a silicon dioxide filler are fed to a third stage C for processing in which gasification is applied in a temperature range of 200°C to 850°C by feeding air and water steam at an over pressure of the gasifier close to the atmospheric one, for example, in a range of up to 20 milibars. During the gasification the polyethylene separators with silicon dioxide filler are degraded to a gas phase and to synthetic amorphous silicon dioxide. The obtained amorphous silicon dioxide is directed for subsequent use.

The amorphous silicon dioxide is subjected to additional processing in order to obtain a commercial appearance by being cooled CI, milled to an appropriate size C2, and packaged C4. After that it is provided for commercial sales for industrial use. Respectively, it is also appropriate to make a classification C3 of the ground silicon dioxide.

The gasification leads to a gas phase, which is processed in stage D via thermal oxidation. This is done in a thermal oxidizer completed with an After-burner via which there is implemented a combustion process at a temperature not lower than 900°C, best between 900°C and 1600°C. At this point to the thermal oxidizer is fed a controlled quantity of air and oxygen. The gas phase is oxidized to hydrogen dioxide and water steam. The obtained hot gases are lead out to an energy module E and more precisely - to an inserted in it boiler-utilizer, which produces the water steam and hot water necessary for the described in the method technological processes.

The additional processing of the remaining part of the sorting (other waste) can be carried out together with the gas phase of the gasification in the thermal oxidizer.

The Invention concerns also an installation for the conducting of the hazardous waste processing method which includes:

A pre-processing unit A that is followed, via a feeder hopper 19, by a sorting unit B, which sorting unit B is connected via a buffer feeder hopper 27 with processing of polyethylene separators unit C, after which is located the unit D for gas phase processing, connected with energy module E. At that, the pre-processing unit A consists of an incoming feeder hopper 1, equipped with vibrating feeder located at the bottom of the hopper. The incoming feeder hopper 1 is followed by a conveyor 2 leading to a universal shredder 3 with a gravity feed to a conveyor with magnetic drum 4, which has an outlet for magnetic metals, for recycling, to container 5, and a second outlet to a lead-containing waste separator 6. The lead-containing waste separator 6 has two outlets - for lead with a lead container 7, and an outlet for the remaining waste connected via elevator 8 with dump feeder hopper 9. The dump feeder hopper 9 has an outlet to at least one neutralization machine 10 with a switch valve 101, and with at least one gravity chute 102. Every gravity chute 102 is connected to a chemical treatment machine 11. It is a good idea each neutralization machine 10 to feed two chemical treatment machines 11 as this provides an opportunity for better synchronization of the duration of the neutralization and chemical treatment processes. The specific number of machines is selected depending on the amount of hazardous to be processed. In the shown example (fig.2), two chemical treatment machines 11 are connected to the neutralization machine 10.

The neutralization machines 10, and the chemical treatment machines 11 also have outlets connected to precipitators 15, and they on their part are connected to sludge compactors 16 with outlets to containers 17 used for follow-up recycling of the lead compounds contained in the sludge. There is also provisioned a station for water preparation and treatment 45, to which precipitators 15 and sludge compactors 16 are connected.

Each chemical treatment machine 11 is connected via a screw conveyer 12 to the respective dryer 13. It is appropriate for the dryer 13 to be mechanical, for example, centrifuges. It is possible to use also thermal dryer.

Each dryer 13 is connected via a pneumatic transport system 14 to the feeder hopper 19 which feeds a waste sorting system for the sorting unit B.

Sorting unit B includes a waste sorting system consisting of three sorting machines 20, 21, 22 that can be gravitational or optical. Standard manufacturing equipment is appropriate to use.

Each one of the three sorting machines divides the waste into two streams - one for the basic waste, and one for the remaining waste.

The first sorting machine 20 with a first outlet for polymers (ABS, PP and PVC), connected to a second sorting machine 22, and to a second outlet for all the remaining waste, and connected to a third sorting machine 21.

The second sorting machine 22 has an outlet for fragments of acrylonitrile butadiene styrene (ABS) and polyvinyl chloride (PVC) for landfilling to container 23, and a second outlet for fragments of polypropylene (PP), for recycling, to container 26.

The third sorting machine 21 has an outlet for polyethylene (PE) separators to the pneumatic transport system 25 and a second outlet for other waste (the remaining part from the sorting process) for landfilling to container 24.

The pneumatic transport system 25 is connected to the buffer feeder hopper 27, which is connected gravitationally to a second pneumatic transport system 28, and through it to a gasifier 29. The last three - the buffer feeder hopper 27, the second pneumatic transport system 28 and the gasifier 29 - are located in the unit for processing of polyethylene separators C.

The gasifier 29 is completed with an air blower 30, and an exhaust gas blower 31 for the gases from the gasification process that leads to a thermal oxidizer 36 from the gas phase processing unit D that includes an after-burner 37 mounted in the thermal oxidizer 36, and controlling the feeding of air through a second air blower 38.

Besides a gasifier 29, the polyethylene separators processing unit C in the shown example also includes a cooler 32 for the amorphous silicon dioxide, behind which is located a mill 33, and, as a variant, a grinding size classifier 34 of the amorphous silicon dioxide connected with the packing system 35.

The thermal oxidizer 36 is connected, via an exhaust gas duct, to a boiler-utilizer 39 of the energy module E. Besides the boiler-utilizer 39, the energy module E also includes a wet scrubber 41 for the cleansing of the exhaust gases, an exhaust gas blower 42, as well as a chimney 43, and a deaerator 44. The boiler-utilizer 39 is completed with a water steam manifold 40, connected to the gasifier 29, as well as to a system for preparation of solutions 18 from the pre-processing unit A.

The water required for the technological processes is supplied by a station for water preparation and treatment 45 to which all the installation facilities are connected and from which waste water is taken off.

The method in accordance with the Invention is implemented via the installation for its implementation in the following way:

The first stage of pre-processing starts with the discharge of the hazardous waste that contains lead compounds, plastics, metals, and mixed waste in the incoming feeder hopper 1, and it ends with a mechanical drying of the waste in dryers 13. This first stage includes four phases where in the first of them Al, the hazardous waste is mechanically reloaded from the big-bag in the incoming feeder hopper 1. Through the vibrating feeder - located at bottom of the feeder hopper, the waste falls on conveyer 2 that can be a belt one or of another appropriate type, and which conveys them into the equipment for implementation of the hazardous waste size reducing process. The process can be conducted via a universal shredder 3 that cuts the soft and breaks down the hard waste. From the universal shredder 3 the hazardous waste is fed onto the magnetic drum conveyer 4, in the shown example - through the gravity chute. The separation of the magnetic metals from the common stream of hazardous waste is conducted with the help of the magnetic drum conveyer 4. The magnetic metals are collected in container 5 for the next recycling, while the remaining part of the hazardous waste is usually fed through a vibrating feeder to the lead-containing waste separator 6. The extracted lead is collected in lead container 7 for a follow-up recycling, and the remaining part of the waste falls on elevator 8, which transfers it in dump feeder hopper 9. On the bottom of dump feeder hopper 9 there is a valve controlled by an automated control system, and it opens periodically to unload the waste through the gravity chute in neutralization machine 10.

The neutralization process - phase A2 of the pre-processing - is intended to eliminate the acidic electrolyte having dried on the surface and in the pores of the waste, and it is carried out in two consecutive phases in one and the same neutralization machine 10. The neutralization machine 10 is fed with the necessary solutions from the system for preparation of solutions 18 that consists of mixers, pumps, heat exchangers for heating of the respective armature, pipe lines and measuring equipment and it is managed by the automated management system. The feeding with demineralized water is done by the station for preparation and treatment of water 45.

The first phase of the process of neutralization, and namely - the washing with an alkaline solution is performed by maintaining a hydrogen potential pH = (11 to 13) and a temperature within the 75°C to 85°C range. This phase is run for 20 to 40 minutes.

After the completion of this phase, the neutralization machine 10 is automatically drained through a drain valve, and the sludge is flushed and compacted in the respective precipitator 15 and sludge compactor 16. The compacted sludge is collected in the container 17 for a follow-up recycling. The waste waters from precipitator 15 and sludge compactor 16 are transferred to the station for preparation and treatment of water 45. The waste that is in neutralization machine 10 remains in it. Next follows the filling of neutralization machine 10 with hot demineralized water for the running of the second phase - rinsing of the waste for 5 to 10 minutes at a temperature from 75°C to 85°C. The filling is done automatically. 11

After the completion of phase two that is controlled by the automated management system, the neutralization machine 10 is once again drained through a drain valve in the system consisting of a precipitator 15 and a compactor 16 for precipitation, flushing of the sludge, and compacting sludge without being emptied of the waste in the neutralization machine 10. After the draining, the neutralization machine 10 automatically discharges itself by opening its switch valve 101, and through the gravity chute 102 it feeds the waste to one of the chemical treatment machines 11 beneath it.

The synchronized work of all machines is conducted by the common automated management system.

The stage A3 of the pre-processing is done in chemical treatment machines 11 in a three- phase process.

In order to conduct each of the three phases of chemical treatment, the filling of the chemical treatment machines 11 is done automatically by the system for preparation of solutions 18, by, respectively, after completing the phases there is also done an automatic draining through a drain valve and sending the sludge to precipitator 15 and sludge compactor 16, and from there to container 17 for it to be sent for the recycling of the lead compounds contained in the sludge. Simultaneously, the waste water of all phases is led to the station for preparation and treatment of water 45.

After the chemical treatment, the waste in the chemical treatment machine 11 is fed via the screw conveyer 12 to dryer 13, and is subjected to drying.

From the dryer 13, via the pneumatic transport system 14, the dried waste is fed to the feeder hopper 19, where there starts the second stage B of the processing method, and namely - sorting of the waste by types that allows for its next recycling.

In this second stage B is done sorting of the waste processed in the first stage A with the consecutive use of the three sorting machines 20, 21 and 23.

This is done by feeding the waste via the vibrating feeder of the feeder hopper 19 through a gravity chute to the first sorting machine 20 that is located beneath it. It separates the waste in two streams: first stream - polymers (polypropylene PR acrylonitrile butadiene styrene ABS, and polyvinyl chloride PVC), and a second stream - polyethylene separators (PE) with silicon dioxide filler, and other waste. The first stream of this first sorting machine (polymers - PP, ABS, and PVC) is fed through the respective outlet via a conveyer belt to the second sorting machine 22. The second stream from polyethylene separators and other waste is also fed via a conveyer belt to the third sorting machine 21. The second sorting machine 22 divides the fed into it waste in two streams: the first stream - acrylonitrile butadiene styrene ABS, polyvinyl chloride PVC, which are both collected in container 23 and are sent to the waste depot, and the second stream - polypropylene PR that is collected in container 26 and sent for recycling.

The third sorting machine 21 separates the waste fed into it from the first waste sorting machine 20 in two streams: the first stream - other waste (microfiber glass separators - AGM, paper, and etc.), that are collected in container 24, and sent to a waste depot, and a second stream - polyethylene (PE) separators with silicon dioxide filler that are fed through the second outlet to the pneumatic transport system 25 and via it - to the buffer feeder hopper 27.

From there, through the gravity chute, the polyethylene separators with silicon dioxide filler are fed through a second pneumatic transport system 28 in the gasifier 29 for the third stage of processing C.

The processing of the polyethylene separators with silicon dioxide filler is done in the process of gasification in the temperature range of 200°C to 850°C, and an over pressure close to the atmospheric one, for example around 20 milibars. It is a good idea the heating to be conducted in four controllable temperature zones: first zone - with temperature between 200°C and 350°C; second zone: temperature between 350°C and 450°C; third zone: temperature between 650°C and 700°C; fourth zone: temperature between 750°C and 850°C.

The additional processing to give a commercial appearance of the amorphous silicon dioxide that is obtained after the gasification is done in a series of facilities as follows : in the beginning, the amorphous silicon dioxide is cooled down in the cooler 32, after that it is ground in mill 33. Classification is performed of the grinding size via a classifier 34, and the processed silicon dioxide is fed into the system for its packing 35. The packaged silicon dioxide is sent to the market for commercial sales for industrial application . It is possible the packing to be done directly after the grinding, and this does not limit the scope of the Invention, depending on the marketing of the resulting commercial product. The gasses released in the process of gasification of the polyethylene separators are fed via the blower 31 to the thermal oxidizer 36 with the after-burner 37. From the thermal oxidizer 36, via the exhaust gas duct, the released in the oxidation gases are sent to the boiler-utilizer 39 of energy module E. Respectively, a cleansing of the exhaust gases is carried out in energy module E with the wet scrubber 41, and they are expelled via the exhaust gas blower 42, and chimney 43. The deaerator 44 feeds the boiler-utilizer 39 with the needed water. Via the water steam manifold 40 of the boiler-utilizer 39 there is fed the necessary steam for the gasifier 29, as well as to the system for preparation of solutions 18 of the pre-processing unit A.