RU2394680C2 - Method and device for processing rubber wastes - Google Patents

Abstract

FIELD: process engineering.

SUBSTANCE: invention relates to processing of wastes and can be use in chemical and rubber industries to produce ingredients of rubber mixes from petrochemical stock wastes. Incompliance with proposed method, rubber wastes, particularly worn-out ties are fed in movable container reactor fro first loading/unloading chamber to be subjected to thermolysis in heat carrier containing superheated steam continuously forced through wastes layer. Formed gaseous phase with withdrawn from the reactor and, partially, returned into the latter mixed with steam, preferably, with steam-to-gaseous phase-ratio of 1:(1.0-5.0). Solid phase is withdrawn from the reactor in moving the container back into first loading/unloading chamber on turning said container relative to lengthwise axis. Then it is ground and subjected to magnetic treatment for separation of metal inclusions. Portion of withdrawn gaseous phase is cooled to separate liquid phase condensed thereat. Gaseous phase not condensed is fired using released heat for superheating of steam. Then the process is repeated by loading wastes into reactor from second loading/unloading chamber and in moving container into second loading/unloading chamber after thermolysis termination. Solid and liquid phase produced in said process are used, for example as fuels or separately, or on mixing them to produce fuel dispersion. In the latter case, solid phase is ground to grains size of 1.0-3.0 mm to perform magnetic treatment and further grinding to, for example 0.05-0.1 mm. A portion of water is extracted from liquid phase to have its content in said phase varying from 5 to 18 % by weight. Now, liquid and solid phases are mixed in mixed at weight ratio of (0.75-1.50):1 and obtained mix is subjected to circulation via disperser by dispersing pump for 600-3600 s. Proposed device comprises thermolysis reactor representing a chamber with gas ducts to feed/discharge steam-gas mix, steam generator, steam superheating heat exchanger, heat exchanger heating furnace, blower to force steam-gas mix through reactor and heat exchanger communicated with gas duct to discharge steam-gas mix from reactor, condenser and separator, as well as two loading/unloading chamber with containers on trucks. Said loading/unloading chambers are arranged on opposite sides of the reactor are connected thereto by gate locks. Every container comprises chamber with no-cave-in grid and gas-steam mix feed branch pipe arranged at container bottom, and mechanism of turning about lengthwise axis. Said bottom part of every loading/unloading chamber is connected with belt conveyor whereto connected are grinder and magnetic separator, and, in case, fuel dispersion is produced, it includes centrifugal mill, accumulating hopper and mixer representing a vessel with mixer and circulation dispersing pump. Said mixer communicates with liquid product discharge from condenser via separator and accumulating tank.

EFFECT: production of fuel dispersions at lower power consumption.

13 cl, 1 dwg, 2 ex

Description

Technical field

The invention relates to waste treatment technology and can be used in the chemical and rubber industry, to obtain rubber compounds ingredients from petrochemical waste, and can also be used in the energy sector to produce fuels and their components.

State of the art

A known method of processing waste polymer compositions, including their thermolysis in a reactor at 400-1500 ° C in a steam-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, С09С 1/48, 1980).

The disadvantages of this method include:

1. Large specific energy consumption, which is due to the high temperature of thermolysis (up to 1500 ° C), as well as large thermal losses at this temperature to the environment.

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 ° 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 is 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 explosion hazard due to the presence of vacuum in the thermolysis chamber and the possibility of air entering the chamber from the environment, which may ultimately 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 for the treatment of rubber waste, including their thermolysis in a reactor in a coolant, separation of the solid phase, separation of liquid and gaseous phases by condensation, use as a coolant superheated to 300-1600 ° 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 gaseous products decomposition of waste (RU 2076501, B29B 17/00, C08J 11/10, C08J 11/14, 1997). Before thermolysis, rubber waste is mixed with 3-40 wt.% 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 presence of 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 liquid and solid phases in the mixer (US 5780518, 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 is crushed to 0.001-0.210 mm particle size after separation, and the liquid phase is mixed with 23.0-55.8 wt.% Of 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 the thermolysis of rubber waste (uncrushed tires), 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 carbon black gas generator, the heater shells being installed outside and inside the integral ring thermolysis chamber, which can be rotated and about a horizontal axis by means of the supporting device with a winch (RU 2258078, V29V 17/00, S10V 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 exchange between the heating gas and 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 (uncrushed 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 carbonaceous residue of thermolysis of tires due to the deposition of part of the liquid products of thermolysis on the particles of the carbon residue during discharge of the residue through a water seal, on the surface of which the gaseous products of thermolysis 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 (unmilled tires) is known, including a thermolysis reactor in the form of a sealed chamber with flues for supplying and discharging a gas mixture, a gas heater connected to an outlet to a duct for supplying a gas mixture to a reactor, a condenser for condensing part of the thermolysis products connected to an input to the outlet of the reactor, a compressor for circulating the gas mixture, connected by an inlet to the outlet of the condenser and an outlet to the inlet of the heater, a separator with a container for collecting liquid resulting from the term Lisa (RU 2212430, C10G 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, a container in the loading chamber on a trolley with the possibility of moving it into the reactor and from the reactor to the cooling and unloading chamber (RU 2247025, BVB 17/00, C08J 11/10, 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 loading / unloading chamber, unloading the 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, subsequent the repetition of the process in which the waste is fed into the reactor in a mobile container from the second loading / unloading chamber, and the container at the end of the thermolysis process in the reactor is moved from the reactor to 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 the mixture equal to 1: (1.0-5.0). A decrease in the content of gaseous decomposition products in the vapor-gas mixture to a ratio of less than 1: 1 leads to a sharp decrease in the specific heat to a value equal to the specific heat of pure water vapor, as well as to an increase in the consumption of water vapor. 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 of (0.75-1.50): 1, circulating the mixture through the mixer using a dispersing pump torus for 600-3600 s, burning the non-condensed gaseous phase to heat water vapor in a 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 from the thermolysis process to the reactor reactor into 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. Using part of the water to produce fuel reduces the load on the purification systems and leads to an increase in the amount of fuel obtained, and it is most natural to return the water separated from the liquid phase 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 and solid phases be in the range (0.75-1.50): 1. With a higher solids content, the stability of the mixture decreases (the solid phase precipitates rapidly). 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 ^{3 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 components of the mixture with 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 wt.%. 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. During the circulation of the mixture using a dispersing pump, water reacts with carbon in the solid phase to form 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 wt.%, Its effect on fuel dispersion quality indicators becomes insignificant, and an increase in water content of more than 18 wt.% 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.).

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 cooling of the solid decomposition products from the unloaded container, and its use for heating the waste in the 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.

The use of a dispersant pump allows not only mixing solid and liquid decomposition products of rubber wastes, but also ensuring a reduction in the content of unsaturated compounds in the resulting fuel dispersion due to mechanical stress (as a result of which the solid surface of carbon particles is activated, mechanochemical destruction, heterogeneous mechanochemical reactions, and others processes), achieve uniform mixing and high stability of the resulting suspension, as well as remove moisture that can accumulate in liquid products during their separation in a separator of the condensed water. 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 drawing, which shows a diagram of the installation, which is an embodiment of the device and implements the method.

The best embodiment of 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; 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.

The method of processing 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 under the influence of its own weight falls 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 so 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 11 for supplying the gas-vapor mixture to the chamber 12 with a wireless grate is connected (joined) with the gas duct 13 for supplying the gas-vapor mixture to the reactor 10. The conveyor 2 is turned from the loading hopper 3 to loading hopper 15. Thereafter, crushed rubber waste is fed from the drive 1 to the loading hopper 15 by the conveyor 2, the shutter 16 is opened, and the waste, under the influence of its own weight, falls 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 the flow meter 19 with a given flow rate, water vapor is supplied to the heat exchanger 20 at a temperature of 110-120 ° C. Simultaneously with the supply of steam to the heat exchanger 20, the fan 21 is turned on and the water vapor is circulated along the circuit: heat exchanger 20 - chamber 12 of the container 5 - waste layer in the container 5 - gas duct 22 for withdrawing the gas mixture from the reactor 10 - fan 21 - heat exchanger 20. During the circulation water vapor, the flow meter 23 is opened, water vapor is partially diverted to the condenser 24, where it is condensed by cooling with air, which is supplied to the jacket 26 of the condenser 24 using a fan 25. Water vapor passing through the waste layer into the reactor e, displaces the air, which is discharged to the condenser 24 with a steam stream. Air that does not condense in the condenser 24 is fed through the valve 27 to the furnace 28. Water vapor is removed to the condenser 24 until the air concentration in the reactor 10 decreases to specified 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 being 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 are opened (water vapor) 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 the pressure in the reactor 10 is maintained above atmospheric pressure using a flow meter 23 (adjust the opening value) to prevent air from entering the reactor 10. B the condenser 24 the gas-vapor 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 wt.%, Which is controlled by the readings of the 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 gaseous thermolysis products are evolved in the reactor 10 using a flow meter 19, the flow of water vapor to the heat exchanger 20 is reduced and, with the help of a flow meter 23, the part of the gas-vapor 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 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 - tire decomposition products in the circulating gas-vapor mixture 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 closing 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 vapor-gas mixture is withdrawn from the reactor to maintain the pressure in the reactor above atmospheric pressure and to maintain the weight 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 from the filter 39, water is 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. Water enters the solid residue and cools it, and it evaporates, and the water vapor generated 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 cooling to 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 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 briquettes, and the carbon residue is fed into 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 the solid and liquid phases is set within 1: (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 gas-vapor 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 rotated using a rotary mechanism ma 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 serves the solid residue in a 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 supplied 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 to the chamber 12 of the container 5 is connected (joined) with the supply duct 13 the gas-vapor mixture into 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.

From the steam generator 18 through the flow meter 19 with a flow rate of 300 kg / h, steam is supplied to the heat exchanger 20 at a temperature of 110 ° 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 the water vapor is circulated along the circuit: heat exchanger 20 — chamber 12 — waste layer in the container 5 — gas duct 22 for discharging the vapor – gas 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 the 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 a density 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 occurs, as a result of which almost all air is displaced from the reactor, which is removed with a steam stream into the condenser 24 and then through the valve 27 to the furnace 28. The air content in the reactor is controlled according to the testimony of the gas analyzer 29. After reaching an air content in the gas mixture of not more than 5 wt.%, the removal of this mixture to the condenser 24 is stopped by closing the valve 23. At the same time, using the valve 19, the flow of water vapor to the heat exchanger 20. is stopped. cession air outlet from the condenser 24 from the tank 30 into the furnace 28 is fed a liquid fuel in an amount of 36 kg / h 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 ° C, cool to 150 ° C and are discharged into the chimney 32.

When the temperature reaches 280 ° C, which is controlled by the temperature sensor 33, the process of thermal decomposition of rubber waste begins to form in the reactor with the formation of solid and gaseous products. 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 the condenser 24, in which products are cooled to a temperature of 90 ° 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 pressure in the reactor 10 is maintained above atmospheric pressure to prevent leakage from the atmosphere into the reactor 10. At the same time, by opening the valve 19, 150 kg / h of water vapor are fed into the reactor to maintain the above ratio between water vapor and thermolysis products in the gas-vapor 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 fed through a tap 41 to the storage tank 42. The residual water content in the liquid phase is 5 wt.%, Which is controlled by the readings of the sensor installed in the separator 37 and working on the principle of specific 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 ratio of water vapor to thermolysis products is maintained at a level of 1: 1. When the amount 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 19. Starting from this moment, the residual vapor-gas mixture circulates in the reactor. Before the container 5 is removed 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 water atomization is stopped.

Using the rotary mechanism 51, the container 5 is turned and installed with the bottom up, 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) 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 to the magnetic separator 55. In the magnetic separator 55, 90 kg of metal are 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, shredded to pieces of 150 mm. Steam is supplied to the heat exchanger 20 at a temperature of 110 ° 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 environment in the reactor. Simultaneously with the process of removing air from the condenser 24 from the container 30, liquid fuel is supplied to the furnace 28 in an amount of 54 kg / h 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 the liquid decomposition products and fed through a valve 38 to a filter 39, where they are purified from organic impurities. Then, through the valve 40, purified water (2.15 kg / h) is supplied to the steam generator to produce water vapor. The 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 wt.%. 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 processing of various industrial and household waste, primarily worn automobile tires, which allows 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.

Claims (13)

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 during rotation of the container 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 is fed to the reactor in a mobile container is carried out from the second loading / unloading chamber, and the container at the end of the thermolysis process in the reactor is moved from the reactor to the second th camera loading / unloading. 2. The method according to claim 1, characterized in that the thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to 1: (1.0-5.0). 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 into the first 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 at a mass ratio of (0.75-1.50): 1, circulating the mixture through the mixer using a dispersing pump for 600-3600 s, burning uncondensed gaseous phases for heating water vapor in the heat exchanger, the subsequent repetition of 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 to the second loading / unloading chamber at the end of the thermolysis process in the reactor. 4. The method according to claim 3, characterized in that thermolysis is carried out with a mass ratio of water vapor and gaseous phase in the mixture equal to 1: (1.0-5.0). 5. The method according to claim 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 wt.%. 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 (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 claim 6, characterized in that the thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to 1: (1.0-5.0). 8. The method according to claim 6, 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 wt.%. 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 connected to the gas duct for withdrawing the gas-vapor mixture from the reactor, as well as two loading / unloading chambers with containers on trolleys located on two opposite sides x sides of the reactor and gate locks connected to it, 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 part is connected to the conveyor belt by its outlet 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 and the storage capacitance. 12. Fuel dispersion prepared by the method according to one of claims 3 to 5. 13. Fuel dispersion prepared by the method according to one of claims 6 to 8.

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