RU2502596C2 - Method of rubber wastes processing - Google Patents

Abstract

FIELD: process engineering.

SUBSTANCE: invention relates to processing of wastes and can be used in chemical and rubber-textile industry for production of rubber mix ingredients from wastes of petrochemical industry wastes, fuel analogs and rubber mix ingredients. Proposed method comprises feeding the wastes into reactor, their thermolysis in the medium of heat carrier forced through the bed of wastes to form gas and fluid phases, discharge of gas phase therefrom, discharge of solid phase from reactor by displacing the container with solid phase from reactor into first chamber, discharge of solid phase and its electromagnetic processing, extraction of liquid phase from gas by cooling, extraction of water from fluid phase, compression of gas phase, process reiteration whereat wastes are fed into reactor in movable container from second chamber to allow displacement of the container from reactor to second chamber after thermolysis termination.

EFFECT: lower power consumption and emissions, higher quality of target products.

1 dwg

Description

The invention relates to a technology for the processing of organic waste and can be applied in the chemical and rubber industries, to obtain petrochemical feedstocks, analogs of fuels, rubber compounds ingredients from waste.

A known method of processing rubber waste (see patent of the Russian Federation No. 2245247, publ. 01/27/2005, bull. No. 3).

A method for processing rubber waste includes its thermal decomposition in a furnace, separation of decomposition products into solid and gaseous, separation of the liquid phase from gaseous products and removal of the latter to incineration to maintain the decomposition process. Prior to thermal decomposition, the waste is mixed with 5-15 wt.% Water, and then re-mixed with water by spraying it in an oven in 50-150 wt.% Of the waste mass, and solid decomposition products are irrigated with water in an amount of 10-20% by weight of rubber waste. As water, condensate is used, which is obtained by separation from the liquid phase.

The disadvantages of this method are:

1. High energy costs due to the need to heat and evaporate a significant amount of water (about 150% of the waste mass), as a result of which the processing time is increased in comparison with the known pyrolysis technologies for waste processing, which, in turn, leads to an increase in heat losses from the reactor.

2. Large emissions of harmful products of fuel combustion into the environment due to the long exposure of waste in the furnace for their complete processing, which is associated with the need not only to heat the waste itself, but also to heat and evaporate a large amount of water.

3. The high water content in liquid products, as well as the high content of harmful components (sulfur, unsaturated hydrocarbons, ash) in solid products of processing, which requires additional purification of these products from water and harmful compounds.

A known method of processing used tires (see patent of the Republic of Belarus No. 11589, publ. 30.08.2008).

A method for processing used tires involves pyrolyzing them in a reactor, producing a hydrocarbon-containing gas and solid carbon-containing material, removing solid carbon-containing material from the reactor, supplying the hydrocarbon-containing gas to the filter reactor, treating it with a coolant, releasing non-condensable gas and burning it.

Solid carbon-containing material is fed into a gasification reactor, where water gas and ash are obtained by filtering superheated water vapor through a layer of material at 800–900 ° С; one part of water gas is used as a heat carrier, which is supplied to the filter reactor at 400–600 ° C is mixed with a hydrocarbon-containing gas at their mass ratio (0.2-1.0): 1, another part of the water gas is mixed with water vapor at a mass ratio of 1: (1-10) and fed to the reactor in an amount of (0.20 -0.62) kg per 1 kg of tires, and the remainder of the water gas is burned in a steam generator d I receive water vapor, the ash is granulated to a particle size of 3-30 mm and used as filling in a filter reactor, from the mixture of water and hydrocarbon-containing gases obtained in the reactor filter, a bitumen fraction with a boiling point of 300-390 ° C is first extracted, which fed into the reactor in an amount of 0.05-0.1 kg of bitumen fraction per 1 kg of worn tires, and then a fraction with a boiling point of 190-299 ° C, which is burned in a steam generator to produce water vapor.

The disadvantages of this method include:

1. High energy consumption for overheating water vapor to a temperature of 800-900 ° C, as well as high energy costs for heating the gasification reactor and filter reactor.

2. Large emissions into the environment of the products of combustion of fuel spent on heating the gasifier reactor and overheating of water vapor.

3. The low quality of the obtained liquid products (bitumen fraction and fraction with a boiling point of 80-189 ° C) of waste processing due to the presence of sulfur and water compounds.

A known method and device for processing rubber waste (see patent of the Russian Federation No. 2356731, publ. 27.05.2009, bull. No. 15). The method includes pyrolysis of waste in a reactor in a coolant medium, separation of the pyrolysis products into gaseous and solid phases, cooling of the solid phase by supplying water, separation from the gaseous phase by condensation of the liquid phase and burning of the gaseous phase to heat the heat carrier in the heat exchanger. The solid fraction is fed to the mill, where water is simultaneously sprayed to carry out wet grinding to obtain a suspension, and the first and second fractions of the liquid phase are isolated from the gaseous fraction by condensation, and then water is extracted from the second fraction, and the first fraction is mixed with the suspension and by excitation of cavitation the mixture is subjected to mechanochemical activation. After separation of the second fraction of the liquid phase, a part of the gaseous phase is burned, and the rest of the gaseous phase is mixed with superheated water vapor and used as a coolant. As water to obtain a suspension, water extracted from the second fraction is used.

The disadvantages of this method include:

1. High energy consumption for the waste recycling process due to the low energy efficiency of cavitation used to process products in order to improve their quality indicators, as well as the high consumption of electric energy necessary for the operation of a special pump that provides coolant circulation.

2. Low quality indicators of the resulting fuel suspension due to the increased water content, which does not allow the use of this fuel at negative temperatures due to freezing of water and delamination of the suspension.

A known method of processing organic waste and a device for processing organic waste (see patent of the Russian Federation No. 2422478, publ. 04/27/2011). A method of processing organic waste includes feeding the waste into the reactor, thermolizing it in the reactor in a coolant medium passing through the waste layer to form a gaseous and solid phases, withdrawing the gaseous phase from the reactor, cooling it, separating the liquid phase condensed by cooling the gaseous phase, burning non-condensed gaseous phase, withdrawal of the solid phase from the reactor at the end of the thermolysis process, its cooling, unloading of the solid phase from the container and its magnetic treatment, while as heat the carrier use a gaseous mixture of combustion products entering the heat exchanger and air in the reactor, the heat carrier is heated to 750-1150 ° C and passed through the waste layer at a speed of 2-25 m / s at a pressure in the reactor of 0.1-1.0 MPa .

The disadvantages of the method are:

1. High energy consumption due to the need to heat the coolant to 1150 ° C and the absence of a heat recirculation system (return to the waste recycling process).

2. Emissions of harmful substances into the environment as a result of the burning of the non-condensed gaseous phase.

3. The low quality of liquid (containing a large amount of water) and solid products (containing a large amount of ash) waste recycling.

Closest to the claimed invention is the method and device adopted by us for the prototype rubber waste processing (see application PCT / RU 2007/000392. Publication 13.03.2008. International publication number WO 2008/030137 A1).

A method for processing rubber waste includes feeding 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 to form a gaseous and solid phases, withdrawing the gaseous phase from the reactor, returning part the gaseous phase into 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 chamber, unloading the solid phase when turning the container relative to the longitudinal axis, grinding the solid phase to a particle size 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 liquid and solid phases in the mixer at a mass ratio (0.75-1.50): 1, circulating the mixture through the mixer using a dispersing pump for 600-3600 s, burning the non-condensed gaseous phase to heat water vapor in t ploobmennike, followed by repeating the process, wherein the waste feed to the reactor in a mobile container is carried from the second loading / unloading chamber and the container at the end of the thermolysis reactor is transferred from reactor to a second load / unload chamber. Thermolysis is carried out at a mass ratio of water vapor and gaseous phase in the mixture equal to 1: (1.0-5.0). Part of the water is separated from the liquid phase to its content in the liquid phase in the range of 5-18 wt.%.

The disadvantages of this method are:

1. High energy consumption for the waste recycling process due to heat losses during the supply of coolant from the reactor through pipelines to the fan, which should be maintained at a high temperature, which prevents condensation of part of the coolant directly in the fan and clogging of it with condensate.

2. Large emissions of harmful gaseous substances into the environment that are contained in the products of combustion of fuel burned to heat the reactor and overheat a large amount of water vapor.

3. The low quality of the resulting products (fuel dispersion) due to the presence of a significant amount of water (the presence of water reduces the specific heat of combustion and makes it impossible to store this fuel at low temperatures), increased ash content (ash is contained in large quantities in the solid phase).

The objective of the invention is to reduce the energy costs of processing rubber waste, reducing harmful emissions into the environment and improving the quality of waste products.

The problem is solved in that the method of processing rubber waste, including feeding waste into the reactor in a mobile container from the first chamber, thermolysis of it in the reactor in a coolant medium, passed through the waste layer, with the formation of a gaseous and solid phases, the withdrawal of the gaseous phase from the reactor, the conclusion the solid phase from the reactor by moving the container with the solid phase from the reactor at the end of the thermolysis process into the first chamber, unloading the solid phase and its electromagnetic treatment, isolating the liquid phase from the gas by cooling it, separating water from the liquid phase, burning the gaseous phase, then repeating the process in which waste is fed into the reactor in a mobile container from the second chamber, and the container is transferred from the reactor to the second chamber at the end of the thermolysis process, according to the invention, liquid fuel is burned and saturated water vapor is obtained with a temperature of 105 ° C., water vapor is pumped through a heat exchanger and a waste layer in a container in a closed loop, excess growth is pressured In the reactor, it is prevented by partial removal of water vapor and condensation by cooling it with water, the air that is filtered through the waste layer is displaced from the waste layer with water vapor, and then the air is displaced from the reactor by the steam flow, since the air does not condense, it is used to burn fuel, output water vapor in a mixture with air is carried out until the air concentration in the reactor decreases to the content necessary to prevent oxidation of the decomposition products of waste - their burning in the reactor re - in this way the reactor is blown with water vapor to remove air, the steam withdrawal from the reactor is stopped when the air content is reduced to a predetermined one, at which it is impossible to ignite the decomposition products in the reactor, at the same time the steam supply to the heat exchanger is stopped, liquid fuel is burned, the fuel combustion products are heated by water steam, then the combustion products are cooled to 150 ° C by a stream of air, after that the combustion products are removed, the waste is heated by heat, and the process of thermal decomposition of rubber from strokes, as a result of which gaseous and solid phases are formed, the gaseous phase is mixed with circulating water vapor and a gas-vapor mixture is created so that the pressure in the reactor is constant, part of the water vapor with the gas-vapor mixture is removed from the reactor, to control the exact time of completion of the process of thermal decomposition of waste, control the content of the gaseous phase of the decomposition of tires in the vapor-gas mixture, the moment of completion of the process of thermal decomposition of waste corresponds to the time when the content of the gaseous phase in a gas-vapor mixture will decrease to almost zero, i.e. almost pure water vapor starts to come out of the reactor, the gas-vapor mixture is cooled and a liquid phase is obtained, from which water is separated and accumulated, this water contains dissolved organic substances - waste decomposition products, this polluted water is used to produce combustible gas that is used for energy supply waste treatment process, the liquid phase is accumulated after water is isolated, the gaseous phase after the liquid phase is separated is partially burned in a mixture with liquid fuel, and partially simply burned, which prevents its release into the environment and at the same time reduces fuel consumption for the processing process, when the moment of termination of the release of gaseous products is reached, water is sprayed over a layer of solid residue in the container, it cools it, evaporates itself, and the resulting water vapor is mixed with the products decomposition of waste is fed to the reactor when the temperature of cooling the solid phase in the container reaches T = 110 ° C, at which the solid decomposition phase of the tires is not ignited in the open air, spraying the odes are stopped, then the solid phase is broken, the metal cord is separated from it, they are electromagnetically separated, the metal is pressed into briquettes, and the solid phase is accumulated, the solid phase is ignited and a burning layer is created, the solid phase and water are supplied in such a quantity that the mass the amount of the solid phase and water was 1: (0.5-1.0), a mixture of the solid phase and water is created in the vessel, a layer of the solid phase is created, in the lower part of which the overlying layers of the solid phase are heated - above the combustion layer, thus reversal gasification process, in which the solid phase impregnated with water and air are supplied from above, and the resulting combustible gas is discharged from below, water evaporates in the upper part of the solid phase layer by heating and water vapor is formed, which is mixed with the supplied air and fed into the gasification zone where the reaction of water vapor interaction with solid phase carbon to produce a combustible gas containing mainly hydrogen and carbon monoxide, as well as a certain amount of methane and resins, a mixture of gases and resins from the gasification zone is fed into the combustion zone of the solid phase, is conducted through this zone and removed from it, the ash formed is accumulated, in the combustion zone of the solid phase the temperature is 1000 ° C and higher, therefore, in this zone the gas is cleaned of resins and organic components, which decompose under high temperature to low-molecular compounds - methane, ethylene and others, thus enriching combustible gas with gaseous components with a high specific heat of combustion, such a gas practically does not contain resinous compounds and therefore does not form when it is burned tsya noxious compounds and carbon black in a weight ratio of the solid phase and the water less than 1: 0.5, i.e. less than 0.5 water per one kg of solid phase, the amount of water vapor generated will not be sufficient for the reaction C + H ₂ O = CO + H ₂ to occur, therefore, part of the carbon in the solid phase will not enter the gas formation reaction, but will burn in the combustion zone with the formation of non-combustible gas СО ₂ , which mixes with combustible gas from the gasification zone, which ultimately leads to a decrease in the specific heat of combustion of combustible gas, when the mass ratio of the solid phase and water is more than 1: 1, the heat consumption for water evaporation increases significantly, a large amount of water vapor, which leads to a sharp decrease in temperature in the gasification zone, because the gasification zone is cooled by excess water vapor, and to stop the flow of gasification reactions, i.e. in this case, the formation of combustible gases is sharply reduced, therefore, in order to efficiently obtain combustible gases from the solid phase, the mass content of water in the solid phase must be maintained within the range of 1: (0.5-1.0), and at the same time the gasification process starts, gas withdrawal is stopped and gas - a mixture of solid phase combustion products, hydrogen, carbon monoxide and tar decomposition products - the combustible gas is mixed with the gaseous phase of the waste decomposition products after the liquid phase is separated from it at their mass ratio of 1: (0.1-0.5), at mixing gas shaped phase with the fuel gas which contains carbon monoxide and hydrogen, the reduction reaction is carried out - the hydrogenation of unsaturated compounds, i.e., a reduction in the mixture of unsaturated compounds, which allows you to burn this mixture without the formation of toxic compounds in the combustion products, the formation of a mixture of combustible gas and gaseous phase with a mass ratio of less than 1: 0.1 leads to the fact that the reaction of interaction of hydrogen and carbon monoxide with unsaturated compounds of gaseous the phases practically do not proceed, and the combustion of such a mixture leads to increased emissions of harmful substances into the atmosphere, the formation of a mixture of combustible gas and a gaseous phase with a mass ratio of more than 1: 0.5 leads to the fact that the mixture also disrupts the reaction of interaction of hydrogen and carbon monoxide with organic compounds of the gaseous phase, resulting in the combustion of such a mixture also leads to increased emissions of harmful substances into the environment, thus, for the environmentally friendly burning of a mixture of combustible gases and of the gaseous phase, the mass content of these products must be maintained within the range of 1: (0.1-0.5), part of the mixture is burnt to produce working water vapor, and the remainder of the mixture is burnt, resulting products Combustion tubes are used to heat the reactor and coolant, the liquid phase contains low-boiling products similar to high-octane gasolines, as well as products similar to diesel fuel, thus, high-quality products are obtained from the liquid phase, and the fraction with a flash point of 35–40 ° C, which is cooled, condensed, and accumulated; the remainder, the liquid phase with a flash point of 61–85 ° C, is also accumulated; the flash temperature is monitored and adjusted due to the time spent a distillation assay, while the amount of combustion products removed for distillation is controlled so that the distillation temperature remains equal to 90-100 ° C, during the liquid phase distillation process, its flash point rises and when the flash temperature reaches 61-85 ° C, liquid distillation the phases stop and the residue accumulates, in this case the formed fraction, which is condensed, has a flash point in the range of 35-40 ° C, which corresponds to the kerosene-gas oil fraction and can be used as in co-sorted fuel, for example, for gas turbine engines, a liquid with a flash point of 61-85 ° С corresponds to diesel fuel in its indicators and can be used as fuel for diesel engines, the combustion products that are formed when a mixture of combustible gases and gaseous phase are burned are used for heating and distillation of the liquid phase, which reduces the consumption of additional fuel for the distillation process, the solid phase in the container after completion of the thermal decomposition of the waste is cooled, sprayed with water, about the boiling steam is discharged into the reactor, the products of fuel combustion are released into the atmosphere, the products of combustion have an average specific heat capacity of Cp = 1.24 kJ / ° C and their cooling from 1000 ° C to 400 ° C at a flow rate of G = 0.269 kg / s or 968 kg / h provides heat input to the reactor:

Q = Cp · G (1000 ° С-400 ° С) = 1.24 kJ / kg ° С × 0.269 kg / s · 600 ° С = 200 kJ / s = 200 kW, the temperature in the reactor rises, the waste heats up and at when the temperature reaches 300 ° С - this temperature is different for different types of waste - the process of thermal decomposition of the waste begins, as a result of which gaseous and solid products are formed, the pressure in the reactor is kept constant at 2 atm, which is important for the process of thermal decomposition and product formation decomposition of constant composition throughout the process, and pressure fluctuations in the reactor will inevitably lead to changes in the composition of the gaseous phase, - after cooling, the solid phase is crushed (broken), then the processing cycle is repeated, which confirms the compliance of the claimed invention with the patentability criteria “novelty” and “prior art”.

It is important that the liquid phase after separation of water is separated by distillation at a temperature of 90-100 ° C into a fraction with a flash point of 61-85 ° C and a fraction with a flash point of 35-40 ° C.

It is significant that the combustion products after heating the reactor and coolant are used to heat the liquid phase and separate it by distillation.

The drawing shows a General view of the device, which implements a method of processing rubber waste.

The device comprises a drive 1 connected to a conveyor belt 2 and a loading hopper 3; loading chamber 4; slide gate 5; container 6; actuator 7 connected to the shutter 8; a feeding device 9 of the container 6 into the reactor 10; nozzle 11; a pipe 12 connected to a heat exchanger 13; belt conveyor 14 connected to the loading hopper 15; loading chamber 16; slide gate 17; container 18; capacity with fuel 19; a steam generator 20; flow meter 21; gas blower 22; a flow meter 23 connected to a capacitor 24; crane 25; gas analyzer 26; flow meter 27; burner 28; smoke exhaust 29; shirt 30; crane 31; heat exchanger 32; chimney 33; temperature sensor 34; pressure sensor 35; a crane 36 connected to the separator 37; a crane 38 connected to the drive 39; a crane 40 connected to the storage tank 41; crane 42; an actuator 43 connected to the gate 44; feeder 45; flow meter 46; a pump 47 connected to the nozzles 48; valve 49; temperature sensor 50; swivel mechanism 51; conveyor 52; engine 53; roll mill 54; electromagnetic separator 55; press 56; drive 57; screw conveyor 58 connected to a gas generator 59; blower 60; crane 61; a weight batcher 62 connected to a container 63; flow meter 64; pump 65; screw conveyor 66; level sensor 67; drive 68; flow meter 69; mixer 70; flow meter 71; regulator valve 72; a valve 73 connected to a distiller 74; heat exchanger 75 with valve 76; storage tanks 77 and 78; temperature sensor 79; a device for determining a flash point of 80; crane 81; a valve 82 connected to nozzles 83; temperature sensor 84; valve 85; smoke pipe 86; rotary mechanism 87; conveyor 88; engine 89; branch pipe 90.

According to the invention, the processing of rubber waste is as follows.

From the drive 1, filled with crushed rubber waste, such as crushed worn tires, using the belt conveyor 2, waste is fed to the loading hopper 3 mounted on the loading chamber 4 with the shutter gate 5 closed. After that, the slide gate 5 is opened and the waste is poured under the influence of its own weight into the container 6. The waste feeding operation is repeated until the container 6 is fully loaded. After that, the shutter 8 is opened using the drive 7 and the feeding device 9 moves the container 6 from the loading chamber 4 to the reactor 10 The container 6 is installed so that the pipe 11 of the container 6 is connected to the pipe 12 of the heat exchanger 13. The shutter 8 is closed.

From the drive 1 with the help of the conveyor belt 14, waste is fed into the loading hopper 15 mounted on the loading chamber 16 with the shutter gate 17 closed. After that, the slide gate 17 is opened and the waste is poured into the container 18 under the influence of its own weight. The container 18 is completely loaded with waste.

From the tank 19, liquid fuel is supplied to the steam generator 20, it is burned and saturated steam is obtained with a temperature of 105 ° C. The resulting steam through a flow meter 21 with a given flow rate is fed into a shell-and-tube heat exchanger 13 (hereinafter referred to as the heat exchanger). Simultaneously with the supply of steam to the heat exchanger 13, a gas blower 22 is turned on and water vapor is pumped through the heat exchanger 13 and the waste layer in the container 6 in a closed loop. In order to prevent excessive pressure buildup in the reactor 10 as a result of steam supply, the flow meter 23 is opened and partially steam is diverted to the condenser 24, condensed by water cooling.

Water vapor filtered through the waste layer displaces air from the waste layer into the reactor and then, with the steam stream, the air from the reactor is displaced into the condenser 24. Since the air does not condense, it is supplied through the valve 25 to the steam generator 19 and used to burn fuel. The output of water vapor in the mixture with air into the condenser 24 is carried out until the air concentration in the reactor 10 decreases to a predetermined content, which is necessary to prevent oxidation of the decomposition products of the waste (their combustion in the reactor). Thus, the reactor is blown with steam to remove air.

The air content in the reactor is controlled by the readings of the gas analyzer 26 and when the air content is reduced to a predetermined one, in which it is impossible to ignite the decomposition products in the reactor 10, the steam output to the condenser is stopped by closing the valve 23. At the same time, the steam supply from the steam generator to the heat exchanger 13 is stopped (the valve is closed) flowmeter 21).

From the tank 19 through the flow meter 27 to the burner 28, connected to the casing of the heat exchanger 13, liquid fuel is fed and burned. The resulting combustion products enter the casing of the heat exchanger 13 and then, using a smoke exhauster 29, the combustion products from the casing of the heat exchanger 13 are led into the jacket 30 of the reactor 10 and then into the chimney 33.

Flowing through the casing of the heat exchanger 13, the fuel combustion products heat the water vapor flowing through the pipes of the heat exchanger 13, and then enter the jacket 30 of the reactor 10 and then through the valve 31 are discharged to the heat exchanger 32, in which the combustion products are cooled to 150 ° C by a stream of air that is supplied into a steam generator and into a burner 28 for burning fuel. After this, the products of combustion are discharged into the chimney 33.

Thus, the heat of the combustion products is transferred to the reactor not only with a stream of heated water vapor, but also through the wall of the jacket 30.

As a result of heat supply (with steam flow and through the wall of the jacket 30), the temperature in the reactor rises, the waste heats up and when a certain temperature is reached (for different types of waste this temperature is different), which is controlled by the temperature sensor 34, the process of thermal decomposition of rubber waste begins as a result of which gaseous and solid phases are formed.

The gaseous phase is mixed with the circulating water vapor and a vapor-gas mixture is formed. Since the amount of circulating water vapor does not change, and the gaseous phase of the decomposition of waste is continuously released, the pressure in the reactor 10 begins to increase, which is monitored by the pressure sensor 35. When a certain pressure is reached, the flow meter 23 is opened and a part of the gas-vapor mixture is removed from the reactor 10 a condenser 24. In this case, the amount of steam-gas mixture discharged by the flow meter 23 is controlled so that the pressure in the reactor is constant. Simultaneously with the removal of the gas-vapor mixture from the reactor using a flow meter 21 from the steam generator 20, water vapor is supplied to the heat exchanger 13, since part of the water vapor with the gas-vapor mixture is removed from the reactor.

The content of the gaseous phase of the decomposition of tires in a gas-vapor mixture is controlled by the readings of a gas analyzer 26, which is necessary for accurate determination of the time for completion of the process of thermal decomposition of waste. After this, the products of combustion are discharged into the chimney 33.

The moment of completion of the process of thermal decomposition of waste corresponds to the time when the content of the gaseous phase in the vapor-gas mixture decreases to almost zero, i.e. almost pure water vapor begins to leave the reactor.

As a result of cooling the gas-vapor mixture in the condenser 24, a liquid phase is formed, which is fed through a tap 36 to a separator 37, where water is separated from the liquid phase and fed through a tap 38 to a storage tank 39. This water contains dissolved organic substances (waste decomposition products) and therefore cannot be returned back to the steam generator to produce working water vapor. Known purification systems for such water are technically complex (water must be cleaned in several stages), energy-intensive and secondary waste (sludge) is generated during cleaning, which must also be disposed of.

The present invention proposes the use of contaminated water from the accumulator 39 to obtain combustible gas, which is spent on energy supply of the waste processing process.

The liquid phase after the allocation of water from the separator 37 through the valve 40 is fed into the storage tank 41.

The gaseous phase after the liquid phase is separated from the condenser 24 through the valve 25 is partially fed into the steam generator 19 and burned in a mixture with liquid fuel, and the gas phase is partially fed through the valve 42 to the burner 28 and burned. At the same time, using a flow meter 27, the liquid fuel supply from the tank 19 to the burner 28 is reduced. The combustion of the gaseous phase prevents its release into the environment and at the same time reduces the fuel consumption for the processing process.

Upon reaching the moment of termination of the release of gaseous products using the actuator 7, the shutter 8 is opened and the supply device 9 moves the container 6 from the reactor 10 to the loading chamber 3. Then, the shutter 7 is closed. With the help of the actuator 43, the shutter 44 is opened and with the supply device 45, the container 18 from the loading chamber 16 is fed into the reactor 10. The container 18 is installed so that the pipe 90 of the container 18 is connected to the pipe 12 of the heat exchanger 13. Then the shutter 44 is closed.

After the container 6 is led into the loading chamber 3 from the drive 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 6. Water enters the solid residue and cools it, and it evaporates and forms water vapor in the mixture with waste decomposition products through the valve 49 leaves the loading chamber 3 into the reactor 10.

In this case, the contaminated water evaporates and a mixture is formed, which contains mainly water vapor and the evaporated waste decomposition products that were in the dissolved water. This gaseous mixture is returned to the reactor 10, i.e. is not released into the environment.

The cooling temperature of the solid phase in the container 6 is controlled according to the testimony of the temperature sensor 50 and after reaching T = 110 ° C, at which the solid phase decomposition of the tires is not ignited in the open air, water spraying is stopped.

Using the rotary mechanism 51, the container 6 is rotated and set upside down, as a result of which the solid phase falls out of the container 6 under the influence of its own weight onto the conveyor belt 52, which is driven by the motor 53, and the solid phase is fed to the roller mill 54. After unloading, the container 6 is installed in the working position (bottom part down) and load it, as described above.

In the roll mill 54, the solid phase, passing through the rolls, is milled, as a result of which the metal cord is separated from the solid phase of the decomposition of waste. After the roll mill 54, the solid phase and the metal cord are fed to an electromagnetic separator 55, in which the metal is separated from the solid phase. The metal is fed to a press 56 and pressed into briquettes, and the solid phase is fed to a storage 57.

From the drive 57 by means of a screw conveyor 58 into the gas generator 59, a solid phase is loaded in an amount to the solid phase in the gas generator so that the solid phase in the gas generator does not exceed 0.1 times the diameter of the gas generator shaft in height. The solid phase is ignited on the grate of the gas generator and a burning layer is created. To maintain the combustion process of the solid phase on the grate using the blower 60, air is supplied to the gas generator from above, and the combustion products are removed from under the gas generator lattice through the faucet 61 into the chimney 33.

Next, from the drive 57 through the weighing batcher 62 into the tank 63 is loaded in a predetermined amount of the solid phase. From the drive 37 through the flow meter 64 using the pump 65 in the tank 63 serves a predetermined amount of water. The solid phase and water are fed into the tank in such an amount that the mass amount of the solid phase and water is 1: (0.5-1.0).

The solid phase has a porous structure and is well impregnated with water, so a mixture of the solid phase and water (water-impregnated particles of the solid phase) is created in the tank.

From the vessel 63, the solid phase impregnated with water by means of a screw conveyor 66 is loaded into the gas generator 59 in an amount so that the layer of the solid phase along the height of the shaft of the gas generator 59 is within (2-3) D (D is the diameter of the shaft of the gas generator), which is controlled by the sensor level 67.

Thus, a solid phase layer is formed in the gas generator 59, in the lower part (on the grate) of which the combustion process proceeds, as a result of which heat is generated, due to which the overlying layers of the solid phase are heated (above the combustion layer).

In the gas generator 59, a reversed gasification process is carried out in which a solid phase impregnated with water and air are supplied to the gas generator shaft from above, and the resulting combustible gas from the gas generator is removed from below (from under the grate).

In the upper part of the solid phase layer, water evaporates due to heating and water vapor is formed, which mixes with the supplied air and enters the lower part of the gas generator, i.e. in the gasification zone, where the reaction of water vapor interaction with the carbon of the solid phase with the formation of a combustible gas containing mainly hydrogen and carbon monoxide, as well as some methane and resins.

The mixture of gases and resins from the gasification zone enters the combustion zone of the solid phase layer on the grate, passes through this zone and enters the outlet of the gas generator.

As a result of combustion and gasification processes, the solid phase layer is lowered through the shaft of the gas generator (sags) and therefore, the solid phase is continuously fed into the gas generator from the tank 63 using the screw conveyor 66 in such a quantity that its level in the gas generator shaft remains constant, which is controlled by the sensor level 67. The ash formed in the gas generator is discharged into the storage device 68.

In the combustion zone of the solid phase, the temperature is 1000 ° C and higher, therefore, when a mixture of gases and resins passes through this zone, the gas is purified from resins and organic components, which decompose under the influence of high temperature to low molecular weight compounds (methane, ethylene, etc.). Thus, the combustible gas is enriched with gaseous components with a high specific heat of combustion. Such gas practically does not contain resinous compounds and therefore, when it is burned, harmful compounds and soot are not formed (see S.D. Fedoseev, A.B. Chernyshov. Semi-coking and gasification of solid fuels. - M.: State Scientific and Technical Publishing House of Petroleum and mining and fuel literature, 1960. - p.131-133).

If the mass ratio of the solid phase and water is less than 1: 0.5 (i.e., less than 0.5 kg of water per one kg of the solid phase), the amount of water vapor generated (water vapor is formed by evaporation of the remaining water in the pores) will be insufficient for reaction progress: C + H ₂ O = CO + H ₂ . Therefore, part of the carbon in the solid phase will not enter the gas generation reaction, but will burn in the combustion zone to form non-combustible gas (CO ₂ ), which will mix with the combustible gas from the gasification zone, which will ultimately lead to a decrease in the specific heat of combustion of the combustible gas.

When the mass ratio of the solid phase and water is more than 1: 1, the heat consumption for water evaporation increases significantly, a large amount of water vapor is formed, which leads to a sharp decrease in temperature in the gasification zone (the gasification zone is cooled by excess water vapor) and to the termination of gasification reactions, t .e. in this case, the formation of combustible gases is sharply reduced.

Thus, in order to efficiently obtain combustible gases from the solid phase, it is necessary to maintain the mass content of water in this phase in the range of 1: (0.5-1.0).

Simultaneously with the start of the gasification process, the valve 61 is closed, as a result of which the gas flow from the gas generator to the chimney 33 is stopped, the flow meter 69 and gas (a mixture of solid phase combustion products, hydrogen, carbon monoxide and tar decomposition products - combustible gas) are opened the mass flow rate is fed into the mixer 70, where through the tap-flow meter 71 with a given mass flow rate the gaseous phase of the waste decomposition products is fed after the liquid phase is separated from it. In this case, the mass ratio of combustible gas to the gaseous phase is set within 1: (0.1-0.5).

In the mixer, a mixture of combustible gas obtained in the gas generator 59 and the gaseous phase of the waste decomposition products after separation of the liquid phase from it is obtained.

The gaseous phase of the decomposition products of rubber waste contains aromatic, unsaturated and other high molecular weight hydrocarbons, the direct combustion of which (direct combustion of gaseous decomposition products) requires the use of special burner devices, and also leads to the formation of harmful substances in the combustion products.

Mixing the gaseous phase with a combustible gas (contains carbon monoxide and hydrogen) leads to the occurrence of reduction reactions (hydrogenation of unsaturated compounds), i.e. reduction in the mixture of unsaturated compounds, which allows you to burn this mixture without the formation of toxic compounds in the combustion products, as well as using standard burner devices.

The formation of a mixture of combustible gas and a gaseous phase with a mass ratio of less than 1: 0.1 leads to the fact that reactions of interaction of hydrogen and carbon monoxide with unsaturated compounds of the gaseous phase practically do not occur, and the combustion of such a mixture leads to increased emissions of harmful substances into the atmosphere. The formation of a mixture of combustible gas and a gaseous phase with a mass ratio of more than 1: 0.5 leads to the fact that the mixture also disrupts the reaction of hydrogen and carbon monoxide with organic compounds of the gaseous phase, as a result of which the combustion of such a mixture also leads to increased emissions of harmful substances into the environment.

Thus, for the environmentally friendly burning of a mixture of combustible gases and the gaseous phase, it is necessary to maintain the mass content of these products in the range of 1: (0.1-0.5).

From the mixer 70, through the control valve 72, part of the mixture is supplied to the steam generator 20 and burned to produce working water vapor, and the remainder of the mixture is burned in a burner 28 connected to the casing of the heat exchanger 13. The resulting combustion products are used to heat the reactor and heat carrier. This eliminates the use of additional fuel for waste processing, and it is also useful to use the gaseous phase of the decomposition products.

The liquid phase of the decomposition products of rubber waste has a low flash point (about 30-37 ° C), a high content of aromatic and unsaturated hydrocarbons and cannot be used as fuel. At the same time, the liquid phase contains low-boiling products similar to high-octane gasolines, as well as products similar to diesel fuel. Thus, high-quality products can be obtained from the liquid phase.

From the storage tank 41, the liquid phase through the valve 73 is fed to the distiller 74, where at a temperature of 90-100 ° C, a fraction with a flash point of 35-40 ° C is isolated from the liquid phase, which is condensed by cooling in the heat exchanger 75 and poured into the storage via the valve 76 capacity 77, and the remainder (liquid phase with a flashpoint of 61-85 ° C) from the distiller 74 is poured into the storage tank 78. In this case, the temperature in the distiller is controlled by the readings of the sensor 79, and the flash temperature is controlled by the readings of the device 80 and the given temperature is controlledcounting the time of the distillation process.

In this case, the amount of combustion products that are removed from the jacket 30 to the jacket of the distiller 74 is controlled by a valve 81 so that the temperature in the distiller remains equal to 90-100 ° C.

During the process of distillation of the liquid phase, its flash point increases, and when the flash temperature reaches 61-85 ° C, the distillation of the liquid phase is stopped and the residue is poured into a container 78. In this case, the formed fraction, which is condensed in the heat exchanger 75, has a flash point of limits 35-40 ° C. A liquid with a flash point of 35–40 ° C corresponds to the kerosene-gas oil fraction and can be used as high-grade fuel, for example, for gas turbine engines. A liquid with a flash point of 61-85 ° С corresponds to diesel fuel in its parameters and can be used as fuel for diesel engines.

The products of combustion, which are formed by burning a mixture of combustible gases and a gaseous phase in the burner 28, after exiting the jacket 30 of the reactor 10 through the valve 81 are sent to the jacket of the distiller 74 and use their thermal energy to heat and distill the liquid phase. This allows you to use the thermal energy of the combustion products, which reduces the consumption of additional fuel for the distillation process.

Similarly carry out the process of processing rubber waste, which are located in the container 18, installed in the reactor 10.

After the thermal decomposition of the waste in the container 18 is completed, the shutter 44 is opened using the actuator 43 and the container 18 is withdrawn from the reactor 10 into the loading chamber 16 using the feeding device 45.

To cool the solid phase in the container 18 from the accumulator 39, water is supplied to the nozzles 83 through the valve 82 and sprayed over the solid phase in the container 18, as a result of which the container and the solid phase are cooled, the cooling temperature is controlled by the temperature sensor 84. The generated vapor from the chamber 17 enters the reactor 10 through the valve 85. The products of fuel combustion in the steam generator 18 through the smoke pipe 86 are released into the atmosphere.

After cooling using the rotary mechanism 87, the container 18 is rotated and set upside down. The solid phase from the container 18 falls out onto the conveyor 88, which is driven by a motor 89 and the solid phase is fed into the roller mill 54.

The invention is illustrated by the following examples.

Example 1

From the drive 1, filled with crushed rubber waste, for example, crushed worn tires to a particle size of 100 mm, using the conveyor belt 2, the hopper 3 is installed on the loading chamber 4 with the shutter gate 5 closed, the waste is fed until the hopper is filled. In our case, the weight of the waste in hopper 3 is 200 kg. After that, the slide gate 5 is opened and the waste is poured into the container under the influence of its own weight 6. The waste supply operation is repeated until the container 6 is fully loaded. When the container 6 is fully loaded, the waste weight is 1000 kg. After that, using the actuator 7, open the shutter 8 and the feeder 9, the container 6 is moved from the loading chamber 3 to the reactor 10. The container 6 is installed so that the pipe 11 of the container 6 is connected to the pipe 12 of the heat exchanger 13. The shutter 8 is closed.

From the drive 1, using a conveyor belt 14, waste is fed to the loading hopper 15 mounted on the loading chamber 16 with the gate shutter 17 closed until the hopper 15 is filled. In this case, the weight of the waste in the loading hopper is 200 kg. After that, the slide gate 17 is opened and the waste is poured into the container 18 under the action of its own weight.

The loading operation is repeated 5 times and the container 18 is completely loaded with waste weighing 1000 kg.

From the tank 19, liquid fuel is supplied to the steam generator 20 with a flow rate of 10 kg / h (specific heat of combustion of the fuel is 40 MJ / kg), it is burned and saturated water vapor is obtained with a temperature of 130 ° C. in an amount of 75 kg / h. The resulting steam through a flow meter 21 with a flow rate of 75 kg / h is fed into a shell-and-tube heat exchanger 13 (hereinafter referred to as the heat exchanger). Simultaneously with the supply of steam to the heat exchanger 13, a gas blower 22 is turned on and water vapor is pumped through the heat exchanger 13 and the waste layer in the container 6 in a closed loop. In order to prevent excessive pressure buildup in the reactor 10 as a result of steam supply, the flow meter 23 is opened and steam with a flow rate of 75 kg / h is discharged to the condenser 24, where it is condensed by cooling with water.

Water vapor filtered through the waste layer displaces air from the waste layer into the reactor and then, with the steam stream, the air from the reactor is displaced into the condenser 24. Since the air does not condense, it is supplied through the valve 25 to the steam generator 19 and used to burn fuel. The withdrawal of water vapor in a mixture with air into the condenser 24 is carried out until the air concentration in the reactor 10 decreases to 10 wt.%, Which is necessary to prevent oxidation of the decomposition products of the waste (their combustion in the reactor).

The air content in the reactor is controlled by the readings of the gas analyzer 26 and, when the air content is reduced to 10 wt.%, The steam output to the condenser is stopped by closing the valve 23. At the same time, the steam supply from the steam generator to the heat exchanger 13 is stopped (the flow meter 21 is closed).

From the tank 19 through the flow meter 27 to the burner 28 connected to the casing of the heat exchanger 13, liquid fuel is supplied with a flow rate of 70 kg / h and burned. The resulting combustion products with a flow rate of 968 kg / h (13.83 kg of combustion products are formed when 1 kg of fuel is burned) enter the casing of the heat exchanger 13 and then with the help of a smoke exhauster 29, the combustion products from the casing of the heat exchanger 13 are removed to the jacket 30 of the reactor 10 and then to the smoke pipe 33.

Flowing through the casing of the heat exchanger 13, the fuel combustion products heat the water vapor flowing through the pipes of the heat exchanger 13 to a temperature of 600 ° C, which from the heat exchanger enters the waste layer, transfers heat to the waste and again enters the heat exchanger. The combustion products passing through the casing of the heat exchanger 13 are cooled from 1000 ° C to 600 ° C (the heat of the combustion products is transferred to water vapor) and then enter the jacket 30 of the reactor 10, cooled and, at a temperature of 400 ° C, are discharged through a valve 31 to the heat exchanger 32, in which the combustion products are cooled to 150 ° C by a stream of air, which is supplied to the steam generator and to the burner 28 for burning fuel. After this, the products of combustion are discharged into the chimney 33.

The heat of the combustion products is transferred to the reactor not only with a stream of heated water vapor, but also through the wall of the jacket 30.

The combustion products have an average specific heat capacity of Cp = 1.24 kJ / s ° C and their cooling from 1000 ° C to 400 ° C at a flow rate of G = 0.269 kg / s or 968 kg / h provides a supply to the reactor (with water vapor and through shirt wall 30) amount of heat:

Q = CpG (1000 ° C-400 ° C) = 1.24 kJ / kg ° C 0.269 kg / s 600 ° C = 200 kJ / s = 200 kW.

As a result of heat supply (with a steam stream and through the wall of the jacket 30), the temperature in the reactor rises, the waste heats up and when it reaches

temperature 300 ° C (for different types of waste, this temperature is different), which is controlled by the temperature sensor 34, the process of thermal decomposition of rubber waste begins, resulting in the formation of gaseous and solid products.

In our case, when heat is supplied to the reactor 10 in an amount of 200 kW, the total thermal decomposition time of the rubber waste is 120 minutes. The amount of gaseous products formed is 50 wt.%, I.e. Thermal decomposition of 1000 kg of waste generates 500 kg of the gaseous phase and 500 kg of the solid phase, which contains 150 kg of metal cord. Since the decomposition process is 120 minutes and during this time water vapor is supplied to the reactor at a rate of 75 kg / h and it is withdrawn at the same rate, the average rate of withdrawal of gaseous products mixed with water vapor from reactor 10 will be equal to [(500 kg ) + (75 kg / h) .2 h]: 7200 s = 0.09 kg / s.

The gaseous phase released in the reactor from the waste is mixed with the circulating water vapor and a vapor-gas mixture is formed. Since the amount of circulating water vapor does not change, and the gaseous phase of waste decomposition is continuously released, the pressure in the reactor 10 begins to increase, which is monitored by the pressure sensor 35. When the pressure reaches 2 atm, the flow meter 23 is opened and the vapor-gas mixture is removed with a flow rate of 0, 09 kg / s from the reactor 10 to the condenser 24. Simultaneously with the removal of the vapor-gas mixture from the reactor using a flow meter 21 from the steam generator 20, water vapor is supplied to the heat exchanger 13 with an average flow rate of 0.021 kg / s. Such a flow of water vapor is due to the fact that a gaseous phase is emitted in the reactor 10 at an average rate of 500 kg / 7200 s = 069. Therefore, the total amount of the vapor-gas mixture enters the reactor: 0.021 kg / s +0.069 kg / s = 0.09 kg / s

Since the vapor-gas mixture is removed from the reactor at a rate of 0.09 kg / s and arrives at the same rate, the pressure in the reactor remains constant, which is important for the process of thermal decomposition and the formation of decomposition products of constant composition throughout the process (pressure fluctuations the reactor will inevitably lead to changes in the composition of the gaseous phase).

Thus, the pressure in the reactor is kept constant, i.e. equal to 2 atm.

The content of the gaseous phase of the decomposition of the tires in the gas-vapor mixture is controlled by the readings of the gas analyzer 26, which is necessary for accurate determination of the completion time of the thermal decomposition of waste. The moment of completion of the process of thermal decomposition of waste corresponds to the time when the content of the gaseous phase in the vapor-gas mixture decreases to almost zero, i.e. almost pure water vapor begins to leave the reactor.

In our case, the process of thermal decomposition of waste is completed within 120 minutes.

As a result of cooling the vapor-gas mixture in the condenser 24, a liquid phase is formed in an amount of 80 wt.% And 20 wt.% Of the gaseous phase of decomposition of waste remains, and water vapor condenses and 150 kg of water is formed.

Thus, a liquid phase in the amount of 500 kg, 0.8 = 400 kg, is separated out from the gaseous phase in the condenser within 120 minutes, i.e. a mixture of a liquid phase and water is formed in the capacitor in an amount of 400 kg + 150 kg = 550 kg. This mixture is fed through a tap 36 to a separator 37, where water is separated from the liquid phase and fed through a tap 38 in an amount of 150 kg to a reservoir 39.

The liquid phase from the separator 37 through the valve 40 in the amount of 400 kg is fed into the storage tank 41.

The gaseous phase of the decomposition of rubber waste from the condenser 24 through the valve 25 with a flow rate of 16 kg / h is fed to the steam generator 19 and burned. In this case, the supply of liquid fuel from the tank 19 to the steam generator 20 is completely stopped. This allows for the processing of 1000 kg of waste to reduce the cost of liquid fuel used to learn working water vapor.

The remainder of the gaseous phase with a flow rate of 34 kg / h through the valve 42 is fed into the burner 28 and burned together with the liquid fuel supplied from the tank 19 to the burner 28.

The specific heat of combustion of the gaseous phase of 25,000 kJ / kg and the burning of 34 kg / h of this phase is equivalent to the combustion of 21 kg / h of liquid fuel with a specific heat of combustion of 40,000 kJ / kg. Since the process of decomposition of waste takes 120 minutes, the combustion of the gaseous phase in the burner 28 can reduce the consumption of liquid fuel from 70 kg / h to (70-21) = 49 kg / h. The reduction in fuel consumption supplied to the burner 28 is carried out using a flow meter 27.

When the moment of termination of the exit of the gaseous phase is reached using the actuator 7, the shutter 8 is opened and the supply device 9 moves the container 6 from the reactor 10 to the loading chamber 3. Then the shutter is closed. Using the actuator 43, the shutter 44 is opened and using the supply device 45, the container 18 is fed from the loading chamber 16 to the reactor 10. The container is installed so that the pipe 90 is connected to the pipe 12 of the heat exchanger 13. Then, the shutter 44 is closed.

After withdrawing the container 6 into the loading chamber 3 from the drive 39 through the tap valve 46 using a pump 47, water is injected into the nozzles 48 and sprayed over a layer of the solid phase in the container 6 in an amount of 100 kg. Water enters the solid phase and cools it, and it evaporates and the water vapor in a mixture with waste products through valve 49 leaves the loading chamber 3 into the reactor 10, then the steam from the reactor enters the condenser, where it condenses and returns through the separation system to drive 39. Such a closed cycle allows not only to eliminate the release of polluted water into the environment, but also to reduce the consumption of clean water for the implementation of the waste recycling process.

The cooling temperature of the solid phase in the container 6 is controlled according to the readings of the temperature sensor 50 and after reaching T = 110 ° C, at which the solid phase is not ignited in the open air, the spraying of water is stopped.

Using the rotary mechanism 51, the container 6 is turned and set upside down, as a result of which the solid phase falls out of the container 6 under the influence of its own weight onto the conveyor belt 52, which is driven by the engine 53, and a solid phase of 500 kg is fed into roll mill 54. After unloading, the container 6 is placed in the working position (bottom part down) and loaded as described above

In the roll mill 54, the solid phase, passing through the rolls, is ground, as a result of which the metal cord is separated from it. After the roll mill 54, the solid phase and the metal cord are fed to an electromagnetic separator 55, in which 150 kg of metal are separated from the solid phase. The metal is fed into a press 56 and pressed into briquettes, and a solid phase in the amount of 350 kg is fed to a storage 57.

From the drive 57 using a screw conveyor 58 into the gas generator 59 on its grate installed in the lower part of the gas generator, load the solid phase in an amount of 50 kg The solid phase is ignited on the grate of the gas generator and a burning layer is created. To maintain the combustion process of the solid phase on the grate using a blower 60 with a flow rate of 250 kg / h, air is supplied from above to the gas generator, and the combustion products are removed from under the gas generator grate through a faucet 61 into the chimney 33.

Next, from the drive 57 through a weighing batcher 62 into the tank 63 load 300 kg of solid phase. From the drive 39 through a flow meter 64 using a pump 65 in the tank 63 serves 150 kg of water.

In this case, the mass ratio of solid phase and water is: 300 kg: 150 kg, i.e. 1: 0.5.

From the vessel 63, the solid phase impregnated with water by means of a screw conveyor 66 is loaded into the gas generator 59 in an amount of 225 kg (contains 100 kg of the solid phase and 50 kg of water) so that the layer of the solid phase along the height of the shaft of the gas generator 59 is within 3D (D is the diameter of the shaft gas generator), which is controlled by the readings of the level sensor 67.

Thus, in the gas generator 59, a solid phase layer 1.5 m high is formed, in the lower part (on the grate) of which the combustion process proceeds, as a result of which heat is generated, due to which the overlying layers of the solid phase are heated (above the combustion layer).

In the gas generator 59, a reversed gasification process is implemented in which a solid phase soaked in water and air are supplied to the gas generator shaft from above, and the resulting combustible gas from the gas generator is removed from below (from under the grate).

In the upper part of the solid phase layer, water evaporates from it and water vapor forms, which mixes with the supplied air and enters the lower part of the gas generator, i.e. in the gasification zone, where the reaction of water vapor interaction with the carbon of the solid phase with the formation of a combustible gas containing mainly hydrogen and carbon monoxide, as well as some methane and resins.

In our case, as a result of gasification, 202 kg / h of solid phase impregnated with water is converted into gas and 23 kg of ash is formed (225 kg / h of solid phase impregnated with water is consumed). In this case, 25 kg / h of solid phase is burned in the combustion zone and 2.5 kg / h of ash is formed. The dry solid phase contains 85 wt.% Carbon, 5 wt.% Hydrogen and 10 wt.% Ash, which includes oxides of zinc, silicon, iron, etc.

When 25 kg / h of solid phase is burned, 298 kg / h of non-combustible products of combustion (containing nitrogen, carbon dioxide, water vapor and other gases) are formed and 2.5 kg / h of ash is formed. Thus, as a result of the implementation of the reversed gasification process in the gas generator 59, 202 kg / h + 298 kg / h = 500 kg / h of combustible gases and 23 kg / h + 2.5 kg / h = 25.5 kg / h of ash are formed. The specific heat of combustion of such a gas is 10,000 kJ / kg. This specific heat of combustion is due to the dilution of combustible gases obtained by gasification of the solid phase, non-combustible products of combustion (298 kg / h) of a part of the solid phase.

It is known that combustible gases obtained by gasification in gas generators of solid fuels with a high moisture content have a low specific heat of combustion. For example, gasification of brown coal with a moisture content of 36 wt.% Produces gas with a specific heat of combustion of 6000 kJ / m ³ (see S.D. Fedoseev, A.B. Chernyshev. Semi-coking and gasification of solid fuel. - M .: State Scientific -technical publishing house of oil and mining and fuel literature, 1960. - p.125, table 35).

The mixture of gases and resins from the gasification zone enters the combustion zone of the solid phase layer on the grate, passes through this zone and enters the outlet of the gas generator.

As a result of combustion and gasification processes, the solid phase layer is lowered through the gasifier shaft (sags) and therefore, the solid phase is continuously fed into the gas generator from the tank 63 using a screw conveyor 66 with a flow rate of 225 kg / h so that its level in the gas generator shaft remains constant, which is controlled according to the testimony of the level sensor 67.

The ash generated in the gas generator with a flow rate of 25.5 kg / h is discharged into the storage tank 68.

Simultaneously with the start of the gasification process, the valve 61 is closed, as a result of which the gas flow from the gas generator to the chimney 33 is stopped, the flow meter 69 and gas are opened (a mixture of solid phase combustion products, hydrogen, carbon monoxide and tar decomposition products - combustible gas) with a flow 500 kg / h is fed into the mixer 70, where through the tap-flow meter 71 with a flow rate of 50 kg / h serves the gaseous phase of the waste decomposition products after separation of the liquid phase from it. In this case, the mass ratio of combustible gas and gaseous phase is set in the range of: 500 kg: 50 kg, i.e. 1: 0.1.

In the mixer, a mixture of combustible gas obtained in the gas generator 59 and the gaseous phase in an amount of 500 kg / h + 50 kg / h = 550 kg / h is obtained. The specific calorific value of such a mixture will be 11,000 kJ / kg. This is because a gaseous phase with a specific heat of combustion of 25,000 kJ / kg in an amount of 50 kg / h is added to the combustible gas.

From the mixer 70, through a regulator valve 72, a mixture with a flow rate of 50 kg / h is fed to a steam generator 20 and burned to produce working water vapor, and the remainder of the mixture with a flow rate of 500 kg / h is burned in a burner 28 connected to the casing of the heat exchanger 13.

Burning 500 kg / h of a mixture with a specific heat of combustion of 11,000 kJ / kg is equivalent to burning 138 kg / h of liquid fuel with a specific heat of combustion of 40,000 kJ / kg. Therefore, the supply of liquid fuel from the tank 19 to the burner 28 is completely stopped. The resulting combustion products are used to superheat water vapor and heat the reactor. This eliminates the use of additional fuel for waste processing, and it is also useful to use the gaseous phase of the decomposition products.

From the storage tank 41, the liquid phase through the valve 73 in the amount of 400 kg is fed to the distiller 74, where at a temperature of 90 ° C, a fraction with a flash point of 35 ° C in the amount of 100 kg is isolated from the liquid phase, which is condensed by cooling in the heat exchanger 75 through the valve 76 is poured into the storage tank 77, and the remainder (liquid phase with a flash point of 61 ° C) from the distiller 74 in the amount of 300 kg is poured into the storage tank 78. In this case, the temperature in the distiller is monitored by the temperature sensor 79, and the flash temperature is monitored t according to the indications of the device 80 and regulate this temperature due to the time of the distillation process. During the process of distillation of the liquid phase, its flash point increases, and when the flash point reaches 61 ° C, the distillation of the liquid phase is stopped and the residue is poured into a container 78. In this case, the resulting fraction, which is condensed in the heat exchanger 75, has a flash point of 35 ° C. A liquid with a flash point of 35 ° C corresponds to the kerosene-gas oil fraction and can be used as high-grade fuel, for example, for gas turbine engines. A liquid with a flash point of 61 ° C corresponds to diesel fuel in its parameters and can be used as fuel for diesel engines.

The products of combustion, which are formed by burning a mixture of combustible gases and a gaseous phase in the burner 28, after exiting the jacket 30 of the reactor 10 through the valve 81 are sent to the jacket of the distiller 74 and use their thermal energy to heat and distill the liquid phase.

In this case, the amount of combustion products that are removed from the jacket 30 to the jacket of the distiller is controlled by a valve 81 so that the temperature in the distiller remains equal to 90 ° C. Excessive combustion products from the jacket 30 through the valve 31 are discharged into the heat exchanger 32 and used to heat the air supplied to the steam generator and burner 28.

This makes it possible to use the thermal energy of combustion products, which reduces the consumption of additional fuel for the distillation process, the production of water vapor and waste treatment.

Similarly carry out the process of processing rubber waste, which are located in the container 18, installed in the reactor 10.

After the thermal decomposition of the waste in the container 18 is completed, the shutter 44 is opened using the actuator 43 and the container 18 is withdrawn from the reactor 10 into the loading chamber 16 using the feeding device 45.

To cool the solid phase in the container 18 from the accumulator 39, water is supplied to the nozzles 83 through the valve 82 and sprayed over the solid phase in the container 18, as a result of which the container and the solid phase are cooled, the cooling temperature is controlled by the temperature sensor 84. The generated vapor from the chamber 17 enters the reactor 10 through the valve 85. The products of fuel combustion in the steam generator 18 through the smoke pipe 86 are released into the atmosphere.

After cooling using the rotary mechanism 87, the container 18 is rotated and set upside down. The solid phase from the container 18 falls out onto the conveyor 88, which is driven by the engine 89 and the solid phase is fed to the roller mill 54.

Example 2

From the drive 1, filled with crushed rubber waste, for example, crushed worn tires to a particle size of 50 mm, using a conveyor belt 2, waste is fed to the loading hopper 3 installed on the loading chamber 4 with the shutter gate 5 closed until the hopper is filled. In our case, the weight of the waste in hopper 3 is 250 kg. After that, the slide gate 5 is opened and the waste is poured into the container under the influence of its own weight 6. The waste supply operation is repeated until the container 6 is fully loaded. When the container 6 is fully loaded, the weight of the waste is 1250 kg. After that, using the actuator 7, open the shutter 8 and the feeder 9, the container 6 is moved from the loading chamber 3 to the reactor 10. The container 6 is installed so that the pipe 11 of the container 6 is connected to the pipe 12 of the heat exchanger 13. The shutter 8 is closed.

From the drive 1, using a conveyor belt 14, waste is fed to the loading hopper 15 mounted on the loading chamber 16 with the shutter gate 17 closed until the hopper 15 is filled. In this case, the weight of the waste in the loading hopper is 250 kg. After that, the slide gate 17 is opened and the waste is poured into the container 18 under the action of its own weight.

The loading operation is repeated 5 times and the container 18 is completely loaded with waste weighing 1250 kg.

From the tank 19, liquid fuel is supplied to the steam generator 20 with a flow rate of 20 kg / h (specific heat of combustion of the fuel is 41 MJ / kg), it is burnt and saturated water vapor with a temperature of 130 ° C. in the amount of 150 kg / h is obtained. The resulting steam through a flow meter 21 with a flow rate of 150 kg / h is fed into a shell-and-tube heat exchanger 13 (hereinafter referred to as the heat exchanger). Simultaneously with the supply of steam to the heat exchanger 13, a gas blower 22 is turned on and water vapor is pumped through the heat exchanger 13 and the waste layer in the container 6 in a closed loop. In order to prevent excessive pressure buildup in the reactor 10 as a result of steam supply, the flow meter 23 is opened and steam with a flow rate of 150 kg / h is discharged to the condenser 24, where it is condensed by cooling with water.

Water vapor filtered through the waste layer displaces air from the waste layer into the reactor, and then with the steam stream, the air from the reactor is displaced into the condenser 24. Since the air does not condense, it is supplied through the valve 25 to the steam generator 19 and used to burn fuel. The withdrawal of water vapor in a mixture with air into the condenser 24 is carried out until the air concentration in the reactor 10 decreases to 10 wt.%, Which is necessary to prevent oxidation of the decomposition products of the waste (their combustion in the reactor).

The air content in the reactor is controlled by the readings of the gas analyzer 26 and, when the air content is reduced to 10 wt.%, The steam output to the condenser is stopped by closing the valve 23. At the same time, the steam supply from the steam generator to the heat exchanger 13 is stopped (the flow meter 21 is closed).

From the tank 19 through the flow meter 27 to the burner 28 connected to the casing of the heat exchanger 13, liquid fuel is supplied with a flow rate of 86 kg / h and burned. The resulting combustion products with a flow rate of 1204 kg / h enter the casing of the heat exchanger 13 and then with the help of a smoke exhauster 29, the combustion products from the casing of the heat exchanger 13 are discharged into the jacket 30 of the reactor 10 and then into the chimney 33.

Flowing through the casing of the heat exchanger 13, the fuel combustion products heat the water vapor flowing through the pipes of the heat exchanger 13 to a temperature of 650 ° C, which from the heat exchanger enters the waste layer, gives off heat to the waste and again enters the heat exchanger. The combustion products passed through the casing of the heat exchanger 13 are cooled from 1000 ° C to 650 ° C (the heat of the combustion products is transferred to water vapor) and then enter the jacket 30 of the reactor 10, cooled and, at a temperature of 400 ° C, are discharged through a valve 31 to the heat exchanger 32, in which the combustion products are cooled to 150 ° C by a stream of air, which is supplied to the steam generator and to the burner 28 for burning fuel. After this, the products of combustion are discharged into the chimney 33.

The heat of the combustion products is transferred to the reactor not only with a stream of heated water vapor, but also through the wall of the jacket 30.

The combustion products have an average specific heat capacity of Cp = 1.24 kJ / s ° C, and their cooling from 1000 ° C to 400 ° C at a flow rate of G = 0.334 kg / s or 1204 kg / h provides a supply to the reactor (with steam and through the wall of the shirt 30) the amount of heat: Q = CpG (1000 ° С-400 ° С) = 1.24 kJ / kg ° С 0.336 kg / s 600 ° С = 250 kJ / s = 250 kW.

As a result of heat supply (with a steam stream and through the wall of the jacket 30), the temperature in the reactor rises, the waste heats up and when the temperature reaches 300 ° C (for different types of waste this temperature is different), which is controlled by the temperature sensor 34, the process of thermal decomposition begins rubber waste, resulting in the formation of gaseous and solid products.

In our case, when heat is supplied to the reactor 10 in an amount of 250 kW, the total thermal decomposition time of the rubber waste is 120 minutes. The amount of gaseous products formed is 55 wt.%, I.e. thermal decomposition of 1250 kg of waste produces 700 kg of the gaseous phase and 550 kg of the solid phase, which contain 200 kg of metal cord. Since the decomposition process is 120 minutes and during this time water vapor is supplied to the reactor with a flow rate of 150 kg / h and it is withdrawn at the same rate, the average rate of withdrawal of gaseous products mixed with water vapor from reactor 10 will be equal to [(700 kg ) + (150 kg / h) .2 h]: 7200 s = 0.138 kg / s.

The gaseous phase released in the reactor from the waste is mixed with the circulating water vapor, and a vapor-gas mixture is formed. Since the amount of circulating water vapor does not change, and the gaseous phase of the decomposition of waste is continuously released, the pressure in the reactor 10 begins to increase, which is controlled by the readings of the pressure sensor 35. When the pressure reaches 2 atm. open the flow meter 23 and transfer the vapor-gas mixture with a flow rate of 0.138 kg / s from the reactor 10 to the condenser 24. Simultaneously with the removal of the vapor-gas mixture from the reactor using the flow meter 21 from the steam generator 20, water vapor is supplied to the heat exchanger 13 with an average flow rate of 0.042 kg / from. Such a flow of water vapor is due to the fact that a gaseous phase is emitted in the reactor 10 with an average rate of 690 kg / 7200 s = 0, 096. Therefore, the total amount of the vapor-gas mixture enters the reactor: 0.042 kg / s + 0.096 kg / s = 0.138 kg / from.

Since the vapor-gas mixture is removed from the reactor at a rate of 0.138 kg / s and arrives at the same speed, the pressure in the reactor remains constant, which is important for the process of thermal decomposition and the formation of decomposition products of constant composition throughout the process (pressure fluctuations in the reactor are inevitable lead to changes in the composition of the gaseous phase).

Thus, the pressure in the reactor is kept constant, i.e. equal to 2 atm.

The content of the gaseous phase of the decomposition of the tires in the gas-vapor mixture is controlled by the readings of the gas analyzer 26, which is necessary for accurate determination of the completion time of the thermal decomposition of waste. The moment of completion of the process of thermal decomposition of waste corresponds to the time when the content of the gaseous phase in the vapor-gas mixture decreases to almost zero, i.e. almost pure water vapor begins to leave the reactor.

In our case, the process of thermal decomposition of waste is completed within 120 minutes.

As a result of cooling the gas-vapor mixture in the condenser 24, a liquid phase in the amount of 60 wt.% Is formed and 40 wt.% Of the gaseous phase of the decomposition of waste remains, and water vapor condenses and 300 kg of water is formed.

Thus, the liquid phase in the amount of 700 kg, 0.6 = 420 kg, i.e. in the condenser, a mixture of a liquid phase and water is formed in an amount of 420 kg + 300 kg = 720 kg. This mixture is fed through a tap 36 to a separator 37, where water is separated from the liquid phase and fed through a tap 38 in an amount of 300 kg to a reservoir 39.

The liquid phase from the separator 37 through the valve 40 in the amount of 420 kg is fed into the storage tank 41.

The gaseous phase of the decomposition of rubber waste from the condenser 24 through the valve 25 with a flow rate of 40 kg / h is fed into the steam generator 19 and burned. In this case, the supply of liquid fuel from the tank 19 to the steam generator 20 is completely stopped. This allows the processing of 1250 kg of waste to reduce the cost of liquid fuel used to produce working water vapor.

The remainder of the gaseous phase with a flow rate of 100 kg / h through the valve 42 is fed into the burner 28 and burned together with the liquid fuel supplied from the tank 19 to the burner 28.

The specific heat of combustion of the gaseous phase of 25,000 kJ / kg and the burning of 100 kg / h of this phase is equivalent to the combustion of 63 kg / h of liquid fuel with a specific heat of combustion of 40,000 kJ / kg. Since the process of decomposition of waste takes 120 minutes, the combustion of the gaseous phase in the burner 28 allows to reduce the consumption of liquid fuel from 86 kg / h to (86-63) = 23 kg / h. The reduction in fuel consumption supplied to the burner 28 is carried out using a flow meter 27.

Upon reaching the moment of termination of the exit of the gaseous phase using the actuator 7, the shutter 8 is opened and the feeding device 9 moves the container 6 from the reactor 10 to the loading chamber 3. Then, the shutter 7 is closed.

Using the actuator 43, the shutter 44 is opened and using the supply device 45, the container 18 is fed from the loading chamber 16 to the reactor 10. The container is installed so that the pipe 90 is connected to the pipe 12 of the heat exchanger 13. Then, the shutter 44 is closed.

After the container 6 is brought into the loading chamber 3 from the drive 39, water is supplied to the nozzles 48 through a flow meter 46 using a pump 47 and sprayed over a solid phase layer in the container 6 in an amount of 140 kg. Water enters the solid phase and cools it, and it evaporates and the steam formed in the mixture with waste decomposition products through valve 49 leaves the loading chamber 3 into the reactor 10.

The cooling temperature of the solid phase in the container 6 is controlled according to the readings of the temperature sensor 50 and after reaching T = 110 ° C, at which the solid phase does not ignite in the open air, the spraying of water is stopped.

Using the rotary mechanism 51, the container 6 is rotated and set upside down, as a result of which the solid phase falls out of the container 6 under the influence of its own weight onto the conveyor belt 52, which is driven by the motor 53 and is fed into the roller phase in the amount of 550 kg mill 54. After unloading, the container 6 is installed in the working position (bottom part down) and load it, as described above.

In the roll mill 54, the solid phase, passing through the rolls, is ground, as a result of which the metal cord is separated from it. After the roll mill 54, the solid phase and the metal cord are fed to an electromagnetic separator 55, in which 200 kg of metal are separated from the solid phase. The metal is fed into a press 56 and pressed into briquettes, and a solid phase in the amount of 350 kg is fed to a storage 57.

From the drive 57 using a screw conveyor 58 into the gas generator 59 on its grate installed in the lower part of the gas generator, load the solid phase in an amount of 50 kg The solid phase is ignited on the grate of the gas generator and a burning layer is created. To maintain the combustion process of the solid phase on the grate using a blower 60 with a flow rate of 250 kg / h, air is supplied from above to the gas generator, and the combustion products are removed from under the gas generator grate through a faucet 61 into the chimney 33.

Next, from the drive 57 through a weighing batcher 62 into the tank 63 load 300 kg of solid phase. From the drive 39 through a flow meter 64 using a pump 65 in the tank 63 serves 300 kg of water.

In this case, the mass ratio of solid phase and water is: 300 kg: 300 kg, i.e. 1: 1.

From the vessel 63, the solid phase impregnated with water by means of a screw conveyor 66 is loaded into the gas generator 59 in an amount of 300 kg (contains 150 kg of the solid phase and 150 kg of water) so that the layer of the solid phase along the height of the shaft of the gas generator 59 is within 3D (D is the diameter of the shaft gas generator), which is controlled by the readings of the level sensor 67.

Thus, a solid phase layer 2.5 m high is formed in the gas generator 59, in the lower part (on the grate) of which the combustion process proceeds, as a result of which heat is generated, due to which the overlying layers of the solid phase are heated (above the combustion layer).

In the gas generator 59, a reversed gasification process is carried out in which a solid phase impregnated with water and air are supplied to the gas generator shaft from above, and the resulting combustible gas from the gas generator is removed from below (from under the grate).

In the upper part of the solid phase layer, water evaporates from it and water vapor forms, which mixes with the supplied air and enters the lower part of the gas generator, i.e. in the gasification zone, where the reaction of water vapor interaction with the carbon of the solid phase with the formation of a combustible gas containing mainly hydrogen and carbon monoxide, as well as some methane and resins.

Let in our case, as a result of gasification, 280 kg / h of solid phase impregnated with water is converted into gas and 20 kg of ash is formed (300 kg / h of solid phase impregnated with water is consumed). In this case, 25 kg / h of solid phase is burned in the combustion zone and 3 kg / h of ash is formed. The dry solid phase contains 83 wt.% Carbon, 5 wt.% Hydrogen and 12 wt.% Ash, which includes oxides of zinc, silicon, iron, etc.

During the combustion of 25 kg / h of the solid phase, 272 kg / h of non-combustible combustion products (containing nitrogen, carbon dioxide, water vapor and other gases) are formed and 3 kg / h of ash are formed. Thus, as a result of the implementation of the reversed gasification process in the gas generator 59, 288 kg / h + 272 kg / h = 560 kg / h of combustible gases and 20 kg / h + 3 kg / h = 23 kg / h of ash are formed. The specific heat of combustion of such a gas is 9000 kJ / kg. This specific heat of combustion is due to the dilution of combustible gases obtained by gasification of the solid phase, non-combustible products of combustion (272 kg / h) of a part of the solid phase.

The mixture of gases and resins from the gasification zone enters the combustion zone of the solid phase layer on the grate, passes through this zone and enters the outlet of the gas generator.

As a result of combustion and gasification processes, the solid phase layer is lowered through the gasifier shaft (sags), and therefore, the solid phase is continuously fed into the gas generator from the tank 63 using a screw conveyor 66 with a flow rate of 300 kg / h so that its level in the gas generator shaft remains constant, which control according to the readings of the level sensor 67.

The ash generated in the gas generator with a flow rate of 23 kg / h is discharged into the accumulator 68.

Simultaneously with the start of the gasification process, the valve 61 is closed, as a result of which the gas flow from the gas generator to the chimney 33 is stopped, the flow meter 69 and gas are opened (a mixture of solid phase combustion products, hydrogen, carbon monoxide and tar decomposition products - combustible gas) with a flow 560 kg / h is fed into the mixer 70, where through the tap-flow meter 71 with a flow rate of 1 kg / h serves the gaseous phase of the waste decomposition products after separation of the liquid phase from it. In this case, the mass ratio of combustible gas and gaseous phase is set in the range: 560 kg: 280 kg, i.e. 1: 0.5.

In the mixer, a mixture of combustible gas obtained in the gas generator 59 and the gaseous phase in the amount of 560 kg / h + 280 kg / h = 840 kg / h is obtained. The specific calorific value of such a mixture will be 14,000 kJ / kg. This is because a gaseous phase with a specific heat of combustion of 25,000 kJ / kg in an amount of 280 kg / h is added to the combustible gas.

From the mixer 70, through a regulator valve 72, a mixture with a flow rate of 80 kg / h is supplied to a steam generator 20 and burned to produce working water vapor, and the remainder of the mixture with a flow rate of 760 kg / h is burned in a burner 28 connected to the heat exchanger casing 13.

Burning 760 kg / h of a mixture with a specific heat of combustion of 14,000 kJ / kg is equivalent to burning 266 kg / h of liquid fuel with a specific heat of combustion of 40,000 kJ / kg. Therefore, the supply of liquid fuel from the tank 19 to the burner 28 is completely stopped. The resulting combustion products are used to superheat water vapor and heat the reactor. This eliminates the use of additional fuel for waste processing, and it is also useful to use the gaseous phase of the decomposition products.

From the storage tank 41, the liquid phase through the valve 73 in the amount of 420 kg is fed to the distiller 74, where at a temperature of 100 ° C a fraction with a flash point of 40 ° C in the amount of 100 kg is isolated from the liquid phase, which is condensed by cooling in the heat exchanger 75 through the valve 76 is poured into the storage tank 77, and the remainder (liquid phase with a flash point of 85 ° C) from the distiller 74 in an amount of 320 kg is poured into the storage tank 78. In this case, the temperature in the distiller is monitored by the temperature sensor 79, and the flash temperature is monitored They are measured according to the indications of the device 80 and regulate this temperature due to the time of the distillation process. During the process of distillation of the liquid phase, its flash point increases and upon reaching a flash point of 85 ° C, the distillation of the liquid phase is stopped and the residue is poured into a container 78. In this case, the resulting fraction, which is condensed in the heat exchanger 75, has a flash point of 40 ° C. A liquid with a flash point of 40 ° C corresponds to the kerosene-gas oil fraction and can be used as high-grade fuel, for example, for gas turbine engines. A liquid with a flash point of 85 ° C corresponds to diesel fuel in its parameters and can be used as fuel for diesel engines.

The products of combustion, which are formed by burning a mixture of combustible gases and a gaseous phase in the burner 28, after exiting the jacket 30 of the reactor 10 through the valve 81 are sent to the jacket of the distiller 74 and use their thermal energy to heat and distill the liquid phase.

At the same time, the amount of combustion products, which is removed from the jacket 30 to the jacket of the distiller, is controlled by a valve 81 so that the temperature in the distiller remains equal to 100 ° C.

Excessive combustion products from the jacket 30 through the valve 31 are discharged into the heat exchanger 32 and used to heat the air supplied to the steam generator and burner 28. This makes it possible to use the thermal energy of the combustion products, which reduces the consumption of additional fuel for the distillation process.

Similarly carry out the process of processing rubber waste, which are located in the container 18, installed in the reactor 10.

After the thermal decomposition of the waste in the container 18 is completed, the shutter 44 is opened using the actuator 43 and the container 18 is withdrawn from the reactor 10 into the loading chamber 16 using the feeding device 45.

To cool the solid phase in the container 18 from the accumulator 39, water is supplied to the nozzles 83 through the valve 82 and sprayed over the solid phase in the container 18, as a result of which the container and the solid phase are cooled, the cooling temperature is controlled by the temperature sensor 84. The generated vapor from the chamber 17 enters the reactor 10 through the valve 85. The products of fuel combustion in the steam generator 18 through the smoke pipe 86 are released into the atmosphere. After cooling using the rotary mechanism 87, the container 18 is rotated and set upside down. The solid phase from the container 18 falls out onto the conveyor 88, which is driven by the engine 89 and the solid phase is fed to the roller mill 54.

Due to the use of solid and gaseous phases (waste decomposition products) for energy supply of the processing process, the effect of reducing energy intensity is achieved, since in comparison with the known processing technologies (grinding, pyrolysis, thermal degradation in oils, etc.), there is no need for additional fuel, which in turn, provides a reduction in emissions of combustion products into the environment. By processing waste, high-quality liquid fuel is obtained, which confirms the compliance of the claimed invention with the criterion of "industrial applicability".

Claims (1)

A method of processing rubber waste, including feeding waste into the reactor in a mobile container from the first chamber, thermolizing it in the reactor in a coolant medium passing through the waste layer to form gaseous and solid phases, withdrawing the gaseous phase from the reactor, discharging the solid phase from the reactor a container with a solid phase from the reactor at the end of the thermolysis process into the first chamber, unloading the solid phase and its electromagnetic treatment, the separation of the liquid phase from the gaseous by cooling it, the allocation of water s from the liquid phase, the combustion of the gaseous phase, the subsequent repetition of the process in which the waste is fed into the reactor in a mobile container from the second chamber, and the container is transferred from the reactor to the second chamber at the end of the thermolysis process, characterized in that the liquid fuel is burned and saturated water vapor with a temperature of 105 ° C, carry out the pumping of water vapor through a heat exchanger and a layer of waste in the container in a closed loop, an excessive increase in pressure in the reactor is prevented by partial removal of the dropsy about steam and its condensation by cooling with water, filtered through a layer of waste water vapor displaces air from the waste layer into the reactor and then the air flows out of the reactor with a stream of steam, because the air does not condense, it is used to burn fuel, water vapor is mixed with air they are carried out until the air concentration in the reactor decreases to the content necessary to prevent oxidation of the decomposition products of the waste — burning them in the reactor — in this way the reactor is blown with steam for air depletion, steam removal from the reactor is stopped when the air content is reduced to a predetermined one, at which it is impossible to ignite the decomposition products in the reactor, at the same time the steam supply to the heat exchanger is stopped, liquid fuel is burned, fuel combustion products are heated up with steam, then the combustion products are cooled to 150 ° С with a stream of air, then the combustion products are removed, the waste is heated by heat, and the process of thermal decomposition of rubber waste is carried out, as a result of which gaseous and solid I phase, the gaseous phase is mixed with circulating water vapor and a gas-vapor mixture is created so that the pressure in the reactor is constant part of the water vapor with the gas-vapor mixture is removed from the reactor, to accurately determine the time for completion of the thermal decomposition of the waste, the content of the gas decomposition phase of the tires in the gas-vapor mixture is controlled, the moment of completion of the process of thermal decomposition of waste corresponds to the time when the content of the gaseous phase in the gas mixture decreases to zero, the gas mixture they add and produce a liquid phase, from which water is separated by separation and accumulate it, this water contains dissolved organic substances - waste decomposition products, this contaminated water is used to produce combustible gas, which is spent on energy supply of the waste processing process, the liquid phase is accumulated after water is separated, the gaseous phase after the separation of the liquid phase is partially burned in a mixture with liquid fuel, and partially simply burned, upon reaching the moment of termination of the release of gaseous products water ra they are sprayed over a layer of solid residue in a container, it cools it, evaporates itself, and the water vapor in a mixture with waste decomposition products is fed to the reactor when the temperature of cooling of the solid phase in the container reaches T = 110 ° C, at which the solid phase is open tire decomposition is not ignited, water spraying is stopped, then the solid phase is broken, the metal cord is separated from it, electromagnetic separation is carried out, the metal is pressed into briquettes, and the solid phase is accumulated, the solid phase is ignited and give a burning layer, the solid phase and water are fed into the container in such an amount that the mass amount of the solid phase and water is 1: (0.5-1.0), a mixture of the solid phase and water is created in the container, a layer of the solid phase is created, in the lower part of which the overlying layers of the solid phase are heated — above the combustion layer, in which the solid phase, impregnated with water, and air are fed from above, and the resulting combustible gas is discharged from below, in the upper part of the solid phase layer, water evaporates and water vapor forms, which is mixed with the supplied air m and fed into the gasification zone, where the reaction of water vapor with solid phase carbon occurs to form a combustible gas containing mainly hydrogen and carbon monoxide, as well as some methane and resins, a mixture of gases and resins from the gasification zone is fed into the solid combustion zone phases, they are passed through this zone and removed from it, the resulting ash is accumulated, in the combustion zone of the solid phase the temperature is 1000 ° C and higher, therefore in this zone the gas is cleaned of resins and organic components, which under the action of high temperatures are decomposed to low molecular weight compounds - methane, ethylene and others; at the same time as the gasification process begins, gas and gas are removed - a mixture of solid products, hydrogen, carbon monoxide and tar decomposition products - the combustible gas is mixed with the gaseous phase of the waste decomposition products after separation from liquid phase at a mass ratio of 1: (0.1-0.5), when mixing the gaseous phase with a combustible gas that contains carbon monoxide and hydrogen, the reduction and hydrogenation reactions are carried out compounds, part of the mixture is burned to produce working water vapor, and the remainder of the mixture is burned, the resulting combustion products are used to heat the reactor and coolant, the liquid phase contains low-boiling products, a fraction with a flash point of 35- is separated from the liquid phase at a temperature of 90-100 ° С 40 ° C, which is cooled, condensed and accumulated, the remainder - the liquid phase with a flash point of 61-85 ° C is also accumulated, the flash temperature is controlled and regulated due to the time of the distillation process, while the products of distillation of the combustion products are controlled so that the distillation temperature remains equal to 90-100 ° C, during the process of distillation of the liquid phase, its flash point increases and when the flash temperature reaches between 61-85 ° C, the distillation of the liquid phase is stopped and the residue is accumulated, in this case, the formed fraction, which is condensed, has a flash point in the range of 35-40 ° C, which corresponds to the kerosene-gas oil fraction, a liquid with a flash point of 61-85 ° C diesel fuel, the combustion products that are formed during the combustion of a mixture of combustible gases and the gaseous phase are used to heat and distill the liquid phase, the solid phase in the container is cooled after completion of the thermal decomposition of waste, sprayed with water, the resulting steam is taken out to the reactor, the fuel combustion products emitted into the atmosphere, the combustion products have an average specific heat capacity Cp = 1.24 kJ / ° C and their cooling from 1000 ° C to 400 ° C at a flow rate of G = 0.269 kg / s or 968 kg / h provides quantities about heat: Q = Ср · G (1000 ° С-400 ° С) = 1.24 kJ / kg ° С × 0.269 kg / s · 600 ° С = 200 kJ / s = 200 kW, the temperature in the reactor rises, waste they are heated and when the temperature reaches 300 ° C - for different types of waste, this temperature is different, the process of thermal decomposition of the waste begins, as a result of which gaseous and solid products are formed, the pressure in the reactor is kept constant at 2 atm, after cooling, the solid phase is crushed (broken), then the processing cycle is repeated.

Images