SK288338B6 - Method of thermal decomposition of organic material and device for implementing this method - Google Patents

Abstract

Thermal decomposition process of organic material of the specified and / or mixed waste from used tires, plastics, paper, textiles, biomass and organic fractions of municipal waste in an inert atmosphere in the absence vzdu-chu / O takes place continuously in a hermetically sealed plug flow device for thermal decomposition so the treated material in the form of debris, cuttings or chips with a size up to 350 mm are transported to the metering hopper (15), and is transported metering spiral conveyor (16) by filling the decomposition of oil (17) defining an inlet oil seal (8) to the tubular flow-through a cracking reactor (1) with the sliding of the spiral conveyor (2), wherein the thermal cracking of the material takes place in a plug flow tubular cracker (1) at a temperature of 165-750 ø C and atmospheric pressure Pa from 100834.6675 to 101815,3325Pa (i.e., at atmospheric pressure, from -50mm to + 50 mm water column) in the gaseous, liquid and solid products also takes place the transport of the gaseous decomposition products of the first portion (1b) of the tubular cracking reactor the flow through the first outlet opening (13) and a second outlet opening (14) in the second part (1c) of the tubular prie-Rotation of the cracking reactor to a condensing system, extend also the transport of particulate product to the second section (1c) of the tubular flow rate of the cracking reactor by means of the spiral conveyor (2) the raw material through the water cooler (7) of solid parts of the third outlet opening (19) the output of solid products into the output water seal (9), from which the solid products collected indentation spiral conveyor (20) and the coil pick-conveyor (22). Device for the thermal decomposition of (1) organic materials to effect thermal decomposition process consists of a tubular flow-through cracking reactor (1), the frame (32) of the tubular flow rate of the cracking reactor, in which is arranged a tubular flow-through cracking reactor (1) at an angle of 8-38 degrees with the horizontal plane, the tubular plug flow cracking reactor (1) is disposed auger (2) the raw materials of which the lower part is immersed into the inlet of the oil seal (8), wherein the second portion (1c) of the tubular plug flow reactor is placed outlet water the cap (9).

Description

Technical field

The present invention relates to a method for the thermal decomposition of organic material and to the construction of an apparatus for the thermal decomposition of organic material. Said equipment enables continuous processing of organic material and production of alternative energy carriers of the second generation (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal decomposition of specified and / or mixed waste from used tires, plastics, biomass, organic parts of municipal waste by a tubular flow-through cracking reactor system for the processing of waste carbonaceous raw materials.

Prior art

Until now, the conventional method of mechanical recycling has been used for the treatment of organic waste. Furthermore, thermal processes are used, from which thermal cracking and pyrolysis make it possible to convert the polymeric material into monomers and other products. Thermal cracking of used tires, waste plastics, biomass and municipal waste allows their thermal degradation without the presence of oxygen / air. During thermal cracking, the waste is heated to high temperatures, at which time its macromolecular structures are broken down into smaller molecules. Products from thermal cracking can be divided into non-condensible gas fraction, liquid fraction and solid residues (coke). Furthermore, thermal cracking of waste provides a very wide compositional spectrum of hydrocarbons and non-hydrocarbons, from low molecular weight gases (hydrogen, carbon monoxide, carbon dioxide, alkanes and C ₁ -C 5 alkenes) through liquids to coke. Liquid thermal cracking products are used to produce valuable motor gasoline, kerosene, diesel, heating oils, alternative oils and valuable chemicals such as d, l-limonene from the thermal cracking of used tires. Optimal thermal cracking conditions and / or preferred catalysts are sought to obtain marketable products. The most valuable components of municipal waste include polymeric materials from industrial or municipal sources. Polymeric materials, and in particular polyethylene and polypropylene, are subjected to thermal cracking at a temperature of 165 to 750 ° C and atmospheric pressure to produce oil waxes with a boiling point of 30 to 450 ° C containing saturated and unsaturated hydrocarbons having carbon numbers of C ₅ to C ₃₀ . Subsequently, the gasoline fraction at 30 to 180 ° C containing saturated and unsaturated unbranched and branched C ₅ to Cu hydrocarbons is separated from the oil waxes by distillation at atmospheric pressure. The atmospheric distillation residue is further subjected to vacuum distillation at a pressure of 10 Pa to 110 kPa, separating the diesel fraction at 150 to 360 ° C containing saturated and unsaturated C ₉ to C ₂₂ hydrocarbons from the residue with a carbon number above C _22. . Gasolines obtained by atmospheric distillation of oil waxes and some naphthas obtained by vacuum distillation of oil waxes can be further hydrorefined on heterogeneous catalysts [Patent SR, number 287556, (2011); EP 2135923 A1].

The decisive technological parameters that most influence the composition of reaction products in thermal cracking include: chemical composition of the raw material, temperature, heat transfer rate, pressure, reaction time, reactor type, presence of reactive gases (eg oxygen), catalyst, additives present in raw material, gaseous and liquid phase of the process. The type of reactor determines the quality of the heat transfer, the mixing, the residence time in the gas and liquid phase and the release of the primary decomposition products. The reactor is selected mainly on the basis of technical assumptions, such as heat transfer and operating properties of the raw material and products. In several processes, the polymeric material is first dissolved in a polymer or wax melt or dispersed in a salt bath to reduce the viscosity of the melt. Other processes use excellent heat and mass transfer in the fluidized bed of thermal or catalytic reactors. Elevated temperature affects thermodynamics, through the relative stability of individual products as well as kinetics and through the physical conditions of the reaction mixture. High temperature and heat transfer, low pressures and residence times favor the formation of primary products.

In order for cracking reactors to be highly efficient in the chemical cleavage of polyalkenes, they must be designed in a flow-through design. For the same reasons, due to the high formation of coke and mineral residues, they should allow the continuous removal of coke during the decomposition of plastic waste.

The best solutions provide fluidized bed processes known from refineries such as fluid catalytic cracking (FCC) in the treatment of petroleum fractions with a cracking catalyst or fluid thermal cracking with coke or other mineral particles as a fluidizing medium.

According to U.S. Pat. No. 5,856,599, the cracking or liquefaction of plastic waste is carried out in a three- or four-stage screw extruder with increasing temperature. Similarly, the catalyst (if used) is removed with coke and a mineral residue. At the end of the process, the distillable hydrocarbon fractions are separated from the solid residue and the coke.

In another U.S. patent [U.S. Pat. No. 5,744,688], a mixture of polyalkenes and used tires is metered into a batch reactor equipped with a special mixer. Either a screw extruder or other device is used to fill the reactor. In this semi-continuous reactor, the feedstock is metered in over time and the main products are gaseous and liquid fractions, as well as a mixture of carbon black, mineral impurities and coke. At the end of the production cycle, the process stops and the mixer reverses. In this cycle, the mixer blades scrape the coke from the inner walls of the reactor. The main disadvantage of this solution is the semi-continuous operating reactor with a relatively small production capacity and problems with the use of a cracking catalyst.

In another reactor solution [U.S. Pat. 5811606] the mixer blades have exactly the same shape and size as the inside of the reactor. During thermal decomposition, the deposited solid material is scraped by the blades from the hot walls of the reactor. The scraped coke falls down and is sucked out of the bottom of the reactor with part of the reaction products by means of a suction line. The main products from thermal cracking are gaseous fractions (suitable for heating), petrol and light fuel oil (VOL) and paraffin fractions.

A batch reactor equipped with a screw metering and mixer is described in another U.S. patent [U.S. Pat. 5738025]. A special grate is installed inside the reactor above the molten cracking mixture of waste plastics. The waste plastics fed to the fission reactor are melted on a special grate and fall down into the reaction mixture. Similar to the description in the previous patent [U.S. Pat. 5811606] also in this case a mixer in a specially designed shape scraps the coke from the walls of the reactor into a specially shaped bottom of the reactor, from where they are removed by a screw conveyor. The temperature in this process reaches 450 ° C.

German researchers [EP 0591703] presented the gasification of waste plastics in a plasma reactor with the subsequent use of waste heat from a turbine to produce steam. Data on process efficiency are missing. The main advantage of the solution is the possibility of using a different composition of the raw material.

The procedure according to Polish workers [WO 03104354] allows the construction of a special semi-continuous reactor equipped with replaceable heating tubes (bodies). Heating pipes, which are heated inside by flue gases, provide heating of the input raw material with subsequent heating and enable the splitting of plastics. Due to the course of secondary cracking reactions, coke is formed. Coke settles on the outer surface of the heating tubes. The special design of the cracking reactor makes it possible to remove carbon deposits by means of vibrations of heating tubes. The heating pipes can be disassembled and replaced after the appliance has been shut down.

Since plastics also contain inorganic components, the use of chemical and non-catalytic processes has certain advantages over catalytic processes. Chinese researchers [CN 1397627/2003] proposed a two-step process. In the first stage, thermal cracking takes place, during which the plastics are partially split. At the same time, inorganic compounds are separated. In the next step, the partially cleaved products are cracked on a fixed catalyst.

Japanese and Chinese inventories have designed and patented several original solutions for cracking reactors. The same design of a cracking reactor is found in the two presented patents [WO 9620254 (1996), U.S. Pat. 2156332]. The waste plastics are metered by means of a screw extruder through a parallel-shaped tubular reactor with an internal conveyor, in which, after mixing, melting, cracking and evaporation take place in the individual zones. Japanese researchers have developed a tubular reactor with a screw mixer and conveying equipment [JP 100446158 (1998)]. Although the design of the reactors is not clear, it is clear from the designs that the main advantage of these reactors is the removal of coke, carbon residues and catalyst (if used) from inside the reactor. There is no mention in the solution of the output of products from the reactor system.

At the Wrocław University of Technology, they developed a tubular reactor with a special internal screw mixer [Polish patent application no. P 355826; J. Walendzievski, Continuous flow cracking of waste plastics, Fuel Proc. Technol. 86, 1265 (2005)]. The molten plastics from the screw extruder pass to a multi-tube reactor, where they are cracked at a temperature of 420 to 500 ° C. The task of the specially shaped internal mixer is to mix the molten plastics, scrape the coke from the inner surface of the tubular reactor and discharge the coke out of the reactor. The coke removal granules fall into the tank at the end of the reactor termination, while the hydrocarbon vapors then pass through air and water coolers to separators to separate the gases from the liquids. Laboratory experiments (0.3 - 2 kg) and pilot plants with a capacity of 20 - 30 kg / h have shown that this type of reactor can find commercial application in a flow-through version. The main advantage of this solution is the continuous removal of coke from the reaction tubes. The reactor cracking unit will consist of 6 or more tubes, which will be equipped with internal mixers, allowing either thermal or catalytic cracking of the waste polyalkenes.

Fluidized bed cracking reactors (thermal or catalytic) seem to be the best solution for their industrial use. However, regeneration and circulation of the so-called equilibrium catalyst is only possible for relatively clean feeds, for example residues from the vacuum distillation of gas oils from petroleum. Municipal plastic waste contains various mineral impurities, trace amounts of products and additives, which can quickly deactivate the expensive catalyst. In several cases, catalyst regeneration is not possible. Therefore, a cheap and available catalyst should be used when cracking plastics. Expensive and sophisticated zeolites or other molecular sieves, as well as noble metal catalysts, are likely to find limited use in recycling processes.

Another solution is thermal processes with an inert fluidizing medium, which have a coke removal section. Multi-tube reactors with internal mixers are suitable for smaller operations.

Thus, the known data on methods of waste recycling, thermal cracking reactors is used and eliminated by the method of production of chemicals, gaseous and liquid fuels, heating oils, solid carbon materials by thermal cracking, ie by way of specified and / or mixed waste from used tires, plastics, biomass, organic fractions of municipal waste in a universal cracking flow tube reactor according to the invention, the aim of which is to process waste carbonaceous raw materials into alternative second-generation energy carriers (chemicals, high-quality ecological fuels) and new carbon materials.

Despite enormous research efforts, there is very little data in the scientific and patent literature on coke formation during radical processes. The formation of coke is undesirable because the carbon products gradually settle on the inner surface of the reactor, which mainly impairs the heat transfer through the reactor wall. Effective control of the decomposition process becomes problematic. The products resulting from coking not only do not have the desired composition, but they cannot be produced efficiently. The performance of the reactors and thus the economy of the process decreases. The products are contaminated with carbon black, so they are not suitable as fuels for market use.

In order to prevent the formation of coke, and thus to enable the production of products with the desired composition, we need to have exact knowledge of the mechanism of decomposition of polymeric carbon raw materials and the course of secondary reactions, as a result of which coke is formed. From this point of view, currently existing conventional technologies are inefficient because they cannot either effectively prevent the formation of coke or effectively target thermal decomposition in the desired direction. Based on our detailed research and knowledge of the mechanism of decomposition of carbon polymeric materials and the course of secondary reactions leading to the formation of coke, we can conclude that the decomposition of polymeric carbon raw materials into gaseous, liquid and solid products takes place by the following processes: solid starting material softens, melts and turns into liquid condition. The raw material in the liquid state is then further heated and subsequently decomposed from higher polymer structures to low molecular weight structures depending on the decomposition temperature. The gaseous components are cooled to standard composition products. The composition of the products obtained and their molecular weight are decisively influenced by the decomposition temperature. The course of cracking reactions in the liquid state is important for the final composition of the obtained products.

To the greatest extent, the thermal cracking of carbon polymeric materials produces coke (carbon), especially when the resulting gaseous low molecular weight unsaturated hydrocarbons remain in the reaction space and are superheated for a long time. All conventional processes are currently carried out under conditions in which the gaseous components are slowly released from the intensively heated reaction space in the reactor. They are either adsorbed on the solid raw material and the resulting coke, or are absorbed in liquid products. These are the main reasons for the formation of huge amounts of coke. It is therefore most important to ensure the thermal cracking of carbon materials so that the gaseous, highly reactive (mainly unsaturated) components released by the decomposition of the liquid fractions are removed from the reaction space as quickly as possible so that they do not overheat intensively and for long periods. It should be noted here that in conventional technologies using melt extrusion equipment, the liquid components after liquefaction are thus transported in a high-density form. When such fluids are retained in the reaction space, a large amount of coke is formed. In addition, the resulting polymer-formed thin layer has a low thermal conductivity, which can lead to incorrect temperature control in the center of the reactor, and thus to poorer control of the composition of the products obtained.

The essence of the invention

The object of the invention, which overcomes said drawbacks, is a process for the production of alternative second generation energy carriers (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal decomposition of specified and / or mixed waste from used tires, plastics, biomass and organic shares of municipal waste. The essence of the solution is the creation of a new design of a tubular flow-through cracking reactor, which enables the continuous processing of waste carbonaceous raw materials.

According to this method, the thermal cracking is carried out in a hermetically sealed flow device. The input raw material prepared in the form of crushed stone, chips or chips with a size of up to 350 mm is transported to the dosing hopper. The transport of the treated feedstock is enabled by a dosing spiral conveyor through the charge of decomposition oil forming the inlet oil seal to a tubular flow-through cracking reactor equipped with a sliding spiral conveyor. The thermal cracking of the input carbon feedstock takes place in a tubular flow-through cracking reactor at a temperature of 165 to 750 ° C at atmospheric pressure from

100834,6675 Pa to 101815,3325 Pa (i.e. at atmospheric pressure from -50 mm up to + 50 mm water column) for gaseous, liquid and solid products. The transport of the formed gaseous decomposition products from the tubular flow-through cracking reactor takes place via two outlets towards the condensing system. The solid products (coke) are transported through the upper part of the reactor by means of a spiral conveyor through a water cooler through an opening for the exit of solid products into the outlet water seal, which forms a hydraulic seal. They are removed from it by a spiral conveyor.

The heating of the tubular flow-through cracking reactor is carried out in a heating furnace, which consists of two parts, the first and the second stage, by heat transfer from the flue gas. These are formed by the combustion of the supplied cooled cooled gas from the thermal cracking process with preheated air from the recuperator in furnace burners. The preheating of the feedstock takes place already in the initial phase of the dosing, namely by the heat from the oil charge, where it forms a condensate of high-boiling fractions of decomposition oil flowing by gravity from the space of the tubular flow-through cracking reactor. The tubular flow-through cracking reactor is placed on a metal frame at an inclination with a horizontal plane. In the tubular flow-through cracking reactor, there is a sliding spiral conveyor, the lower part of which is immersed in an oil cap. The upper part is closed by a water seal, while the oil and water caps are hermetically sealed. The oil and water seal are essential and necessary components of a tubular flow cracking reactor. The thermal decomposition of the carbon feedstocks taking place inside the tubular flow-through cracking reactor is thus carried out at atmospheric pressure from 100834.6675 Pa to 101815.3325 Pa (i.e. at atmospheric pressure from -50 mm up to + 50 mm water column). In said arrangement, when there is no overpressure in the tubular flow-through cracking reactor, the oil and water levels are stabilized. During the sudden (rapid) release of the vapors formed, overpressure occurs in the reactor space. Then, thanks to the liquid closures, the overpressure of the gas can be released into the air, and thus the pressure of the resulting gases does not increase above the permissible limit, because it can escape into the atmosphere through the liquid closures. This prevents possible destruction or other damage to the tubular flow cracking reactor. The safety system connected to the liquid closures can immediately stop the dosing of the raw material into the system in the event of a sudden increase in the pressure in the reactor and start the safe shutdown of the thermal cracking operation.

The range and quality of the products depend crucially on the ongoing reactions. One of the first to predominate is the primary cracking of carbonaceous raw materials into low molecular weight products. The latter include secondary condensation reactions, thermal alkylations, oligomerizations, polymerizations and cyclizations of primary products, which can lead to carboids (coke). It follows from the equilibrium composition that thermal decomposition thermodynamically promotes a reduction of the total pressure in the reaction system. Unlike decomposition reactions, secondary reactions are higher than first order. They are supported by higher concentrations of reactive components such as alkenes, acetylenes, dienes, aromatics and pressure. Therefore, higher pressure is also undesirable for cracking during kinetic reasons. Condensations with the formation of a concentrated liquid phase are also undesirable. Therefore, condensations that eventually form coke are even more sensitive to temperature fluctuations in the reactor and exchangers. More prominent are molecular condensation reactions, such as Diels-Alder syntheses. They gradually form polyenes, polyaromatics, tar and coke.

During thermal cracking, coke is regularly deposited on the inner surface of the reactor. Opinions on the mechanism of coke formation are not stable. There are probably two mechanisms. According to the first, the coking agents are adsorbed directly from the gas phase at the active sites of the surface and here by successive reactions with radicals from the gas phase and subsequent polymerizations and condensations passing to the coke. According to the second, these interactions, polymerizations and condensations take place in the gas phase up to the formation of an aerosol. The formed droplets settle on the surface and pass to coke by further reactions. In the second case, fibrous coke is formed. In the latter case, the form of the coke depends on whether the drops wet the surface or not. If so, an area of amorphous coke is formed. If not, globular (spheroid) coke is formed. Important precursors are vinyl and phenyl radicals and polyenes, polyacetylenes and polyaromatics formed therefrom. The effect of surface composition is significant. The advantage of reduced pressure (not overpressure) in the reactor is that the course of secondary reactions of gaseous hydrocarbons is limited. The method of production of alternative energy carriers of the second generation (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials in a flow-through cracking tube reactor according to the present solution represents an original technology using waste carbon polymer materials from municipal waste with universal waste. use. The versatility of a tubular flow-through cracking reactor is manifested above all in the fact that it enables the recycling of raw materials such as used tires, waste plastics, biomass and municipal waste. According to the invention, an efficient process is also realized by using the waste heat for preheating the air. The air is heated in recuperators before entering the burners. Flue gases are used as the heating medium. Waste process heat is also used to preheat the incoming raw material, which removes heat from the oil seal.

An advantage of the thermal decomposition method according to the invention is also its technical simplicity in the connection of the cracking tube reactor to the dosing hopper via the oil inlet cap, the cracking tube reactor in the upper part being equipped with a solid product conveyor and a take-off conveyor. The cracking tubular reactor is designed so that the gaseous and solid products can leave the reaction zone as quickly as possible. This prevents them from overheating and from undergoing secondary reactions leading to the formation of coke.

The thermal decomposition process according to the invention is an energy and material-intensive process. The recycling of carbon polymer waste protects the environment while producing high-quality second-generation alternative fuels. This replaces some of the fossil fuels, especially oil, which many countries (including Slovakia) import from abroad.

Further information on how to produce second generation alternative energy carriers (chemicals, solid, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal cracking of specified and / or mixed waste from used tires, plastics, biomass, organic municipal waste in a universal cracker flow tube reactor, as well as other advantages, are apparent from the exemplary embodiments, which, however, do not limit the scope of the invention.

Overview of figures in the drawings

The invention is further elucidated with the aid of the figures in the drawings. Figure 1 shows an apparatus for the thermal decomposition of organic material. Figure 2 shows a detail of the oil seal and Figure 3 shows a detail of the water seal.

Examples of embodiments of the invention

The technological process of thermal decomposition of carbon materials is carried out in a tubular flow-through cracking reactor 1a. The versatility of the tubular flow-through cracking reactor 1a is manifested in particular in the fact that it allows the recycling of raw materials such as used tires, waste plastics, biomass and municipal waste. The thermal decomposition device 1 consists of three parts, the dosing part, which consists of the dosing hopper 15, the dosing spiral conveyor 16 with the drive 18 of the dosing spiral conveyor and the oil inlet 8 and the spiral conveyor 2 of the raw material with the drive 3 of the spiral conveyor. reactor part (hot part) consisting of a first part 1b of the tubular flow cracking reactor, a second part 1c of the tubular flow cracking reactor from the heating furnace 4 of the first part 1b of the tubular flow cracking reactor and the heating furnace 5 of the second part 1c of the tubular flow cracking reactor cold take-off part), which consists of a water cooler 7 of solid parts, an outlet 9 water seal and a take-off spiral conveyor 22 with a drive 23 of the take-up spiral conveyor via conveying paths 26. The tubular flow cracking reactor 1a is schematically shown in figure 1.

The feedstock is located in the first part 1b of the tubular flow-through cracking reactor 1a. It ensures the entry of raw material through the dosing hopper 15, in connection with the dosing spiral conveyor 16, in which the decomposition oil charge 17 forming the inlet oil cap 8 is located. The connection of the dosing spiral conveyor 16 and the tubular flow cracking reactor 1a is at an angle of 90 to 125 degrees. The dosing of the raw material is provided by a dosing spiral conveyor 16 with a drive 18 of the dosing spiral conveyor.

The basis of the hot part is a tubular flow-through cracking reactor 1a placed on the frame 32 at an angle of 8 to 38 degrees with the horizontal plane. The tubular flow-through cracking reactor 1a is constructed of stainless steel with a diameter of up to 550 mm and a length of up to 16.0 m, in which a spiral conveyor 2 for transporting raw material and products along the tubular flow-through cracking reactor 1a is located. The drive 3 of the spiral conveyor of raw material is accommodated in the first part 1b of the tubular flow-through cracking reactor. Other parts of the hot part are the heating furnace 4 of the first part 1b of the tubular flow cracking reactor and the heating furnace 5 of the second part 1c of the tubular flow cracking reactor, the gas burner 12, the air preheater 6, the inlet oil cap 8 at the raw material inlet and the water cooler 7 for solid residues. . The tubular flow-through cracking reactor 1a has two successive stages with different operating temperatures. In the first part of the heating furnace 4 the temperature is maintained from 165 to 500 ° C, in the second part of the heating furnace 5 the temperature is 520 to 750 ° C, the temperature regulation depending on the input raw material. The tubular flow cracking reactor 1a is located in the heating furnace 4 of the first part 1b of the tubular flow cracking reactor and the heating furnace 5 of the second part 1c of the tubular flow cracking reactor with thermal insulation. The tubular flow cracking reactor 1a is heated by the heat of the hot flue gases flowing against the movement of the feedstock from the gas burner 12 located in the heating furnace 5 of the second part 1c of the tubular flow cracking reactor. In the gas burner 12, after the start of the process, decomposition gas is burned with air, which is formed by thermal cracking of the injected raw materials. The flue gases from the heating furnace 4 are discharged at the flue gas outlet point 11. They are fed via an inlet air preheater 6 to the flue gas outlet 29 of the gas gas.

The gaseous fission products resulting from the thermal cracking of the carbon feedstock leave the tubular flow-through cracking reactor 1a through the first outlet 13 in the first part 1b of the tubular flow-through cracking reactor. The decomposition gas formed in the free-radical cracking process leaves the tubular flow-through cracking reactor 1a also through a second outlet 14 in the second part 1c of the tubular flow-through cracking reactor. In the body of the tubular flow cracking reactor 1a, in its first part 1b of the tubular flow cracking reactor, a dosing hopper 15 for the input of raw material is located. In the second part 1c of the tubular flow-through cracking reactor, there is a third outlet opening 19 for the outlet of solid products (coke, steel cords from tires).

The resulting decomposition gas is discharged from the tubular flow-through cracking reactor 1a through the first outlet 13 and the second outlet 14 for condensation. It passes through a two-stage condensing system. In the first condensation stage, it enters the quench column. The decomposition gas vapors are cooled with the resulting decomposition oil to a temperature of 65 to 80 ° C. In the second condensation stage, the vapors of the gaseous products are cooled to a temperature of 30 to 35 ° C, where mainly C ₄ and C ₅ hydrocarbons condense. In the separator, the water is separated from the light heating oil. The condensed water is collected in an intermediate storage and returned to the technological process. Decomposition gases are compressed into tanks. After filtration and extrusion, they are used for combustion in gas burners in a cracking furnace.

The inclination of the tubular flow cracking reactor 1a fulfills the following functions: it naturally creates the necessary oil inlet cap 8 in the first part 1b of the tubular flow cracking reactor and allows easy and trouble-free transfer of the feedstock in the form of pulp, chips and reaction intermediates and products (coke, steel cords). ) along the tubular flow cracking reactor 1a ensures a smooth and easy transfer of heat and substances for the decomposition gases, liquids and coke during the decomposition process; allows the natural flow of residual decomposition oils into the oil inlet cap 8.

The heating of the tubular flow cracking reactor 1a takes place in the heating furnace 4 of the first part 1b of the tubular flow cracking reactor and in the heating furnace 5 of the second stage 1c of the tubular flow cracking reactor by heat transfer from flue gases resulting from combustion of combustion air and an inlet air preheater 6 through a gas gas and preheated air mixer 31 in the gas burner 12.

In the outlet second part 1c of the tubular flow-through cracking reactor 1a there is an injection spiral conveyor 20 of solid products with a drive 21 of a pick-up spiral conveyor (coke, steel cords from used tires) and a pick-up spiral conveyor 22 with a drive 23 of the pick-up spiral conveyor. Between the solid product injection spiral conveyor 20 and the take-off spiral conveyor 22, there is an outlet water seal 9. The level 24 of the outlet water seal forms a barrier to the entry of air from the outside into the inert environment in the reactor. The water supply to the outlet water seal 9 is at point 25. The connection between the solid product transport paths 26 and the pick-up spiral conveyor 22 is at an angle of 90 to 125 degrees.

The inlet oil cap 8 is located on the inlet metering part 1b of the tubular flow cracking reactor 1a and the outlet water cap 9 located on the outlet second part 1c of the tubular flow cracking reactor are essential and necessary components of the reaction system. The oil and water filling ensure hermetic sealing of the reaction space. The thermal decomposition taking place inside the tubular flow-through cracking reactor 1a is thus carried out at atmospheric pressure. In said arrangement, the level 10 of the oil seal and the level 24 of the outlet water seal are stabilized. Sometimes, during the sudden release of a pair of emerging products (bubble theory of the decomposition process), overpressure occurs in the reactor space. Thanks to the liquid closures, the overpressure of the gas can be released into the air, thus preventing the pressure of the resulting gases from rising above a safe limit. This prevents possible destruction or other damage to the tubular flow-through cracking reactor 1a. The safety system connected to the liquid valves 8 and 9 can, in the event of a sudden increase in the pressure in the reactor, immediately stop the dosing of the raw material into the reactor and start the safe shutdown of the thermal cracking operation.

Industrial applicability

Method of thermal decomposition of production of alternative liquid energy carrier of second generation (chemicals, gaseous and liquid fuels, heating oils) and solid carbon materials by thermal cracking from specified and / or mixed wastes from used tires, plastics, paper, textiles, biomass and organic municipal waste in the device for thermal decomposition of organic materials by means of a tubular flow-through cracking reactor according to the present invention, it is usable mainly in the recycling of waste carbonaceous raw materials in both small and large energy sources. It allows the flexible use of either smaller plants with an annual processing capacity of up to 20,000 tonnes built on a green field, or large-capacity plants at oil refineries, which make it possible to valorise the products obtained to an even greater extent.

Claims (7)

PATENT CLAIMS A process for the thermal decomposition of organic material from specified and / or mixed wastes from used tires, plastics, paper, textiles, biomass and organic municipal waste in an inert atmosphere without the presence of air / oxygen, characterized in that the thermal decomposition takes place continuously in a hermetically sealed manner. closed thermal decomposition device (1) so that the treated material in the form of crushed stone, chips or chips up to 350 mm in size is transported to the dosing hopper (15), then transported by a dosing spiral conveyor (16) through the filling of decomposition oil (17). ) forming an inlet oil cap (8) to the tubular flow-through cracking reactor (1a) by means of a spiral conveyor (2) of raw material, where thermal cracking of the material takes place in a flow-through cracking tubular reactor (1a) at a temperature of 165 to 750 ° C at atmospheric pressure from 100834,6675 Pa to 101815,3325 Pa (ie at atmospheric pressure from -50 mm up to + 50 mm water column) and decomposition of the raw material for gaseous, liquid and solid products, further the transport of gaseous decomposition products from the first part (1b) of the tubular flow cracking reactor through the first outlet opening (13) and the second outlet opening (14) in the second part (1c) of the tubular flow cracking reactor to the condensing system, the solid products are further transported to the second part (1c) of the tubular flow-through cracking reactor by means of a spiral conveyor (2) of raw material through a water cooler (7) of solid parts through a third outlet opening (19) to exit solid products to the outlet water valve (9), from which the solid products are removed by an injection spiral conveyor (20) and a removal spiral conveyor (22). Thermal decomposition method according to claim 1, characterized in that the heating of the tubular flow cracking reactor (1a) takes place in the heating furnace (4) of the first part (1b) of the tubular flow cracking reactor and in the heating furnace (5) of the second stage (1c) tubular flow cracking reactor by transferring heat from the flue gases resulting from the combustion of the supplied purified cold gas from thermal cracking by supplying pyrogen (30) from preheating (27) of combustion air and supplying (30) pyrogen via mixer (31) of gas and preheated air to gas burner ( 12). Thermal decomposition method according to Claim 1, characterized in that the preheating of the starting material already takes place in the initial dosing phase by heat from the decomposition oil (17) by means of condensed high-boiling fractions of decomposition oil from the first stage space (1b) of tubular flow cracking. reactor, flowing by gravity. Device for thermal decomposition (1) of organic material for carrying out the thermal decomposition process according to claims 1 and / or 2 and / or 3, characterized in that it consists of a tubular flow-through cracking reactor (1a), a frame (32) of tubular flow-through of a cracking reactor, on which a tubular flow cracking reactor (1a) is located at an angle of 8 to 38 degrees with a horizontal plane, a tubular flow cracking reactor (1a) comprising a spiral feed conveyor (2) and an inlet oil cap (8), an outlet water valve (9) is arranged on the second part (1c) of the tubular flow reactor. Device for thermal decomposition of organic material according to claim 4, characterized in that the first part (1b) of the tubular flow cracking reactor is located in the heating furnace (4) of the first part of the tubular flow cracking reactor and the second part (1c) of the tubular flow cracking reactor is located in the heating furnace (5) of the second part of the tubular flow cracking reactor, while the inlet air preheater (6) is located on the heating furnace (4) of the first part (1b) of the tubular flow cracking reactor and on the heating furnace (5) in the second part ( 1c) a tubular flow-through cracking reactor comprises a pyrogen-gas inlet (30), a pyrogen-gas and preheated air mixer (31) and a gas burner (12). Device for thermal decomposition of organic material according to claim 4, characterized in that a dosing spiral conveyor (16) and an inlet oil cap (8) are arranged on the tubular flow-through cracking reactor (1a) and placed at an angle of 90 to 125 degrees, the tubular the flow-through cracking reactor (1a) has a third solids outlet opening (19) formed in the second part (1c) and a pick-up spiral conveyor (22) at an angle of 90 to 125 degrees, on which the pick-up spiral conveyor drive (21) is located . Device for thermal decomposition of organic material according to claim 4, characterized in that a first outlet opening (13) of the first part of the tubular cracking flow reactor and a second outlet opening (14) of the second stage of the tubular cracking reactor are formed on the tubular flow cracking reactor (1a). flow reactor.