WO2008030137A1

WO2008030137A1 - Method and device for processing rubber waste

Info

Publication number: WO2008030137A1
Application number: PCT/RU2007/000392
Authority: WO
Inventors: Gennady Ivanovich Zhuravsky; Vitaly Aleksandrovich Zhdanok; Yury Igorevich Uchanin; Oleg Valentinovich Likharev
Original assignee: Konstanta, Obschestvo S Ogranichennoy Otvetstvennostyu
Priority date: 2007-01-10
Filing date: 2007-07-19
Publication date: 2008-03-13
Also published as: RU2008137470A; RU2394680C2

Abstract

The invention relates to waste processing and can be used in the chemical and industrial rubber industry, for obtaining ingredients of a rubber mixture from waste of petrochemical raw material, and in power engineering for producing fuels and the components thereof. The inventive method consists in supplying rubber waste to a reactor by means of a movable container, in carrying out thermolysis in a medium containing water vapour of heat carrier which is passed through a waste layer in such a way gaseous and solid phases are formed. The gaseous phase is separated from the reactor and is partially returned to water vapour mixtures at a mass ratio between water vapour and the gaseous phase of 1: (1.0-0.5).The solid phase is removed from the reactor, is ground to a particle size ranging from 1.0 to 3.0 mm and is exposed to magnetic treatment. The gaseous phase is cooled and a liquid phase, condensed during the cooling thereof, is separated. The thus processed solid and liquid phases are mixed in such a way that a fuel dispersion is obtained. The mixing is carried out in a mixer at a mass ratio of (0.75-1.50):1 and the mixture is circulated with the aid of a dispergator pump for 600-3600 sec. Said invention makes it possible to restore the environment health, to obtain high quality useful products, in particular fuel dispersions, to reduce energy consumption for rubber waste processing and to decrease discharge into the environment.

Description

METHOD AND DEVICE FOR PROCESSING RUBBER WASTES

Technical field

The invention relates to waste treatment technology and can be used in the chemical and rubber industry, for the production of petrochemical raw materials from waste, rubber compound ingredients, and can also be used in the energy sector to produce fuels and their components.

State of the art

A known method of treating waste polymer compositions, including their thermolysis in a reactor at 400-1500 ° C in a vapor-gas mixture stream containing superheated water vapor, nitrogen and carbon oxides, with the formation of a solid carbon residue and the release of gaseous products, subsequent grinding of the carbon residue in a gaseous stream products at 350–400 ° C and its magnetic treatment, thermolysis of gas-vapor products at 1400-1500 ° C (SU 747868, C09C 1/48, 1980).

The disadvantages of this method include:

1. A large specific energy consumption, which is due to the high thermolysis temperature (up to 1500 ° C), as well as large thermal losses to the environment at this temperature. 2. Large amounts of harmful substances formed during the thermal decomposition of gas-vapor products, and the need to use complex systems for cleaning gaseous products from these substances.

3. The need to use heat-resistant and corrosion-resistant materials for the manufacture of equipment, which significantly increases the cost of the target products obtained by this method.

A known method of processing rubber waste, including their thermolysis in a reactor in a water vapor environment, separation of the solid phase and its grinding, separation of the liquid and gaseous phases by condensation, combustion of the gaseous phase to heat the reactor (US 5720232, 110/346, 1998). According to the specified method, the waste is fed from the loading system into the hopper and sent via a screw conveyor to the thermolysis chamber, where it is moved using the screw and heated to a temperature of 359-650 ° F (181.7-343.3 ⁰ C). The thermolysis chamber includes a steam system to remove steam and create a vacuum. The gaseous phase is passed through a heat exchanger and fed to a separator in which it

1 SUBSTITUTE SHEET (RULE 26) partially condensed, and not a condensing gas is used as fuel. The solid residue of tire thermolysis using a closed conveyor is fed into a closed hopper, which is used as a lock gate to prevent air from entering the reactor. The disadvantages of this method are:

1. A large specific energy consumption, due to the need to create and maintain a vacuum in the thermolysis chamber.

2. Low efficiency of heat transfer processes in the thermolysis chamber due to the presence of vacuum, which leads to an increase in thermolysis time and increased energy consumption.

3. A high degree of explosive ™ due to the presence of vacuum in the thermolysis chamber and the possibility of air entering the chamber from the environment, which ultimately can lead to an explosion and release of harmful substances into the environment.

4. Significant emissions of harmful substances into the environment during operation.

A known method of processing rubber waste, including their thermolysis in a reactor in a coolant, separation of the solid phase, separation of the liquid and gaseous phases by condensation, use as a coolant superheated to 300-1600 ⁰ C water vapor (98-85 wt.%) And gaseous phase (2-15 wt.%), mixing solid and liquid phases in a mass ratio (0.03-0.40): 1 followed by briquetting the resulting mixture while heating it to 100-500 ° C by filtering the gas obtained after separating the liquid phase from the gaseous products waste decomposition (RU 2076501, B29B 17/00, C08J 11/10, C08J 11/14, 1997). Rubber waste before thermolysis is mixed with 3-40 mass. % of the liquid phase by passing gaseous decomposition products through the waste layer at their mass ratio (0.05-1.62): 1.

The disadvantages of this method include:

1. Large specific consumption of water vapor, high process temperature (up to 1600 ° C) and, as a result, high energy consumption for waste treatment.

2. Large emissions of fuel combustion products consumed in the production of large quantities of water vapor and overheating it to a high temperature.

3. The low quality of the resulting fuel briquettes due to the availability

2 SUBSTITUTE SHEET (RULE 26) unsaturated compounds in the liquid phase, which is used for the preparation of briquettes.

Closest to the claimed is a method of treating rubber waste, including feeding the waste into the reactor, thermolysis in the reactor in a medium containing water vapor coolant, passed through the waste layer, with the formation of gaseous and solid phases, the withdrawal of the solid phase from the reactor, its grinding and magnetic treatment , cooling the gaseous phase, separating the liquid phase condensed by cooling the gaseous phase, burning the non-condensed gaseous phase to heat the heat carrier in the heat exchanger, mixing idkoy and solid phases in a mixer (US 5,780,518, 521/45, 1998). According to this method, superheated water vapor in the amount of 18-110% of the waste mass is used as a heat carrier, the solid phase after separation is crushed to particle sizes of 0.001-0.210 mm, and the liquid phase is mixed with 23.0-55.8 mass. % of the crushed solid phase to obtain a fuel dispersion.

The disadvantages of this method are:

1. High energy costs for processing, which is due to the large (up to 110% of the waste mass) water vapor consumption and the need for a long mixing time of the liquid and solid phases to obtain a homogeneous mixture. 2. Large emissions of harmful substances into the environment during the combustion of the gaseous phase.

3. The low quality of the resulting fuel dispersion due to the presence of a large amount of water in it - low heat of combustion, high freezing point, large amounts of water vapor generated during its combustion, which leads to the need to throw combustion products into the environment at a higher than for conventional fuels, temperature to prevent condensation of water vapor directly in the chimney.

A device for thermolysis of rubber waste (not shredded tires) is known, comprising a reactor in the form of an annular chamber with a gas duct for discharging a gas mixture, a hatch for loading and unloading, a heater made in the form of several shells equipped with spiral plates for turbulence of heating gas, with supply pipes and removal of heating gas, as well as a gas generator that runs on carbon black, and the heater shells are installed outside and inside the integral ring chamber

3 SUBSTITUTE SHEET (RULE 26) thermolysis, made with the possibility of its rotation around the horizontal axis using a support device with a winch (RU 2258078, B29B 17/00, ClOB 53/08, 2005).

The disadvantages of this device include: 1. High specific energy consumption for the processing process, due to the frequency of operation of the device and the long duration of thermolysis of worn-out tires due to low-efficient heat transfer between the heating gas and the unshredded tires having a small specific heat-transfer surface. 2. Large emissions of harmful substances into the environment caused by the use of fuel combustion products obtained by gasification of carbon black as heating gas.

3. High explosiveness due to the presence in the thermolysis chamber of flammable products of tire thermolysis and high temperature in the chamber, which can lead to the release of toxic products into the environment.

A device for treating rubber waste (not shredded tires) is known, including a vertical reactor with a heater, a lock chamber for loading tires on the side of the reactor and a lock chamber for unloading in the lower part of the reactor, a condenser for condensing part of the thermolysis products connected to the input of the vapor-gas phase from the reactor , and a storage tank-settler of the liquid phase with a tap and a flow meter (RU 2251483, B29B 17/00, 2005). The lock chambers of loading and unloading are made with water gates with the possibility of sealing the reactor. The airlock loading chamber is equipped with a loading conveyor, which is equipped with pressure rollers at the inlet and outlet of the water lock. The reactor is additionally equipped with a catalytic cracking cartridge and equipped with a burner furnace. The furnace body is made conical in the form of a guide for stringing tires onto the top of the cone from the loading conveyor. An annular infrared emitter made of heat-resistant steel is mounted at the base of the furnace cone. The disadvantages of this device are:

1. High specific energy consumption for the processing process, which is caused by the moistening of the tires as they pass through the water lock and the subsequent energy consumption for the evaporation of water introduced with the tires into the reactor.

2. The low quality of the obtained carbon residue thermolysis of tires due to

4 SUBSTITUTE SHEET (RULE 26) the deposition of a part of the liquid thermolysis products on the particles of the carbon residue during the discharge of the residue through a water seal, on the surface of which the gaseous thermolysis products inevitably condense, forming an oil film. 3. High explosiveness due to the low degree of reliability of the water gates due to the instability of such gates with a sharp increase in pressure in the reactor.

A device for treating rubber waste (not shredded tires) is known, including a thermolysis reactor in the form of a sealed chamber with gas ducts for supplying and discharging a gas mixture, a gas heater connected to an outlet to a gas duct for supplying a gas mixture to a reactor, a condenser for condensing part of the thermolysis products, connected inlet to the outlet of the reactor, a compressor for circulating the gas mixture, connected to the inlet of the condenser and the outlet to the inlet of the heater, a separator with a tank for collecting liquid resulting from the term olysis (RU 2212430, ClOG 1/10, C08J 11/00, C08J 11/04, 2003).

The disadvantages of this device include:

1. High specific energy consumption for the processing process, due to the presence of fans, compressor, valves, which require a large amount of electrical energy.

2. High emissions of harmful substances into the environment caused by the release of gas into the atmosphere.

3. The low quality of the obtained processing products due to the difficulty of regulating the process of gas extraction from the thermolysis chamber and the inefficient isolation of the processed products in the separator.

Closest to the proposed device is a device for the treatment of crushed rubber waste, including a thermolysis reactor in the form of a chamber with flues for supplying and outputting a gas mixture, a steam generator, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the gas mixture inside reactor, connected in series to the gas duct for withdrawing the gas mixture from the reactor, a condenser and a separator, a loading chamber and a cooling and unloading chamber, p located on two opposite sides of the reactor and connected with gate locks, the container in the loading chamber on

5 SUBSTITUTE SHEET (RULE 26) a trolley with the possibility of moving it into the reactor and from the reactor to the cooling and unloading chamber (RU 2247025, B29B 17/00, C08J 1 1/10, 2005). The device also contains a disperse filling of refractory material, forming a gas duct from the furnace into the chimney. The heat exchanger is made in the form of two sections connected in series, and the output of the last section is connected to the furnace, and dispersed filling is placed between the furnace chamber and the reactor. The disadvantages of this device are:

1. High specific energy consumption for the processing of rubber waste, due to the low efficiency of heat transfer in the reactor to the waste, heat loss with fuel combustion products emitted into the chimney, and the need to maintain dispersed filling at high temperature.

2. Large emissions of harmful combustion products into the environment, as a result of the burning of non-condensable thermolysis gases and fuel in the furnace under the reactor.

3. The low quality of the resulting rubber waste treatment products caused by the uneven heating of the waste in the reactor, the heating time due to low heat transfer efficiency, and the uneven heating of the reactor itself, in which the lower part above the furnace is overheated and the upper part has a lower temperature .

Disclosure of invention

The objective of the invention is to reduce energy costs in the processing of worn tires, improving the quality of products obtained during processing, and reducing harmful emissions into the environment. To solve this problem, a method for treating rubber waste is proposed, which includes feeding waste into the reactor in a mobile container from the first loading / unloading chamber, thermolysis of it in the reactor in the medium containing coolant water vapor passing through the waste layer, with the formation of gaseous and solid phases, the output of gaseous phase from the reactor, the return of part of the gaseous phase to the reactor, the removal of the solid phase from the reactor by moving the container with the solid phase from the reactor at the end of the thermolysis process in the reactor in the first th loading / unloading chamber, unloading of the solid phase upon rotation of the container relative to the longitudinal axis, grinding of the solid phase and its magnetic treatment, cooling of the gaseous phase, separation of the liquid phase,

6 SUBSTITUTE SHEET (RULE 26) condensed during cooling of the gaseous phase, burning the non-condensed gaseous phase to heat water vapor in the heat exchanger, then repeating the process in which waste is fed to the reactor in a mobile container from the second loading / unloading chamber, and the container is transferred from the reactor at the end of the thermolysis process in the reactor into the second loading / unloading chamber.

As a result of the process, as in the known methods, a solid phase (carbon residue) and a liquid phase (a mixture of organic liquid products and water) are obtained, which can be used as fuels or raw materials to produce any products (liquid phase) - after water separation), as well as metal waste separated as a result of magnetic treatment.

In this variant of the proposed method, the return to the reactor of the part of the gaseous phase exiting the reactor, and the use of the gas-vapor mixture as a heat carrier, thereby reducing the heat carrier consumption, since the gas-vapor mixture has a higher (1.5-2 times) specific heat in comparison with pure water vapor, as a result of which 1 kg of such a mixture, ceteris paribus (the same temperature and pressure) can carry 1.5-2 times more heat than pure water vapor. In addition, when the gaseous products of thermolysis of tires that are contained in the coolant are heated in a heat exchanger to a temperature of 500-700 ° C, they are further thermally decomposed to form products of lower molecular weight, and thus the quality of the liquid phase is improved (the content of unsaturated compounds decreases and specific heat of combustion increases). By passing the vapor-gas mixture through the waste layer, the uniformity of their heating also increases (local overheating is prevented), and this improves the quality of solid decomposition products, since they exclude the presence of insufficiently processed solid products containing some residual amount of undecomposed rubber waste. It is preferable to carry out thermolysis at a mass ratio of water vapor and gaseous phase in a mixture equal to 1: (1, 0-5.0). A decrease in the content of gaseous decomposition products in a gas-vapor mixture to a ratio of less than 1: 1 leads to a sharp decrease in specific heat to a value equal to the specific heat of pure water vapor, as well as to an increase

7 SUBSTITUTE SHEET (RULE 26) water vapor consumption. With a higher content of gaseous decomposition products in a gas-vapor mixture than at a ratio of 1: 5, the density of such a mixture sharply increases (the molecular weight of the decomposition products of tires is more than 200 kg / kmol, and water vapor is 18 kg / kmol), and some of the products can be deposited on the walls of the heat exchanger with the formation of a solid bitumen-like layer, which as a result will reduce the yield of decomposition products of tires and the failure of the heat exchanger itself.

As another option for solving the problem, a method for treating rubber waste with obtaining a fuel dispersion is proposed, which includes feeding the waste into the reactor in a mobile container from the first loading / unloading chamber, thermolizing it in the reactor in the medium containing water vapor passing through the waste layer to form gaseous and solid phases, the withdrawal of the gaseous phase from the reactor, the return of part of the gaseous phase to the reactor, the withdrawal of the solid phase from the reactor by moving the container with the solid phase from p actor at the end of the thermolysis process in the reactor into the first loading / unloading chamber, unloading the solid phase when the container is rotated relative to the longitudinal axis, grinding the solid phase to particle sizes of 1.0-3.0 mm, its magnetic treatment and further grinding, cooling the gaseous phase, separating the liquid phase condensed by cooling the gaseous phase, separating part of the water from the liquid phase, mixing the liquid and solid phases in the mixer at a mass ratio (0.75-1.50): 1, circulating the mixture through the mixer using a dispersion pump atom for 600-3600 s, burning the non-condensed gaseous phase to heat water vapor in the heat exchanger, then repeating the process in which waste is fed into the reactor in a mobile container from the second loading / unloading chamber, and the container is moved to the reactor after thermolysis from the reactor to the second loading / unloading chamber.

In this embodiment of the method, as in the previous one, due to the return to the reactor of the part of the gaseous phase exiting the reactor, a reduction in energy costs and an improvement in the quality of the products obtained are achieved. Preliminary separation of part of the water from the liquid phase, its subsequent mixing with the solid phase at the specified ratio and circulation of the mixture through the mixer using a dispersing pump allows you to get high-quality fuel dispersion. Use of water for

8 SUBSTITUTE SHEET (RULE 26) receiving fuel reduces the load on the cleaning system and leads to an increase in the amount of fuel received, and the water separated from the liquid phase is most naturally returned to the process to produce steam used in the thermolysis process; All this helps to reduce harmful emissions into the environment.

In this method, the preliminary grinding of the solid phase to particle sizes of 1.0-3.0 mm allows you to separate the carbon component from the metal cord (wire). When grinding to a particle size of more than 3 mm, a part of the carbon component will not separate from the metal cord, since there will be residues of the carbon component on the wire (its diameter is 1 mm or less). Grinding to a particle size of less than 1 mm requires increased energy consumption.

To obtain a homogeneous mixture of solid and liquid phases, which can be used as fuel, it is necessary that the ratio of liquid to solid phases be in the range (0.75-1.50): 1. With a higher content of the solid phase, the stability of the mixture decreases (solid phase precipitated quickly). In this case, the specific heat of combustion of the mixture also decreases (the specific heat of combustion of the liquid phase is 40-41 MJ / kg, and the solid - 30-35 MJ / kg). An increase in the content of the liquid phase beyond these limits requires an increased consumption of the liquid phase and leads to a decrease in the density of the fuel (the density of the solid phase is more than 1400 kg / m ³ and the density of the liquid phase is about 930 kg / m ³ ), which reduces the amount of energy, which can be obtained by burning 1 m of fuel, i.e. reduced fuel quality.

It was found that the circulation of the mixture using a dispersing pump allows not only to uniformly mix solid and liquid decomposition products of rubber waste, but also to reduce the content of unsaturated compounds in the resulting fuel, to achieve high stability of the resulting suspension. This effect is achieved due to the mechanical effect on the mixture. In a dispersant pump, the mixture is exposed to cavitation microstructures that occur when the cavities of cavitation bubbles are slammed shut. In this process, high pressures arise and mechanochemical activation of the surface of the particles of the solid phase occurs, as a result of which heterogeneous mechanochemical reactions occur between the liquid and solid phases, mechanochemical destruction and other processes, including the interaction of the mixture components with

9 SUBSTITUTE SHEET (RULE 26) water contained in the liquid phase. As a result of these processes, the decomposition of high molecular weight compounds that are contained in the liquid products of the decomposition of waste, with the formation of compounds with a lower molecular weight. In the resulting fuel, the content of gasoline and diesel fractions increases, the smell disappears, and the content of unsaturated compounds decreases, i.e. fuel quality is improving. At the same time, the amount of moisture in the resulting liquid fuel decreases, which leads to an increase in its specific heat of combustion and lowering the freezing temperature, i.e. also to improve its quality. The circulation of the mixture for a period of time less than 600 s does not allow to achieve uniform mixing of solid and liquid phases, as well as improve the performance of the resulting fuel. The circulation of the mixture over a period of more than 3600 s leads to an increase in energy consumption for obtaining fuel, but does not improve the quality of the fuel, since the mixing process is already completed by this time.

It is preferable to separate part of the water from the liquid phase before mixing it with the solid phase so that its content in the liquid phase is 5-18 mass. % The presence of such an amount of water in a mixture of liquid and solid phases allows you to get fuel, the combustion of which will reduce the formation of toxic combustion products - nitrogen oxides. In the process of circulating the mixture using a dispersing pump, water reacts with solid phase carbon to produce CO and H ₂ , which then react with liquid decomposition products, which leads to a decrease in the number of unsaturated compounds, i.e. hydrogenation reactions occur, and thereby an additional improvement in the quality of the resulting fuel dispersion is achieved. With a decrease in water content below 5 mass. % its influence on the quality indicators of the fuel dispersion becomes insignificant, and the increase in water content is more than 18 mass. % leads to a sharp drop in the specific heat of combustion of the resulting fuel.

The proposed process for processing solid and liquid phases generated during the thermolysis of rubber wastes can be implemented with other modifications of the proposed process for thermolysis of wastes in a coolant medium, which is a mixture of water vapor with a gaseous phase formed during thermolysis (for example, with a different organization of loading processes and unloading, etc.).

10

SUBSTITUTE SHEET (RULE 26) To solve this problem, it is also proposed a device for treating rubber waste, including a thermolysis reactor in the form of a chamber with flues for supplying and withdrawing a gas mixture, a steam generator, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the gas mixture through the reactor and a heat exchanger connected in series to the gas duct for withdrawing the gas mixture from the reactor, a condenser and a separator, as well as two loading / unloading chambers with containers and trolleys located on two opposite sides of the reactor and connected with gate locks, each container containing a chamber in the lower part with a wireless grate and a steam-gas mixture supply pipe, as well as a rotation mechanism around the longitudinal axis, and each loading / unloading chamber in the bottom its output is connected to a conveyor belt, to which a chopper and a magnetic separator are connected in series. The indicated device design provides the implementation of the proposed method - the process of thermolysis of rubber waste using a mixture of water vapor with a gaseous phase formed in the process as a heat carrier passing through the waste layer, due to the fact that it is placed in a reactor with gas ducts for supplying and withdrawing a gas-vapor mixture a container containing in the lower part a chamber with a wireless grill and a steam-gas mixture supply pipe, a heat exchanger and a fan form a closed circulation circuit.

The circulation of the gas-vapor mixture in this circuit through the waste layer provides an increase in the efficiency of heat transfer, i.e. heat transfer increases from the steam-gas mixture to the waste in the reactor, the waste treatment time is reduced, the steam consumption is reduced, the heating of the waste is more uniform (local overheating is prevented), and the quality of solid and liquid decomposition products is improved.

The loading / unloading chambers located on two opposite sides of the reactor and connected to it by lock gates are used alternately for loading waste, feeding loaded containers into the reactor and subsequent unloading. This arrangement of the chambers allows to reduce energy costs for the waste treatment process due to the possibility of returning to the reactor water vapor released during the cooling of solid products

11 SUBSTITUTE SHEET (RULE 26) decomposition from the unloaded container, and its use for heating waste in a container placed at that time in the reactor, and also because the placement of loading / unloading chambers on opposite sides of the reactor reduces heat loss through the surface of the reactor to the environment. A chamber installed at the bottom of the container with a wireless grate and a steam-gas mixture supply pipe ensures uniform supply of the gas-vapor mixture to the waste layer and prevents their failure at the bottom of the container with the formation of waste accumulations into which the gas-vapor mixture practically does not enter, as a result of which the waste in these accumulations practically does not decompose. The heat exchanger can be a shell-and-tube heat exchanger, the annular space of which is connected to the furnace, the tube space of the heat exchanger is connected to the fan outlet by its inlet, and the outlet to the gas supply duct for the gas-vapor mixture to the reactor, the fan is connected by its inlet to the gas duct leading the gas-vapor mixture from the reactor, and the output to the input heat exchanger and condenser inlet.

As another solution to the problem, a device for treating rubber waste to produce a fuel dispersion is proposed, including a thermolysis reactor in the form of a chamber with flues for supplying and outputting a gas-vapor mixture, a steam generator, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the vapor-gas mixture through the reactor and the heat exchanger, connected in series to the gas duct to withdraw the vapor-gas mixture from the reactor, a condenser, a separator torus and storage tank, as well as two loading / unloading chambers with containers on trolleys located on two opposite sides of the reactor and connected with gate locks, each container containing a chamber with a wireless grill and a steam-gas mixture supply pipe in the lower part, as well as a mechanism rotation around the longitudinal axis, and each loading / unloading chamber in the bottom part with its output is connected to a conveyor belt to which a roller mill, a magnetic separator, a cent are connected in series obezhnaya mill storage bin and the mixer in a tank with an agitator and a circulation pump-disperser, the mixer is connected to the output of liquid product from the condenser through the separator and the storage capacitance.

Using a dispersant pump allows you to more than mix solid and

12 SUBSTITUTE SHEET (RULE 26) liquid products of decomposition of rubber wastes, and to ensure a decrease in the content of unsaturated compounds in the resulting fuel dispersion due to mechanical stress (as a result of which the solid surface of the carbon residue particles is activated, mechanochemical destruction, heterogeneous mechanochemical reactions and other processes), to achieve uniform mixing and high stability of the obtained suspension, as well as remove moisture that can accumulate in liquid products when separating them in a separator from dropsy of condensate. A decrease in the amount of moisture in the fuel dispersion leads to an increase in its specific heat of combustion and a decrease in the freezing temperature, i.e. to improve the quality of the resulting product. As a result of the mechanochemical destruction (decomposition) of high molecular weight compounds that are contained in the liquid waste decomposition products, compounds with a lower molecular weight are formed, and thus the content of the gasoline and diesel fraction increases in the resulting product, i.e. its quality is increasing.

The proposed embodiment of a device for treating rubber waste to obtain a fuel dispersion can be implemented with some modifications of the loading and unloading units, for example, when there are separate chambers for loading and unloading. Brief Description of the Drawings

The method and device are illustrated by the attached figure, which shows the installation diagram, which is an embodiment of the device and implements the method.

BEST MODE FOR CARRYING OUT THE INVENTION In accordance with the drawing, the installation comprises a drive 1 connected to a conveyor 2; loading hopper 3 with shutter 4; container 5; actuator 6 connected to the lock gate 7; conveyor 8; a loading chamber 9 connected to the reactor 10; a pipe 11 for supplying a gas-vapor mixture to the lower chamber 12 of the container 5, separated from the upper chamber by a wireless grill; a gas duct 13 for supplying a gas-vapor mixture to the reactor; rotary platform 14; loading hopper 15 with shutter 16; container 17; a steam generator 18 with a flow meter 19; a heat exchanger 20 connected to a fan 21; a gas duct 22 for discharging the vapor-gas mixture from the reactor; a flow meter 23 connected to a capacitor 24; a fan 25 connected to the jacket 26 of the capacitor 24;

13 SUBSTITUTE SHEET (RULE 26) a crane 27 connected to the furnace 28; gas analyzer 29; capacity 30; a smoke exhauster 31 connected to a chimney 32; temperature sensor 33; pressure sensor 34; temperature sensor 35; a crane 36 connected to the separator 37; a valve 38 connected to the filter 39; cranes 40 and 41; storage capacity 42; lock gate 43; conveyor 44; loading chamber 45; a flow meter 46 connected to a pump 47 and nozzles 48; valve 49; temperature sensor 50; swivel mechanism 51; belt conveyor 52 with an engine 53; roll mill 54; magnetic separator 55; press 56; centrifugal mill 57; storage hopper 58; dispenser 59 connected to mixer 60; weight batcher 61; stirrer 62; dispersing pump 63; crane 64; nozzles 65; temperature sensor 66; rotary mechanism 67; belt conveyor 68 with an engine 69; valve 70; smoke pipe steam generator 71; a lower chamber 72 of the container 17, separated from the upper chamber by a wireless grid; a pipe 73 for supplying a gas-vapor mixture to the lower chamber 72 of the container 17. A method for treating rubber waste is as follows.

From drive 1, using a conveyor 2, a portion of crushed rubber waste (worn tires) is fed into the loading hopper 3. After that, the shutter 4 is opened and the waste falls under the influence of its own weight into the container 5. Then the shutter 4 is closed, the next portion of waste is fed into the loading hopper 3, after which the shutter 4 is opened and the waste falls into the container 5. The loading operation is repeated as many times as necessary to fully load the container 5. Using the actuator 6 open the lock gate 7 and, turning on the conveyor 8, the container 5 from the loading chamber 9 is fed into the reactor 10, after which the shutter 7 is closed. In this case, the container 5 in the reactor 10 is installed in such a way that the pipe 1 1 for supplying the gas-vapor mixture to the chamber 12 with the wireless grid is connected (joined) with the gas duct 13 for supplying the gas-vapor mixture in the reactor 10. The conveyor 2 is turned from the loading hopper 3 by means of a rotary platform 14 to the loading hopper 15. After this, crushed rubber waste is fed into the loading hopper 15 from the drive 1 to the loading hopper 15, the shutter 16 is opened and the waste falls under the influence of its own weight into the container 17. The container 17 is completely loaded ayut waste similar manner as described above for the container 5.

From the steam generator 18 through a flow meter 19 with a given flow rate, water vapor is supplied to the heat exchanger 20 at a temperature of 1 10-12O ⁰ C. At the same time

14 SUBSTITUTE SHEET (RULE 26) with the supply of steam to the heat exchanger 20, turn on the fan 21 and circulate the water vapor along the circuit: heat exchanger 20-chamber 12 of the container 5- layer of waste in the container 5-gas 22 withdrawing the gas mixture from the reactor 10-fan 21-heat exchanger 20. During the circulation of water steam open the flow meter 23, partially divert water vapor into the condenser 24, where it is condensed by cooling with air, which is fed to the shirt 26 of the condenser 24 using a fan 25. Water vapor passing through the waste layer in the reactor displaces the air The steam with the flow of steam is discharged to the condenser 24. Air that does not condense in the condenser 24 is supplied through the valve 27 to the furnace 28. Water vapor is discharged to the condenser 24 until the air concentration in the reactor 10 decreases to a predetermined content. After reaching the specified air content in the vapor-gas mixture, the discharge of this mixture to the condenser 24 is stopped by closing the valve 23. The air content in the reactor is monitored by the readings of the gas analyzer 29. Air removal from the reactor is necessary to prevent oxidation (burning) of waste decomposition products in the reactor 10. Simultaneously with the air outlet from the condenser 24, liquid fuel is supplied to the furnace 28 from the tank 30 and burned. The resulting high-temperature combustion products (1000 ° C and more) enter the casing of the heat exchanger 20, where they heat the water vapor flowing through the pipes of the heat exchanger 20, while they are cooled to 150-200 ° C and are discharged into the chimney 32 using a smoke exhauster 31.

When a certain temperature is reached in the reactor (depending on the type of waste) controlled by the temperature sensor 33, the process of thermal decomposition of rubber waste begins to form with the formation of solid and gaseous products, which are mixed with the circulating vapor-gas mixture. The amount of tire thermolysis products in a gas-vapor mixture is controlled by the readings of a gas analyzer 29 and, when the mass ratio of water vapor-thermolysis products is reached within 1 :( 1.0-5.0), the flow meter 23 and part of the gas-vapor mixture (water vapor) are opened and gaseous decomposition products of rubber waste) is discharged into a condenser 24, in which the products are cooled to a temperature of 100 ° C. The cooling temperature is controlled by the readings of the temperature sensor 35. The pressure in the reactor 10 is controlled by the readings of the pressure sensor 34 and using a flow meter 23 (the opening value is controlled), the pressure in the reactor 10 is maintained above atmospheric,

15 SUBSTITUTE SHEET (RULE 26) to prevent leakage from the atmosphere of air into the reactor 10. In the condenser 24, the vapor-gas mixture is cooled by heat exchange with the air supplied to the jacket 26 of the condenser. As a result of cooling the gas-vapor mixture, a liquid phase is formed, which is supplied through the valve 36 to the separator 37. In the separator 37, water is separated from the liquid decomposition products and fed through the valve 38 to the filter 39, where they are purified from organic impurities, and then the purified water through the valve 40 served in a steam generator to obtain water vapor. This helps to prevent the formation of contaminated wastewater and thus reduce emissions of harmful substances into the environment. Liquid decomposition products from the separator through the valve 41 are fed into the storage tank 42. The water is partially separated so that the residual water content in the liquid phase is in the range of 5-18 masses. %, which is controlled by the readings of a sensor installed in the separator 37 and working, for example, on the principle of measuring the electrical conductivity of a mixture of a conductive liquid (water) and non-conductive (liquid products of tire thermolysis). Gaseous products of thermolysis, not condensed in the capacitor 24, through the valve 27 is fed into the furnace 28 and burned in a mixture with liquid fuel. The burning of these products helps to prevent their release into the environment and at the same time reduce fuel consumption for heating the vapor-gas mixture in the heat exchanger 20. As the gaseous products of thermolysis are released in the reactor 10, the flow of water vapor to the heat exchanger 20 is reduced by means of a flow meter 19 and using a valve - flow meters 23 regulate the output of a part of the gas-vapor mixture to the condenser 24 so that the pressure in the reactor 10 is constantly above atmospheric. This is controlled by the readings of the pressure sensor 34. At the same time, by the readings of the gas analyzer 29, the water vapor content in the steam-gas mixture is controlled and the mass ratio of water vapor to thermolysis products is maintained within the range of 1: (1, 0-5.0). In the process of thermolysis, the amount of gaseous products formed first increases to a maximum value, and then decreases until the complete exit of gaseous products.

Since, as indicated above, by supplying water vapor to the reactor and withdrawing a part of the gas-vapor mixture to the condenser 24, the pressure in the reactor 10 is kept constant while maintaining the mass ratio of water vapor-decomposition products of the tires in the circulating gas-vapor mixture

16. SUBSTITUTE SHEET (RULE 26) within 1: (1, 0-5.0), then the moment of complete termination of the release of gaseous thermolysis products (the moment the process ends) corresponds to the moment of complete closure of the flow meter 23 and the flow meter 19, i.e. at this moment, the steam supply to the reactor 10 is stopped and the steam-gas mixture is withdrawn from the reactor to maintain the pressure in the reactor above atmospheric pressure and to maintain the mass ratio of vapor-decomposition products of tires within 1 :( 1.0-5.0). From this moment on, only the residual vapor-gas mixture circulates in the reactor. Before withdrawing the container 5 from the reactor 10 in order to avoid explosion of the residual vapor-gas mixture (when the lock gate 7 is opened from the loading chamber 9, air may enter the reactor 10), it must be removed from the reactor 10. For this, the flow meter 19 and the flow meter 23 are again opened. and purge the reactor with steam for 5 minutes, and then the taps 19 and 23 are closed. After that, the lock gate 7 is opened and, using the conveyor 8, the container 5 is withdrawn from the reactor 10 into the loading chamber 9. Then, the shutter 7 is closed. The shutter 43 is opened and, using a conveyor 44, a container 17 is fed from the loading chamber 45 to the reactor 10, and then the shutter 43 is closed.

After the container 5 is brought into the loading chamber 9, water is supplied to the nozzles 48 through a valve 47 through a valve 47; the flow meter 46 uses a pump 47 to spray water over a layer of solid residue in the container 5. Water enters the solid residue and cools it, and it evaporates, and the resulting steam through the valve 49 leaves the charge chamber 9 into the reactor 10. The cooling temperature of the solid residue in the container 5 is monitored by the temperature sensor 50 and after cooling to 120 ⁰ C, the water atomization is stopped.

Using the rotary mechanism 51, the container 5 is turned and set upside down, as a result of which the solid residue is poured out of the container 5 from the container 5 onto the belt conveyor 52, driven by the motor 53 and feeding the solid residue into the roller mill 54.

After unloading, the container 5 is installed in the working position (bottom part down) and load it, as described above.

In the roll mill 54, the solid residue passing through the rolls is ground to a particle size of 1-3 mm. After the roll mill 54, the solid phase is fed to an electromagnetic separator 55 where metal cord is separated from the carbonaceous decomposition products. The metal is fed into a press 56 and pressed into

17 SUBSTITUTE SHEET (RULE 26) briquettes, and the carbon residue is fed to a centrifugal mill 57, where it is ground to a particle size of 0.05-0.1 mm and then fed to a storage hopper 58.

From the storage hopper 58 into the mixer 60 through a weighing batcher 61 serves a predetermined amount of crushed carbon residue. At the same time, a predetermined amount of the liquid phase is supplied from the tank 42 through the flow meter 59 to the mixer 60. By adjusting the flow meter 59 to the amount of the supplied liquid phase, in the mixer 58, the ratio of solid and liquid phases is set in the range l: (0.75-1.5). Once this ratio has been established, the mechanical stirrer 62 is turned on and the solid and liquid phases are mixed. At the same time, the dispersant pump 63 is turned on and the mixture is circulated in a closed loop: mixer-pump-dispersant-mixer for 600-3600 s.

The process of thermal decomposition of the rubber waste that is in the container 17 is carried out in the reactor 10 similarly to that described above, using the pipe 73 for supplying the vapor-gas mixture to the chamber 72. At the end of the process, to cool the solid residue in the container 17 from the filter 39 through the valve 64 into the nozzles 65, water is supplied, and the cooling temperature is controlled by the readings of the temperature sensor 66. The resulting steam from the chamber 17 enters the reactor 10 through the valve 70. After cooling, the container 17 is turned using a rotary mechanism zm 67 and set upside down. The solid residue from the container 17 is poured onto the conveyor 68, which is driven by the engine 69 and the solid residue is fed into the roller mill 54. Thus, the containers 5 and 17 are loaded with waste and fed into the reactor

10 in turn.

The invention is also illustrated by the examples. Example 1. 600 kg of waste are loaded into a container of 5 portions of 100 kg each and fed from the loading chamber 9 to the reactor 10. The container 5 is installed in the reactor 10 so that the pipe 11 for supplying the gas-vapor mixture into the chamber 12 of the container 5 is connected (joined) the gas duct 13 for supplying the gas-vapor mixture to the reactor 10. Using the rotary platform 14, the conveyor 2 is turned from the loading hopper 3 to the loading hopper 15 and 600 kg of waste are loaded into the container 17 similarly to that described.

eighteen

SUBSTITUTE SHEET (RULE 26) From the steam generator 18 through a flow meter 19 with a flow rate of 300 kg / h, steam is supplied to the heat exchanger 20 at a temperature of 1 10 ⁰ C (liquid fuel consumption in the steam generator 24 kg / h with a heat of combustion of 40 MJ / kg). Simultaneously with the steam supply to the heat exchanger 20, the fan 21 is turned on and water vapor is circulated along the circuit: the heat exchanger 20-chamber of the 12-layer waste in the container 5-gas 22 of the outlet of the gas-vapor mixture from the reactor 10-fan 21-heat exchanger 20. In the process of water vapor circulation open the flow meter 23 and for 10 minutes steam at a flow rate of 180 kg / h is discharged into a condenser 24 cooled by air, which is supplied through a jacket 26 of the condenser 24 with a fan 25, and the corresponding amount of steam is 30 kg in 10 minutes (or 37.5 m ³ at pl specificity of 0.8 kg / m ³ ) - enters the reactor from the steam generator. With a reactor volume of 6 m ³ , a 6-fold change of the gaseous medium in the reactor takes place, as a result of which almost all air is displaced from the reactor, which is removed with the steam stream into the condenser 24 and then through the valve 27 to the furnace 28. The air content in the reactor control according to the testimony of the gas analyzer 29. After reaching the air content in the vapor-gas mixture of not more than 5 mass. % removal of this mixture to the condenser 24 is stopped by closing the valve 23. At the same time, using the i9 valve, the supply of water vapor to the heat exchanger 20 is stopped. At the same time, 36 kg / h of liquid fuel is supplied to the furnace 28 from the vessel 30 to the furnace 28. and burn it. The resulting combustion products (396 kg / h) enter the casing of the heat exchanger 20, heat the steam flowing through the pipes to 700 ⁰ C, cool to 15 ^{O 0} C and are discharged into the chimney 32. When the temperature reaches 28 ^{O 0} C, which is controlled by the sensor temperature 33, the process of thermal decomposition of rubber waste with the formation of solid and gaseous products begins to proceed in the reactor. Gaseous products are mixed with a circulating vapor-gas mixture. The decomposition process takes 2 hours (7200 seconds). The consumption of the gas-vapor mixture during its circulation with the help of the fan 21 is 600 kg / h. The amount of thermolysis products in a gas-vapor mixture is controlled by the readings of a gas analyzer 29 and, upon reaching a mass ratio between water vapor and thermolysis products of 1: 1, a flow meter 23 is opened and a part of the gas-vapor mixture with a flow rate of 300 kg / h is discharged into

19 SUBSTITUTE SHEET (RULE 26) a condenser 24, in which the products are cooled to a temperature of 9O ⁰ C. The cooling temperature is controlled by the readings of the temperature sensor 35. The pressure in the reactor 10 is controlled by the readings of the pressure sensor 34 and the pressure in the reactor 10 is maintained above atmospheric pressure using a flow meter 23 to prevent leakage from the atmosphere of air to the reactor 10. At the same time, by opening the valve 19, 150 kg / h of water vapor is supplied to the reactor to maintain the above ratio between water vapor and thermolysis products in the vapor-gas mixture.

The vapor-gas mixture withdrawn from the reactor 10 is subjected to partial condensation in a condenser 24, which is cooled by heat exchange with the air supplied to the jacket 26. In this case, all water vapor and 90% of the mass of gaseous thermolysis products condense, i.e. 150 kg / h of water vapor and 135 kg / h of gaseous products of thermolysis. The resulting condensate is separated in a separator 37, and the aqueous layer is fed through a valve 38 to a filter 39, where it is cleaned of organic impurities. Then, through the valve 40, purified water (142.9 kg / h) is supplied to the steam generator to produce water vapor. This helps to prevent the formation of contaminated wastewater and thus reduce emissions of harmful substances into the environment. Liquid decomposition products from the separator (142.1 kg / h) are supplied through a tap 41 to a storage tank 42. The residual water content in the liquid phase is 5 mass. %, which is controlled by the readings of the sensor installed in the separator 37 and operating on the principle of measuring the electrical conductivity of a mixture of a conductive liquid (water) and non-conductive (liquid thermolysis products). Non-condensable gaseous products of thermolysis from the condenser 24 through the valve 27 in the amount of 15 kg / h are fed into the furnace 28 and burned in a mixture with liquid fuel, which helps to prevent their release into the environment and at the same time reduce fuel consumption from 36 kg / h to 28.5 kg / h

As the process proceeds and the amount of gaseous thermolysis products in the circulating mixture increases, the supply of water vapor to the heat exchanger 20 is reduced and, using a flow meter 23, the part of the vapor-gas mixture is regulated to the condenser 24 so that the pressure in the reactor 10 is constantly above atmospheric. This is controlled by the readings of the pressure sensor 34. At the same time, by the readings of the gas analyzer 29, the water vapor content in the gas-vapor mixture is monitored and the mass

20 SUBSTITUTE SHEET (RULE 26) the ratio of water vapor to thermolysis products at a level of 1: 1. When the quantity of gaseous thermolysis products decreases, the amount of steam-gas mixture discharged from the reactor is reduced by means of a flow meter 23 and, simultaneously, a quantity of steam is introduced using a flow meter 19 until the formation of gaseous thermolysis products is completely stopped, which corresponds to the moment the valve flow meter 23 is completely closed flow meter valve 19. From this moment on, the residual vapor-gas mixture circulates in the reactor. Before withdrawing the container 5 from the reactor 10, the flow meter 19 and the flow meter 23 are opened and the reactor is blown with steam for 5 minutes, and then the valves 19 and 23 are closed. After that, the lock gate 7 is opened and, using the conveyor 8, the container 5 is withdrawn from the reactor 10 into the loading chamber 9. Then, the shutter 7 is closed. The shutter 43 is opened and, using the conveyor 44, the container 17 from the loading chamber 45 is fed into the reactor 10, and then the shutter 43 is closed. After the container 5 is discharged into the loading chamber 9 from the filter 39, 54 kg of water are supplied to the nozzles 48 through a flowmeter 46 using a pump 47 and sprayed over a layer of solid residue in the container 5 for 10 minutes. Water enters the solid residue and cools it, evaporating, the steam formed through the valve 49 leaves the loading chamber 9 into the reactor 10. The cooling temperature of the solid residue in the container 5 is monitored by the temperature sensor 50 and, after reaching 120 ° C, the spraying of water is stopped.

Using the rotary mechanism 51, the container 5 is turned and set upside down, as a result of which a solid residue is poured from the container 5 in the amount of 300 kg (50 wt% of the number of worn tires) under its own weight onto the conveyor belt 52, which feeds the solid residue into the roll mill 54. The container 5 after unloading is installed in the working position (bottom part down) and load it, as described above.

In the roll mill 54, the solid residue passing through the rolls is ground to a particle size of 1 mm, as a result of which the carbon component (solid phase) is separated from the metal cord. The predetermined grinding value in the roller mill is set by adjusting the distance between the rollers.

After the roll mill 54, the solid phase and the metal cord are fed into

21 SUBSTITUTE SHEET (RULE 26) magnetic separator 55. In the magnetic separator 55, 90 kg of metal is separated from the carbonaceous decomposition products, fed to a press 56 and pressed into briquettes. The carbon residue in the amount of 210 kg is fed to a centrifugal mill 57, where it is ground to a particle size of 0.05-0.1 mm and then fed to a storage hopper 58.

From the storage hopper 58, 210 kg of ground carbon residue are supplied to the mixer 60 through the weight dispenser 61. At the same time, 157.5 kg of the liquid phase (liquid to solid phase ratio is 0.75: 1) is supplied to the mixer 60 from the tank 42 through the flow meter 59. Once this ratio has been established, the mechanical stirrer 62 is turned on and the solid and liquid phases are mixed. At the same time, the dispersant pump 63 is turned on and the mixture is circulated in a closed loop: mixer-pump-dispersant-mixer for 600 s.

Similarly carry out the process of thermal decomposition of rubber waste, which are in the container 17. Thus, the containers 5 and 17 are alternately loaded with waste and fed into the reactor 10.

Example 2. The process is carried out analogously to example 1 with the following differences. In the container 5, as well as in the container 17, in portions of 150 kg serves 900 kg of waste, crushed to a piece size of 150 mm. Steam is supplied to the heat exchanger 20 at a temperature of HO ⁰ C with a flow rate of 450 kg / h. 36 kg / h of liquid fuel with a calorific value of 40 MJ / kg are burned in a steam generator. In the process of circulating water vapor, the flow meter 23 is opened and for 10 minutes water vapor at a flow rate of 270 kg / h is discharged into the condenser 24, and the corresponding amount of steam - 45 kg (56.3 m ³ ) in 10 minutes - enters the reactor from a steam generator, which with a reactor volume of 6 m ³ means a 9-fold change in the gas medium in the reactor. Simultaneously with the process of removing air from the condenser 24, from the tank 30, 54 kg / h of liquid fuel is supplied to the furnace 28 and burned with the formation of 594 kg / h of combustion products. The thermolysis process takes 2 hours (7200 s). The flow rate of the circulating vapor-gas mixture during thermolysis is 900 kg / h. The mass ratio of water vapor to thermolysis products is set at 1: 5.

The vapor-gas mixture withdrawn from the reactor 10 (216 kg / h) is subjected to partial condensation in the condenser 24. In this case, all water vapor and 85% of the mass of gaseous thermolysis products are condensed, i.e. 36 kg / h of water vapor and 153 kg / h of gaseous thermolysis products. In the separator 37, water is separated from

22 SUBSTITUTE SHEET (RULE 26) liquid decomposition products and serves it through a valve 38 to a filter 39, where it is cleaned of organic impurities. Then, through the valve 40, purified water (2.15 kg / h) is supplied to the steam generator to produce water vapor. Liquid decomposition products from the separator (186.85 kg / h) are supplied through a tap 41 to a storage tank 42. The residual water content in the liquid phase is 18 mass. % Non-condensable gaseous products of thermolysis from the condenser 24 through the valve 27 in the amount of 27 kg / h are fed into the furnace 28 and burned in a mixture with liquid fuel, which helps to prevent their release into the environment and at the same time reduce fuel consumption from 54 kg / h to 40.5 kg / h After completion of the process and withdrawal of the container 5 into the loading chamber 9 from the filter 39, 81 kg of water are supplied to the nozzles 48 through a flow meter 46 using a pump 47 and sprayed over a layer of solid residue in the container 5 for 10 minutes. The solid residue from the container 5 in an amount of 540 kg (60 wt.% Of the number of worn tires) is crushed in a roller mill 54 to a particle size of 3 mm In a magnetic separator 55, 162 kg of metal are separated from the carbonaceous decomposition products and pressed into briquettes. The carbon residue (378 kg) in a centrifugal mill 57 is ground to a particle size of 0.05-0.1 mm and then fed to a storage hopper 58.

From the storage hopper 58 to the mixer 60 through a weight batcher 61 serves 249 kg of crushed carbon residue. At the same time, 373 kg of the liquid phase (ratio of liquid to solid phase is 1.5: 1) is supplied from mixer 42 through a flow meter 59 to a mixer 60. Once this ratio has been established, the mechanical stirrer 62 is turned on and the solid and liquid phases are mixed. At the same time, the dispersant pump 63 is turned on and the mixture is circulated in a closed loop: mixer-pump-dispersant-mixer for 3600 s.

Industrial applicability

The invention can be used in the treatment of various industrial and household waste, primarily worn automobile tires, which helps to improve the environment with useful products of high quality, in particular fuel dispersions, with reduced energy costs for processing and low emissions into the environment .

23 SUBSTITUTE SHEET (RULE 26)

Claims

METHOD AND DEVICE FOR THE PROCESSING OF RUBBER WASTE

1. A method of treating rubber waste, including feeding waste into a reactor in a mobile container from a first loading / unloading chamber, thermolizing it in a reactor in a medium containing water vapor of a heat carrier passing through a waste layer to form a gaseous and solid phases, withdrawing a gaseous phase from the reactor returning part of the gaseous phase to the reactor, withdrawing the solid phase from the reactor by moving the container with the solid phase from the reactor at the end of the thermolysis process in the reactor to the first loading / unloading chamber, unloading solid phase when the container is rotated relative to the longitudinal axis, grinding the solid phase and its magnetic treatment, cooling the gaseous phase, separating the liquid phase condensed by cooling the gaseous phase, burning the non-condensed gaseous phase to heat water vapor in the heat exchanger, and then repeating the process in which waste into the reactor in a mobile container is carried out from the second loading / unloading chamber, and the container is transferred from the reactor to the second at the end of the thermolysis process in the reactor th load / unload chamber.

2. The method according to paragraph 1, characterized in that thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to l: (l, 0-5.0).

3. A method of processing rubber waste to obtain a fuel dispersion, comprising feeding the waste into the reactor in a mobile container from the first loading / unloading chamber, thermolizing it in the reactor in a medium containing water vapor coolant, passed through the waste layer, with the formation of gaseous and solid phases the gaseous phase from the reactor, the return of part of the gaseous phase to the reactor, the removal of the solid phase from the reactor by moving the container with the solid phase from the reactor at the end of the thermolysis process in the reactor in the first chamber loading / unloading, unloading of the solid phase when the container is rotated relative to the longitudinal axis, grinding the solid phase to a particle size of 1.0-3.0 mm, its magnetic processing and further grinding, cooling the gaseous phase, separating the liquid phase condensed by cooling the gaseous phase, separating part of the water from the liquid phase, mixing the liquid and solid phases in the mixer with a mass ratio of (0.75-1.5): 1, circulating the mixture through the mixer using a dispersing pump in

24 SUBSTITUTE SHEET (RULE 26) for 600-3600 s, burning the non-condensed gaseous phase to heat water vapor in the heat exchanger, then repeating the process in which waste is fed into the reactor in a mobile container from the second loading / unloading chamber, and the container is transferred from the reactor at the end of the thermolysis process in the reactor into the second loading / unloading chamber.

4. The method according to paragraph 3, characterized in that the thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to l: (l, 0-5.0).

5. The method according to paragraph 3, characterized in that part of the water is separated from the liquid phase to its content in the liquid phase in the range of 5-18 mass. %

6. A method of processing rubber waste to obtain a fuel dispersion, including thermolysis of waste in a reactor in a medium containing water vapor, with the formation of a gaseous and solid phases, the withdrawal of the gaseous phase and solid phase from the reactor, the return of part of the gaseous phase to the reactor, grinding of the solid phase to particle sizes of 1.0-3.0 mm, its magnetic treatment and further grinding, cooling of the gaseous phase, separation of the liquid phase condensed by cooling of the gaseous phase, separation of part of the water from the liquid phase, cm the liquid and solid phases are mixed in the mixer at a mass ratio of (0.75-1, 50): 1, the mixture is circulated through the mixer using a dispersing pump for 600-3600 s, and the non-condensed gaseous phase is burned to heat water vapor in the heat exchanger.

7. The method according to paragraph 6, characterized in that the thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to l: (l, 0-5.0).

8. The method according to paragraph 6, characterized in that a portion of the water is separated from the liquid phase to its content in the liquid phase in the range of 5-18 mass. %

9. A device for treating rubber waste, including a thermolysis reactor in the form of a chamber with flues for supplying and withdrawing a gas mixture, a steam generator, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the gas mixture through the reactor and the heat exchanger, in series a condenser and a separator, as well as two loading / unloading chambers with containers on trolleys connected to the gas duct to withdraw the gas mixture from the reactor

25

SUBSTITUTE SHEET (RULE 26) located on two opposite sides of the reactor and connected with gate locks, each container in the lower part containing a chamber with a wireless grill and a steam-gas mixture supply pipe, as well as a rotation mechanism around the longitudinal axis, and each loading / unloading chamber in the bottom part is connected with its outlet to the conveyor belt, to which the chopper and the magnetic separator are connected in series.

10. A device for treating rubber waste with obtaining a fuel dispersion, comprising a thermolysis reactor in the form of a chamber with flues for supplying and outputting a steam-gas mixture, a steam generator, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the vapor-gas mixture through the reactor and a heat exchanger connected in series to the gas duct for withdrawing the gas mixture from the reactor, a condenser, a separator and a storage tank, as well as two loading / unloading chambers with cont trolleys on two opposite sides of the reactor and connected with lock gates, each container in the lower part containing a chamber with a wireless grate and a steam-gas mixture supply pipe, as well as a rotation mechanism around the longitudinal axis, and each loading / unloading chamber in the bottom parts with its output connected to a conveyor belt to which a roller mill, a magnetic separator, a centrifugal mill, a storage hopper and a mixer in the form of a container with a mixer are connected in series minutes and a circulation pump-disperser, the mixer is connected to the output of liquid product from the condenser through the separator and the storage capacitance.

11. A device for treating rubber waste with obtaining a fuel dispersion, including a thermolysis reactor with flues for supplying and outputting a gas-vapor mixture, a loading and unloading chamber, a heat exchanger for overheating the steam generated in the steam generator, a furnace for heating the heat exchanger, a fan for circulating the gas mixture through the reactor and a heat exchanger connected in series to the gas duct for withdrawing the vapor-gas mixture from the reactor, a condenser, a separator and a storage tank, as well as connected in series to the chamber e discharging roller mill, the magnetic separator, a centrifugal mill, a storage hopper and a mixer in a container with an agitator and a circulation pump-disperser, the mixer is connected to the output of liquid product from the condenser through the separator

26 SUBSTITUTE SHEET (RULE 26) and storage capacity.

12. Fuel dispersion prepared by the method according to one of paragraphs 3-5.

13. Fuel dispersion prepared by the method according to one of paragraphs 6-8.

27 SUBSTITUTE SHEET (RULE 26)