Classifications

• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B19/00—Heating of coke ovens by electrical means
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
  • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
  • C10B47/06—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in retorts
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
  • C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
  • C10B47/16—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge with indirect heating means both inside and outside the retorts
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B51/00—Destructive distillation of solid carbonaceous materials by combined direct and indirect heating
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
  • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
  • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
  • C10B53/07—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of solid raw materials consisting of synthetic polymeric materials, e.g. tyres
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E50/00—Technologies for the production of fuel of non-fossil origin
  • Y02E50/10—Biofuels, e.g. bio-diesel
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W30/00—Technologies for solid waste management

Definitions

• the proposed solution relates to a equipment for performing thermal decomposition of organic materials without access to oxygen.
• thermolysis Thermal decomposition of materials, thermolysis, is performed in order to obtain usable products.
• thermolysis in case of organic materials, pyrolysis is generally chosen, during which the decomposition takes place without access of oxygen, and thus without combustion.
• Decomposition of the material is caused by high temperatures and pressure, which are selected and continuously adjusted according to the composition of the material and the type and quality of the desired product.
• the material to be treated is placed in an enclosed heated space, for example a furnace chamber, where it is subjected to high temperatures while the gases evolved are removed from the heated space for further processing.
• the material is in a treatment allowing a good heat access, for example in the form of crushed or ground particles. Gases generated when the material is heated change their composition as the temperature of the material increases.
• Heated chambers usually do not work continuously, it is necessary to cool them for each batch of raw material before opening. Usually, the heating of the heated space is stopped first while the heat is still allowed to act for a certain time, after which the space is allowed to cool naturally or it is cooled artificially.
• the device for the above mentioned method is described, for example, in patent application CZ PV 2010-586.
• the device for thermal treatment of rubber waste consists of a chamber provided with a heating element, a cooling element and a condensing circuit with a flow source and a condenser.
• the heating element is in the form of a body of four electric spirals provided with a common cover, where this heating body is placed as a housing inside the chamber. From the outside, the chamber is provided with an insulating layer.
• a cooling element a tube system of ribbed tubes located in a heated chamber is described in the first case in the stated file and in the second case a partition wall situated on at least two sides of the chamber. There is an air gap between the partition wall and the chamber wall, cooled by flowing air.
• the condensing circuit is equipped with a fan to ensure the circulation of the gaseous medium from the chamber to the circuit and from the circuit back to the chamber, and it is also equipped with a condensate collecting vessel.
• Rubber waste in an amount of 0.1 to 0.9 of volume of the heated chamber is placed in the heated chamber, the chamber is closed and the temperature is raised to 350 to 400 °C.
• Combustible liquid condensate is removed from the gaseous air from the chamber via a condensing circuit from the condenser for further use.
• the chamber space is cooled to a temperature below 200 °C. Finally, the chamber is opened and the resulting solid residue is removed.
• the disadvantage of the given device is that it does not allow sufficient decomposition of the processed raw materials.
• the heaters are located only around the material, or in one place inside the material while there is no heating from below. During heating, the material settles down and a cake is formed, which may or may not have a crust. This makes it difficult for the passage of heat into the material and the possibility of leaving by the decomposition of the resulting substances, which prolongs the necessary processing time and dispels the limits of the selectivity of the composition of the leaving substances.
• the device does not allow other processing of gaseous vapors and aerosols generated during thermolysis other than condensation, so that only oil is obtained and no usable combustible gas is extracted. Residual fumes contained in the chamber may escape into the environment when the chamber is opened.
• Application PCT / CZ2013 / 000133 (CZ pat. 304 835) describes a device and method for the production of fuels for power engineering, in which carbonaceous material is processed by thermal decomposition in the absence of a flame.
• the batch of material is placed in the cavity of the reactor in the form of a mobile tank consisting of a pressure vessel with a flat or rounded bottom and with a lid provided with a gas outlet which is connected to a gas line.
• the device for heating the reactor consists of two chambers, a preheating chamber and a heating chamber. In the preheating chamber, the pressure vessel is preheated to a temperature of 90 to 120 °C over a period of 60 to 120 minutes and the gas mixture resulting from the thermal decomposition is removed.
• the pressure vessel is then transferred in a closed state to a reheating instrument, heated to a higher temperature, up to 550 °C, where it is reheated for up to 180 minutes at a pressure of 2 to 5 kPa, discharging the resulting gas mixture for further processing.
• the heated chamber spaces are maintained continuously in a heated state, and after removing one pressure vessel, another pressure vessel is placed in its place.
• the preheating chamber is in the form of a tank, filled with a liquid heat transfer medium and containing a bed for a pressure vessel, or several beds.
• the reheating chamber also contains at least one bed for the pressure vessel.
• the side wall around the pressure vessel is formed by a ceramic ring made of fireclay with built-in electric heaters.
• the densification in a high layer prevents perfect heat transfer and escape of released substances.
• Intensive heating is carried out by means of electric heaters only on the sides around the reactor, its heating from below only by liquid medium is not fast enough and efficient.
• the ring heating during the entire heating time by heaters of the same temperature over the entire height of the reactor does not provide optimal conditions for the economic decomposition of the settling material.
• the upper part heats excessively around the empty space in the reactor, while in the lower part, where the material is compacted, the heating is slower and a relatively large amount of electrical energy is needed to sufficiently heat and maintain the required temperature for thermolysis.
• Document CZ pat. 305,015 states that the material subjected to thermolysis is suitable to be layered into a thinner or thin layer.
• This patent performs thermal decomposition of only loose particles by a continuous method.
• the equipment according to this patent is a reactor in the form of a vertical body with a cylindrical wall provided with a hollow casing with a liquid heat transfer medium, an upper hopper of the material and a lower discharge of the material. Inside there are hollow heaters that flow around the processed material. These hollow heaters are filled with a liquid heat transfer medium with inlets and outlets outside the reactor.
• these heaters form heated chambers with a conical upper surface, and at the height in the middle there is a heated conduit with a passage for material around the walls of the reactor as well as in the middle of the reactor.
• the path for the material to be treated is formed on the one hand by the heated surfaces of these heaters located inside the reactor, and on the other hand by the passages between the heaters and the heated wall of the reactor. From above, the material is poured into the reactor, which in the reactor is stratified into a thin layer on heated inclined surfaces. After the material falls on the heated surfaces, it subsequently moves under the action of gravity and spreads down the various heated surfaces.
• the material is heated and the escaping gaseous thermolysis products are discharged through the side walls of the reactor.
• the outlet from which the dry residue is taken is the outlet from which the dry residue is taken.
• the heating is performed by heating the hollow casing of the reactor, and also inside the reactor, where the material path is heated by the liquid heat transfer medium.
• the temperature and pressure in the reactor are maintained and varied according to the composition of the material to be treated and the composition requirements of the presumed products.
• the disadvantage of this solution is the inability to process material other than liquid or loose particles. Another disadvantage is that since the material in the reactor does not stop and more and more material constantly flows in and out, only material mixtures of constant composition are discharged and not continuously over time significantly different pyrolysis products.
• the thermal decomposition equipment comprises at least one reactor and a thermal chamber for heating it, wherein the thermal chamber has walls provided with electric heaters and comprises a depression having the shape of a bed adapted to its shape and dimensions for accommodating the reactor.
• the reactor is in the form of a pressure vessel made of thermally conductive material with a gas-tight lid arranged at the top.
• the lid is provided with at least one handle for handling and at least one outlet for escaping gaseous substances and aerosols.
• the principle of the new solution of this equipment is the following constructional solution of the combination of a thermal chamber and reactor.
• the thermal chamber is arranged from a heating bath and a hollow ring located above the heating bath and reaching at least to the reactor lid.
• the heating bath reaches a height of 1/2 to 9/10 of the reactor placed in it.
• the heating bath is equipped with electric heaters inside the walls and in the bottom of the bed and it is provided with a double thermoregulatory casing around it, which is filled with a moving heat transfer medium.
• the hollow ring is placed above the walls of the heating bath and the thermoregulatory casing and it is connected to the thermoregulatory casing of the heating bath while it is also filled with a heat transfer medium.
• the walls, by which the heating bath with the thermoregulatory casing, the heating bath with the hollow ring, the heating bath with the reactor, the thermoregulatory casing with the hollow ring and the hollow ring with the reactor are in contact, consist of a thermally conductive material.
• the electric heating elements of the heating bath are preferably arranged in at least three independently controllable height sections one above the other.
• the bed formed in the thermal chamber for inserting and heating the reactor preferably has a cylindrical wall.
• the bottom of the bed is flat or convex.
• the reactor has also a cylindrical wall of the shape and dimensions corresponding to the bed, preferably abutting the cylindrical wall of the bed.
• the bottom of the reactor is convex at least in the peripheral part of the reactor, i.e. near the edge of the bottom. This means that the cross-section of both the bed and the reactor is circular or oval, whereas the cross-section of the bed has the same shape as the cross-section of the reactor, so that the dimensions correspond to the bed circumference of the reactor.
• the bottom of the reactor does not have such a condition. It may or may not have the same shape as the bottom of the bed, so that the bottom of the reactor according to the proposed solution does not have to rest on the bottom of the bed.
• the reactor preferably has a concave bottom in its central part, where this bulge forms a hollow central protrusion towards the inside of the reactor for spreading and thinning the layer of material to be treated and for supplying heat from the heated bottom of the heating bath to the material thus spread.
• the central protrusion according to the preceding paragraph preferably extends to the lower 1/10 to 1/2 of the height of the reactor.
• a hollow pocket is preferably arranged inside the reactor, formed at the bottom by the lower part of the reactor and at the top by a bulkhead dividing the space inside the reactor.
• the bulkhead is preferably located at the lower 1/10 and 1/3 of the height of the reactor.
• the bulkhead comprises a plurality of openings.
• a bulkhead in the form of a sieve, a mesh, a grid, a plate of perforated stainless steel plate, etc. can be used.
• at least one gas tube is led out under the bulkhead with openings, which passes through the reactor lid and leads through the space in the reactor down into the pocket under the bulkhead.
• the reactor comprises a central protrusion
• the central protrusion has a greater height than in which the bulkhead is situated.
• the proposed equipment for thermal decomposition is especially suitable for thermal decomposition of organic substances containing carbonaceous compounds, such as rubber, plastics, biomass, sewage sludge, etc. They can therefore be used for secondary treatment of many types of waste, such as PET bottles, plastic waste in general, used tires, waste from agriculture, waste from food production, etc.
• Thermal decomposition using the proposed equipment can be used to obtain products such as various additives, fertilizers, gaseous fuels, industrial oils and lubricants, hydrogen, activated carbon and other sorbents, pigments, composites.
• Various semi-finished products for industry can be produced, for example hydrocarbons, fractions for the production of other substances such as polypropylene, liquid products for petrochemistry, solid products for agriculture.
• the advantage of the proposed equipment is mainly to increase the economic efficiency of the thermal decomposition process. It is not necessary to relocate the reactor during the ongoing pyrolysis process, thus eliminating the safety risks, the need for unnecessary handling of hot reactors and the heat loss caused by the current situation when moving hot reactors from the preheating chamber to the reheating chamber.
• the efficiency is increased by supplying heat to the middle of the material layer and by reducing the heating of the heaters during the processing of the material so that the height from which the heat is supplied to the reactor is reduced in proportion to the settling of the layer of the decomposed material.
• the removal of the released products from the material can be improved by temperature and pressure control, as well as by feeding the activating medium to the reactor and handling it in a controlled manner through the decomposed material.
• the efficiency of the process is also increased by the proposed acceleration of the final cooling by a controlled supply of inert gas.
• Fig. 1 view of a vertical section taken in the middle through the thermal chamber with an inserted reactor
• Fig. 2 arrangement of heaters around the bed of the thermal chamber, seen from the front of the thermal chamber itself without the reactor, in section
• Fig. 3 top view of the thermal chamber with an inserted reactor
• Fig. 4 bottom view of the heaters under the bed in the thermal chamber, in cross section led under the heaters
• Fig. 5 reactor with a perforated bulkhead and a central protrusion, looking at a vertical section taken centrally through the reactor
• FIG. 6 top view of the reactor bulkhead itself according to the previous figure
• FIG. 8 top view of the reactor bulkhead itself according to the previous figure
• Fig. 9 bottom view of the thermal chamber with a terminal block
• Fig. 10 reactor heating scheme during operation, where the letters A, B, C, D indicate the individual successive phases of the process.
• Example of technical solution An exemplary design of the proposed solution is shown by means of a description of the construction of the equipment for performing thermal decomposition according to figures Fig. 1 to Fig. 9 and a subsequent description of the function of this equipment, shown schematically by means of figure Fig. 10.
• the equipment is formed as two separable bodies, which are the reactor 1 and the thermal chamber 2 for its heating.
• the thermal chamber 2 is in the form of a flameless furnace, the walls of which are provided with electric heaters 3 and inside there is a hollow bed 4, adapted in its shape and dimensions for accommodating the reactor T
• the reactor 1 is in the form of a hollow pressure vessel made of a thermally conductive material, for example stainless steel, which is provided at the top with a gas-tight lid 5.
• the lid 5 is provided with three handles 6 for handling and an outlet 7 for escaping gaseous substances and aerosols.
• thermal chamber 2 here means a heating equipment, i.e. a furnace, without an inserted reactor 1.
• This thermal chamber 2 is composed of two heating parts one above the other, namely a heating bath 8 and a hollow ring 9, located above the heating bath 8.
• the heating bath 8 reaches a height of 1/2 to 9/10 of the reactor placed inside.
• the height of the reactor 1 is understood here as the height dimension inside the reactor 1 closed by the lid 5, from the lowest point at the bottom to the highest point at the top, which is in the case of the figures of demonstrated shape of the reactor 1 in the middle of the bottom surface of the lid 5.
• the heating bath 8 is provided with electric heaters 3, which are located not only in the side walls but also in the bottom of the bed 4, as shown in figures Fig. 1, Fig.
• thermoregulatory casing 10 The surface part of the heating bath 8 is provided around the circumference with a double thermoregulatory casing 10.
• the hollow space in this double thermoregulatory casing 10 is filled with a moving heat transfer medium H, for example oil, in the operating state of the thermal chamber 2.
• H moving heat transfer medium
• the hollow ring 9 is placed on the heating bath 8.
• the thickness of the hollow ring 9 is such that it is located concurrently above the walls of the heating bath 8 as well as above the thermoregulatory casing 10.
• the hollow space located in the hollow ring 9 is connected to the hollow space of the thermoregulatory casing 10 and is also filled with heat transfer medium V ⁇ _.
• thermoregulatory casing 10 the heating bath 8 with the hollow ring 9
• thermoregulatory casing 10 with the hollow ring 9 and the hollow ring 9 with the reactor 1 consist of well thermally conductive materials such as copper, stainless steel, brass, aluminum, fiberglass, ceramics, slate, concrete, acrylate-based polymer, or combinations of these materials.
• the electric heaters 3 of the heating bath 8 situated above the bottom are arranged as three independently controllable height sections 301, 302, 303 one above each other. This arrangement is illustrated in figure Fig. 2.
• the division into sections 301, 302, 303 and the controllability of their operation is achieved by conventional technical means, for example by means of the terminal block 12 shown in figure Fig. 9, which can be connected to the control unit.
• the terminal block 12 according to figure Fig. 9 contains six pairs of contacts, of which one pair of these contacts is the inlet and outlet for the heater 3 in the bottom of the heating bath 8, one pair for the side first section 301, one pair for the second section 302, one pair for the third section 303 of the heaters 3, one pair for the temperature sensor (not shown in the figures) and one pair as a reserve.
• the bed 4 in the thermal chamber 2 intended for the insertion of the reactor 1 has a cylindrical wall and a flat or convex bottom and the reactor 1 also has a cylindrical wall and a bottom convex at least in the peripheral part, where optimally the cylindrical wall of the bed 4 and the reactor 1. fit tightly together.
• the reactor 1 has a concave bottom in its central part, where this bulge forms a hollow central protrusion 13 towards the inside of the reactor for supplying heat from the heated bottom of the heating bath 8 to the layer of material to be treated. It extends to 1/10 to 1/2 of the height of the reactor .
• a hollow pocket 14 is formed inside the reactor , formed at the bottom by the lower part of the reactor , i.e. by the lower part of its walls and its bottom, and at the top by a bulkhead 15 partitioning the hollow space inside the reactor T
• the bulkhead 15 is located at 1/10 and 1/3 of the height of the reactor 1 In the optimal variant of the reactor 1, shown in figures Fig. 1 , Fig.
• the bulkhead 15 is provided with a plurality of openings 16. Under the bulkhead 15, a gas tube 17 leads, which passes through the lid 5 of the reactor 1 and leads down through the hollow space in the reactor 1, through the bulkhead 15, where it leads into the pocket 14 under the bulkhead 15.
• the central protrusion 13 has a greater height than that in which the bulkhead 15 is located. Specifically, in this case, the central protrusion 13 reaches a height of approximately 1/3 of the height of the reactor 1 and the bulkhead 15 is located approximately at 1/8 of the height of the reactor 1, so that the central protrusion 13 protrudes above the bulkhead 15.
• the bulkhead 15 with the plurality of openings 16 can be in the form of a screen, a grid or, for example, also a perforated plate as shown in figure Fig. 6.
• the reactor 1_ has a welded curb forming a base 18, which prevents it from tipping over when it is filled in the outer space.
• the stated variant of the reactor 1 is optimal for the processing of particles and smaller bodies, such as biomass, plastics, various industrial wastes and crumbs of various materials.
• the reactor 1 may be adapted or manufactured for use without activating the material so that the gas tube 17 is not used.
• the perforated bulkhead 15 can be replaced by a non-perforated one, or the reactor 1 can be used without any bulkhead 15.
• modified reactor 1 is particularly suitable for thermal treatment of material falling through openings 16, for example for liquid sewage sludge or liquid industrial waste.
• the reactor 1 differs from the previous design in that it lacks a central protrusion 13.
• the bottom of the reactor 1 has a simple convex shape.
• a preferred design of the reactor 1 comprises a bulkhead 15 provided with a plurality of openings 16 and a gas tube 17.
• This variant of the reactor 1 is suitable, for example, for the thermal treatment of materials such as used tires, which are relatively bulky but hollow and contain steel cords which prevent easy grinding before processing.
• a batch of material to be processed is placed in the reactor 1 If the reactor 1 with the central protrusion 13 is used, the central protrusion 13 prevents the accumulation of material in the middle when it is filled into the reactor 1 and the material spreads around the central protrusion 13. If a reactor with the central protrusion 13 and the bulkhead 15 is used, the material is spread on the bulkhead 15 and up to the height of the central protrusion 13 around the central protrusion 13. The material can also be laid above the central protrusion 13. If the reactor 1 without the central protrusion 13 is used, the material is distributed over the entire bulkhead 15. If non-liquid material is used, the material in the reactor forms a pile that is highest in the middle.
• the reactor 1 with the material batch is inserted into the preheated thermal chamber 2 and is heated there without the access of oxygen when the lid 5 is closed.
• the generated vapors, gases and pyrolytic aerosols are continuously discharged from the upper part of the reactor 1 via the outlet 7. These are then passed to other processing equipments, in particular to cooling systems for fractionation of the final products.
• the decomposition process of the material in the reactor 1 is continuously regulated according to the type of starting material and requirements for the substance composition of products by temperatures and pressure levels in the reactor 1. Differently composed fractions of vapors, gases and aerosols are gradually released from the decomposed material.
• the pressure is regulated with respect to the material to be processed and the required type and quality of substances taken by the outlet 7 from the reactor 1.
• the thermal treatment of the material in the thermal chamber 2 is carried out in a total of at least four phases, of which the reactor 1 is heated in at least three phases, so that
• the reactor is preheated to a temperature of 90 to 120 °C and the processed material is freed of water vapor and air
• the reactor is heated to 120 to 600 °C and pyrolytic aerosols and gaseous substances from pyrolysis are removed from the reactor
• the heating of the reactor 1 is carried out only to the extent that the maximum temperature reached is maintained and the pyrolytic aerosols and gaseous substances from the pyrolysis are removed from the reactor 1
• the heating is stopped and then the reactor is removed from the thermal chamber 2 and the residual material is poured out.
• the heating of the reactor is carried out gradually at different heights.
• the heating is shown schematically in figure Fig. 10.
• FIG. 10 shown by the letters A, B, all the electric heaters 3 of the thermal chamber 2 are in operation. All three sections 301, 302 and 303 of the heaters 3 heat all around in the walls of the heating bath 8 as well as the heaters 3 in the bottom of the bed 4. In addition, it is also heated via the hollow ring 9.
• the heating of the reactor 1 is therefore intensive in the first and second phase of the thermal treatment of the material in the thermal chamber 2.
• the heat enters the reactor simultaneously from the sides and from the bottom of the bed 4.
• the material is heated from all directions except from above.
• the heat comes through the bottom of the reactor 1, the pocket 14 and the bulkhead 15.
• the heat comes along the entire height of the reactor .
• the reactor 1 having a concave bottom bulge in the form of a central protrusion 13 is used, so the heat supplied from below on the one hand heats the material layer from below and on the other hand enters the central protrusion 13 and through it into the material layer, where it heats the material away from the axis of the reactor 1
• the heat supply in the middle of the material layer via the central protrusion 13 significantly increases the heating efficiency, inter alia also with regard to the fact that the bulk material in the reactor 1 is usually in the shape of a pile with the greatest height in the middle.
• the pressure in the reactor 1 is preferably kept lower than 3.5 kPa in the first phase.
• the pressure in the reactor is preferably increased to 3.5 to 5.5 kPa.
• the values at which the temperature and pressure in the reactor 1 increase in the second phase are then preferably maintained in the second phase for the period of 2 to 3 hours.
• the decomposed material is eventually activated.
• This phase is shown in figure Fig. 10, indicated by the letter C.
• the activation phase can be carried out if the reactor 1 containing the bulkhead 5 with the plurality of openings
• the activation phase in the material pyrolysis process depends on the user's choice. He decides for it according to the current conditions, especially according to the type of processed material, the presence of other related equipments for the processing of fractions of discharged substances and according to the requirements for the material composition of the products.
• the temperature in the reactor is raised to 560 to 700 °C. All temperatures mentioned in the reactor are measured under the lid 5, at a height of 2/3 to 9/10 of the height of the reactor . Also in the activation phase, all three sections 301. 302 303 of the heaters 3, the heaters 3 in the bottom of the heating bath 8, as well as the hollow ring 9 are used to increase the temperature.
• the heat transfer medium H is heated by the heating of the heaters 3 and circulates from the thermoregulatory casing 0 to the hollow ring 9 and back.
• the pressure required in the reactor 1 for this phase is 6 to 200 kPa.
• an activation medium based on water vapor is supplied into the reactor 1 through the gas tube
• the activation medium flows from below and disperses through the plurality of openings 16 in the bulkhead 15 and the decomposed material, then flows upwardly through them.
• the flow of the activating medium as it passes through the decomposed material disintegrates the settling particles, helps in the supply of heat to the material, and at the same time facilitates the release and removal of substances from the decomposed material.
• the release medium enriched in released substances rises above the material to be treated up to the lid 5, from where it is then discharged out of the reactor .
• the most preferred volume of activation medium to be fed to the reactor 1 during the third phase is 3 to 5 times the volume of the reactor 1
• the penultimate phase of the heat treatment begins.
• the penultimate phase is the third phase if no activation is performed. If activation is performed, the penultimate phase is the fourth phase. This phase is shown in figure Fig. 10 and it is marked with the letter D. In the penultimate phase, the maximum temperature reached in the reactor 1 is maintained.
• the heat transfer medium H is discharged from the hollow ring 9 and is heated only by the electric heaters 3, so that the reactor 1 is heated only from below under the bottom and around the side walls to a height of 1/10 to 1/2 of the reactor 1_.
• the penultimate phase is preferably carried out for 15 to 30 minutes. Only the heaters 3 are allowed to heat under the bottom of the bed 4 and the heating by the sections 303, 302, 301 is limited, in particular it is heated by the lower section 301. It is heated optimally to the height of the material, with regard to reducing the height of the layer of descending residue of the processed material. When using several sections 303, 302, 301 in this phase, these are gradually switched off from above. After a sufficient degree of decomposition of the material, it proceeds to the last phase, which represents cooling.
• the last phase is shown in figure Fig. 10 and it is marked with the letter E.
• the cooling rate is optionally regulated by introducing nitrogen into the gap below the bulkhead 15, i.e. into the pocket 14. On the one hand, it accelerates the cooling and, on the other hand, expels the residues of the pyrolysis gas.
• the economic volume of nitrogen fed to the reactor 1 in the last phase of the material processing is 1 to 2 times the volume of the reactor 1 If accelerated cooling is required in the double thermoregulatory casing 10 and the hollow ring 9, a cold heat transfer medium 11. circulates.
• the bulkhead 15 facilitates the distribution of material, facilitates the even distribution of the supplied medium and heat from below, prevents clogging of the mouth of the gas tube 17 and facilitates the removal of any solid residue from the processed material as well as the cleaning and maintenance of the reactor 1
• the reactor 1 After cooling, the reactor 1 is removed from the bed 4, the lid 5 is opened and the rest of the material is removed.
• the remainder is usually in the form of powdered carbon, but in the presence of inorganic substances other particles may be present, for example in case of processing of old tires, in addition to carbon, steel cords remain in the reactor 1.

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• Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

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• 2021
  • 2021-02-10 CZ CZ2021-38549U patent/CZ34946U1/cs active Protection Beyond IP Right Term
• 2022
  • 2022-02-07 CN CN202220249775.2U patent/CN217368415U/zh active Active
  • 2022-02-09 WO PCT/CZ2022/000007 patent/WO2022171217A1/en active Application Filing

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