A PROCESS AND THERMOLYSIS SYSTEM FOR OBTAINING RECOVERED CARBON BLACK AND FUEL FROM DISPOSED TIRES

Abstract

A thermolysis process and system for obtaining recovered carbon black and fuel from used tires, including a thermolysis reactor and a flash vessel working together to refine the fuel without requiring post-treatment for cleaning. In thermolysis, the condensers are cleaned without interrupting the flow or diverting the gas stream, as the deposits formed inside the heat exchanger tubes are cleaned using a portion of the recovered fuel. The carbon black obtained is comparable to current semi-reinforcing carbon blacks. The resulting fuel has a high aromatic content, and its carbon content is reduced to 3% by weight and to as low as 0.8% by weight compared to fuels obtained through pyrolytic processes, without requiring post-treatment such as distillation or catalytic treatment.

Description

A PROCESS AND A THERMOLYSIS SYSTEM FOR OBTAINING RECOVERED CARBON BLACK AND FUEL FROM DISUSED TIRES. Field of Invention A process and system for thermolysis of used tires is described for obtaining recovered carbon black and fuel of better quality than those of the state of the art, where the recovered carbon black is of a quality comparable to the semi-reinforcing carbon blacks currently on the market, thanks to its surface chemistry and its behavior in rubber and where the fuel obtained has a low content of carbonaceous material. Furthermore, the characteristics of the fuel obtained by the process of the invention allow the cleaning of the condensers without stopping the process, by introducing part of the same fuel obtained into the condenser tubes. Background of the Invention Various pyrolysis and thermolysis processes and systems are known for treating used tires, where a crude fuel of a dark brown to black color is obtained, the objective of which is to improve the fuel through post-treatment stages. Document WO0226914 provides tire pyrolysis systems and procedures that include feeding tire strips into a pyrolysis vessel and pyrolyzing the strips in said pyrolysis vessel to produce a mixture of pyrolysis gas and carbon black; the pyrolysis gas is processed by centrifugally separating entrained particles therefrom, separating the pyrolysis gas into a hydrocarbon condensate and a light vapor, extracting the entrained hydrocarbon condensate from the light vapor, and purifying and refining the hydrocarbon condensate; the carbon black mixture is processed by pulverizing the mixture to fragment all filaments and masses of inorganic solids, cooling the carbon black mixture, separating crude contaminants from the carbon mixture, and purifying and refining the carbon black;The hydrocarbon condensate is purified and refined by removing all remaining contaminants, eliminating any polycyclic aromatics to produce a clear, colorless plasticizing oil; the carbon black is purified and refined by pulverizing it as a powder, eliminating all particulate contaminants; The remaining two can be optionally granulated and stored in bags or packages for shipment. However, this document does not describe the use of a flash distillation unit in direct communication with the pyrolysis reactor that would allow the recirculation of part of the liquid hydrocarbon phase to the pyrolysis reactor, preventing the entrainment of carbonaceous material in the gas stream. Document JP2005074320 describes a device for separating pyrolysis residues generated during dry distillation of waste materials such as a scrap tire. This device, for separating metal and carbide contained in the pyrolysis residue generated during dry distillation, comprises: a hopper that introduces the pyrolysis residue into a water tank while protecting the residue from air; a paddle positioned beneath the water layer in the hopper that rotates to generate a water flow; a metal recovery apparatus that recovers the metal precipitated at the bottom of the water tank; and a carbide recovery apparatus that recovers the carbide floating on the surface of the water in the tank.This document does not specify the pyrolysis process itself, but rather the treatment of the waste generated in a pyrolysis process; for the same reason, a Flash distillation stage or equipment is not described either. Document CL-51.252 (application CL-26-2010) describes a method for the thermal treatment of used tires, based on preheating the previously shredded raw material in a feeding mechanism of a vertical reactor, which allows increasing the efficiency of the thermal treatment by reducing energy consumption through the use of waste energy. This method comprises: (a) supplying the previously shredded used tires to a conveyor; (b) feeding said used tires to a feeding mechanism located above a reactor; (c) preheating said used tires inside said feeding mechanism with a first stream of exhaust gases from an internal combustion engine; (d) feeding said preheated used tires to said reactor;(e) supplying a second stream of exhaust gases from the engine through a first gas connection pipe located in the middle zone of said reactor or thermolysis reaction zone, generating in said reactor an oxygen-free environment, generating with said thermolysis reaction a thermolysis gas stream that leaves the reactor through an outlet; ML / a / zuz i / un oí ua (f) recirculating the gases used in step (c) from inside the feeding mechanism to an inlet pipe located in a lower cooling zone of the reactor to cool the solid thermolysis products obtained in step (e); (g) evacuating the cooled solid thermolysis products from step (f), such as carbon black, mineral tire aggregates, metallic reinforcement, and others, exiting the bottom of the reactor through a feeder airlock to a receiver for solid thermolysis products; (h) delivering the cooled solid thermolysis products through an airlock feeder to a magnetic separator to separate the solid thermolysis products, carbon black, and others, from the metallic reinforcement; and (i) recirculating said thermolysis gas stream.Although a tire thermolysis process is described, it is not carried out in a horizontal cylindrical reactor, nor is the reactor atmosphere inerted with nitrogen; the combustion gases are in direct contact with the material to be thermolyzed, unlike the present invention, where the heat flow is through an external chamber surrounding the reactor. Furthermore, document CL-51.252 does not mention a recirculation operation of liquid hydrocarbons from a flash distillation vessel to the reactor, nor does it specify a particular design of the distillation cylinder. Document JP2014142460 describes a treatment system for waste tires, plastic waste, etc., for conversion into pyrolysis oil. This system utilizes the energy of pyrolysis gas at high temperature to efficiently separate Class 1 petroleum from the oil content. The treatment system for conversion into pyrolysis oil includes a lower tank, a heater for heating the lower tank, a distillation cylinder with a waste gas outlet at the top, a cooling section, a collection system for the liquefied ingredients in the cooling section, a temperature sensor located directly above the collection system within the distillation cylinder, and control means for operating the heater.Although a system for tire pyrolysis is described that includes, among other things, a distillation cylinder after the pyrolysis reactor, a recirculation operation from this distillation cylinder to the reactor is not described, nor is a particular design specified. -4 of the distillation cylinder. Document TW462984 describes a method for recycling solid waste such as waste tires, which comprises using a series of steps including: heating, dry distillation, and pyrolysis to form gases and solid carbides; discharging the solid carbides from the bottom of the reactor furnace; applying a series of processing steps, including water washing, magnetic sorting, alkaline washing, and acid washing, to the solid carbides to separate the steel wires and remove the ash content containing heavy metals; pulverizing the carbides to a desired particle size to form high-purity carbon black; introducing the carbon black into an activation furnace to heat and activate it in a steam environment, thereby producing granular activated carbon; condensing the gas product and applying an oil / gas separation stage to the gas product to form fuel oil and fuel gas by-products.Such fuel oil and / or fuel gas can be introduced into a pyrolysis furnace and an activation furnace as fuel for heating outside the furnace. This document describes a dry distillation process in conjunction with pyrolysis; however, the pyrolysis reactor is not horizontally operated and surrounded by an outer chamber, and the flash distillation vessel does not have the specific design described in the present invention. Furthermore, an additional advantage of the present invention relates to the cleaning of the condenser tubes used in the thermolysis process, which is carried out with part of the fuel obtained through the process of the invention, which is passed in co-current along with the process flow that flows through the condenser tubes. Generally, the cleaning of the heat exchangers inside is carried out during equipment maintenance and / or by diverting the gas flow to be condensed, to inject a cleaning flow instead. Techniques for cleaning heat exchangers include: • High-pressure washing with a water flow of the disassembled equipment, inside or outside the plant and during maintenance periods. • Use of chemical products to remove deposits inside disassembled or non-disassembled equipment, inside or outside the plant, during maintenance or operation, in the latter case, it is necessary to cut off the feed to the process flow, using recirculation systems (US 6485578 Bl). ιнАЛ / a / zuz i / un oí ua • Use of tools to clean pipes, commonly with a rod on disassembled equipment inside or outside the plant during maintenance. • Use of robotic system to clean the heat exchanger in situ, without disassembling the equipment, but with process flow cut off (CN1664486 A). • Online cleaning system with a system of cleaners such as solid spheres capable of dragging deposits out of the tubes, without interrupting the process flow (CN 104315919, CN203615822 U, US4569097 A). Specifically, document JP2005134079 describes a method and equipment for efficiently removing contamination from the cooling tubes of a condenser used for the condensation of polystyrene pyrolysis gas. Within the condenser, cooling tubes are arranged through which a refrigerant is circulated. Polystyrene pyrolysis gas from a thermal decomposition device is supplied to the condenser, where it is cooled by heat exchange with the refrigerant in the cooling tubes. A high-boiling-point component containing styrene condenses into an oil (fuel). When the surfaces of the cooling tubes are contaminated, the oil obtained from the condensation is sprayed onto the surface of the cooling tubes using a spraying medium, and the contaminant is removed by the cleaning effect of the spray.Although this document implicitly mentions the cleaning of a condenser associated with a pyrolysis process, this cleaning is not performed by injecting a hydrocarbon fuel obtained from the same process and recirculated in co-current. In the present invention, the fuel obtained has a high content of aromatic compounds, which gives it a high capacity for dissolving the solids encrusted inside the condenser tubes. Furthermore, in the present invention, the cleaning is more efficient because it depends not only on the fuel outlet pressure through the injectors but also on the characteristics of the fuel itself—that is, the product used to clean the inside of the condenser tubes—and its ability to dissolve the internal scale within the condenser tube.The fact that the fuel is injected into the tubes in co-current creates a synergistic entrainment effect between the cleaning fluid (fuel) and the process gas flow, increasing cleaning efficiency compared to other similar systems. Furthermore, the invention includes a fuel filtration system. ΙνΙΛ / α / ΖυΖΊ / UI OI UU -6 where a fraction of this is recirculated for cleaning the condenser tubes, where the residues carried by this fraction are trapped in the same filter. In document JP2005134079, the refrigerant or service fluid passes through the inside of the tubes and the cleaning is generated on the external surface of the tubes through which the process fluid or the gas stream to be condensed passes. US Patent 7998281B2 describes an apparatus for the online cleaning and maintenance of a tubular heat exchanger line. It involves injecting a cleaning fluid at high pressure without interrupting the process line, meaning without opening the equipment or stopping operations. Its application is in the petrochemical industry, particularly for cooling the effluent from the cracking furnace. This patent does not use the cleaning agent itself, that is, it does not use a hydrocarbon fuel produced in the same process with the characteristics obtained through the system and process of the invention. Furthermore, the heat exchanger system described in that patent relates to a tubular heat exchanger (a line with a water jacket) and not to a shell and tube heat exchanger like those used in the present invention. Brief Description of the Figures of the Invention Figure 1: Flowchart of the invention process where each of the components of the invention system are identified, along with the flow streams involved. Figure 2: Explanation of the condensation system with 2 heat exchangers in series, where the use of part of the fuel produced is indicated, which is being recirculated from the temporary fuel storage tank. Detailed Description of the Invention The process of the invention will be explained through the flow diagram in Figure 1, identifying each of the streams involved in the process and each of the components of the system of the invention. The thermolysis process for obtaining recovered carbon black and fuel from used tires comprises the following stages: a) shred the used tires until they reach pieces of rubber ranging in size from 0.1 to 4 (0.25 cm to 10.16 cm); b) feeding the crushed material (A) to a rotating horizontal cylindrical thermolysis reactor (1), which is surrounded by an outer chamber (2); c) close the reactor (1) and feed the reactor an inert gas (3) preferably gaseous nitrogen, in order to generate an oxygen-free atmosphere (between 99.0% and 99.9%) and maintain a gauge pressure inside the reactor of between 10 and 200 mbar (1 and 20 kPa); d) indirectly heating the reactor (1) with gases (N) from a combustion chamber (4), which are directed to the outer chamber (2); e) gradually increase the temperature from ambient temperature and maintain it in a range of between 250°C and 350°C for a period of between 1 and 4 hours, gasifying the water, all of the lighter hydrocarbons and some of the heavier hydrocarbons; f) increase the temperature again to more than 450°C, achieving the gasification of the heavy hydrocarbon that was still in a liquid state, for a period of between 2 and 4 hours; g) obtain from the reactor assembly (1) and outer chamber (2) a gaseous stream of hydrocarbons (B), combustion gases (0) and recovered carbon black (C); h) cooling the recovered carbon black (C) inside the reactor (1) and extracting the residual hydrocarbons from the recovered carbon black by entrainment with the inert gas (3) and extracting the recovered carbon black (C) from the reactor (1); i) carrying the gaseous hydrocarbon current (B) to a Flash distillation vessel (5), where thanks to the design of the Flash vessel (5) and due to the pressure changes inside it, part of the current remains in the gaseous phase (D) and another part passes to the liquid state (Bl); j) passing the gas stream (D) from the Flash vessel (5) to a heat exchanger system (6), where part of the gas stream is condensed and another part is kept in a gaseous state, finally obtaining a two-phase stream (G) at the end of the passage through the heat exchanger system (6); ινΐΛ / a / zuz i / un oí uu k) carrying the two-phase stream (G) coming out of the exchanger system (6) to a phase separation tank (11) where a separation of the condensate with the gas occurs due to the phase difference of the two-phase stream (G), producing a gas-phase stream (I) and a liquid-phase stream (H); 1) direct the gaseous phase (I) towards a battery of water seals (7), whose current (J) then feeds the combustion chamber (4) to generate the heat needed in the process and make it energy self-sustaining; m) directing the liquid phase (H) to a filtration system (8) to obtain a filtered fuel stream (K) which is stored for sale (M) in a final storage tank (not shown in the figures), where a portion of this filtered fuel stream (K) remains in a buffer vessel (9); and n) use part of the fuel (L) produced and coming from the buffer tank (9) in the co-current cleaning (L1, L2...) of the exchanger system (6). Prior to and during the crushing stage, there is a metal extraction process, for example using a magnetic separator (not shown in Figure 1). In stage e) there is a heat transfer from the external chamber (2) to the reactor (1) where the crushed material (A) is located, which regulates the fuel supply (J) to the combustion chamber (4) through a control loop that takes the temperature signal inside the reactor, to avoid violent processes of rubber sublimation and preventing the increase of excessive gas flows that carry carbonaceous material. The reactor (1) has a temperature sensor system that delivers a signal to the control loop system, thereby regulating the amount of fuel (J) used in the combustion chamber (4) by means of a set temperature, and therefore the amount of combustion gases (N) fed to the outer chamber (2) of the reactor (1). Furthermore, in stage e) a liquid bed is maintained where the liquid / vapor phase is in equilibrium inside the reactor (1). Thermolysis inside the reactor (1) ends when gas generation ceases, after the second temperature increase in stage f), which is monitored by a gas flow sensor. Residence time -9maximum of the crushed material in the reactor (1) is 12 hours. The combustion chamber (4) is capable of working with gaseous or liquid fuel, generating the thermal energy necessary to achieve the operating conditions of the reactor (1), using the combustion gases as a heat source for the reactor. The Flash distillation vessel (5) has a vertical cylindrical design such that its upper part, where the gaseous phase is located, has a larger volume than its lower part, where the liquid phase accumulates. This allows the liquid phase (Bl), separated by the pressure change within the Flash vessel (5), to be returned to the reactor (1). Simultaneously, the entrainment of carbonaceous material in the gaseous stream (D) is prevented by the reduced flow velocity. Consequently, the heavy hydrocarbons present in the liquid phase (Bl) are reprocessed, as the design incorporates an overflow that allows the liquid hydrocarbons to return (Bl) to the reactor. This reduces carbonaceous residues in the final fuel and decreases the particulate matter deposited inside the tubes (14) of the heat exchanger system (6). The combustion gases (N) generated in the combustion chamber (4) pass through the outer chamber (2) of the reactor (1) providing the heat necessary to perform the thermolysis of the crushed rubber material (A). The combustion gases (0) exiting the outer chamber (2) are mixed with fresh air (P) in a centrifugal blower (13) to generate a stream of fresh combustion gases (Q). Part of this stream (Q) of fresh combustion gases is recirculated (Q1) to the combustion chamber (4) to improve energy efficiency and ensure complete combustion of the gases, with this air (P) that has been preheated by the combustion gases (0) that exited the outer chamber (2) of the reactor (1), the remaining fraction (Q2) is released to the atmosphere (10). The water seal battery (7) of stage I) consists of a series of vertical containers with water through which the non-condensed gas (I) passes, acting as a safety system to prevent ignition of the gas. One of these vertical containers of the water seal battery (7) contains a solution of calcium hydroxide or caustic soda, which reduces the sulfur content of the gas stream (I). The heat exchanger system (6) comprises at least two - 10 tube (14) and shell (15) heat exchangers in series (as shown in Figure 2) or in parallel (not shown). In the heat exchanger system (6) used in step j), the following steps are carried out to achieve the cleaning of the inside of the tubes (14), without the need to stop the operation / process: jl) introducing into the gas stream (D) coming from the Flash vessel (5) in co-current, part of the generated fuel (L1, L2...) to the inside of the tubes (14), where the fuel recirculation stream (L1, L2...) enters the inside of the heads (17) of the tubes (14) by means of injectors (16) oriented in co-current direction with the flow of the gas stream; j.2) introduce the cooling water flow (Fl , F2...) from a cooling circuit (12) to the housing (15); and j.3) clean the inside of the tubes (14) thanks to the high pressure with which the recirculated fuel is injected (Ll , L2. . .) and its dissolving capacity, carrying away the material deposited inside the tubes (14). One injector (16) will be provided for every 4 tubes (14) to ensure proper cleaning of the inside of these in each heat exchanger. The recirculation of the fuel stream (L1, L2...) is automatically activated when heat exchange efficiency is lost, which occurs when the temperature difference between the inlet and outlet of the cooling water stream (E, E1, E2) passing through the heat exchanger housings (15) decreases. This cooling water stream (E, E1, E2) is directed to the cooling circuit (12) for return to the heat exchanger system (6). This verification is carried out by sensors. The system and process of the invention obtains as products a recovered carbon black (C) and a liquid fuel (L) whose main characteristics are described below: Recovered carbon black has a quality comparable to the semi-reinforcing carbon blacks currently on the market, thanks to its surface chemistry and rubber-like behavior. Depending on the application, it can partially or totally replace conventional carbon blacks, such as those used where heat dissipation is required. The recovered carbon black obtained can be applied to various rubber items such as motor vehicle components, shoe soles, - 11 hoses; anti-vibration elements; roof covers; conveyor belts; plus black inks for the graphic arts industry; and for black pigment in the plastics industry. One of the main advantages of the recovered carbon black obtained by the invention is that, compared to conventional carbon black production processes, CO2 emissions are considerably reduced. It is estimated that producing 1 ton of recovered carbon black through the process of the present invention generates 130 kg of CO2 compared to the 2.5 tons of CO2 generated by the production process of conventional carbon black, which is equivalent to a 95% reduction in the carbon footprint. The fuel obtained by the invention has the following characteristics: It is a fuel with a calorific value that falls within the range of traditional fuels such as diesel and No. 6 fuel oil. Its low viscosity allows it to be used as an additive to improve the performance of more viscous fuels. Its pour point and cold filter plugging point occur at lower temperatures than traditional fuels, giving it an operational advantage when used in extreme conditions such as low temperatures in mountainous regions. Compared to heavy fuels, this fuel has a lower content of sulfur, carbonaceous material, ash, sediment, and water, resulting in lower emissions of pollutants. The use of this fuel has a neutral fraction of CO2 emissions, because it is obtained from tires that contain biomass (natural rubber) in their composition. The fuel obtained from the thermolysis process can be used in stationary engines, electric generators, boilers to heat water and generate steam, as an additive for heavy fuels, and as raw material for the manufacture of other products. It is a cleaner liquid fuel with an aromatic content exceeding 90%, compared, for example, to the fuel obtained under patent US8137508B2, which has a maximum of 80% aromatics, and the fuel obtained under patent application CN 105694942, which reaches 60%. This high aromatic content allows the fuel to act as a solvent for the material. - 12 solid adhered to the inside of the tubes of the heat exchanger system (6). In addition to the condition of pressure injection of the fuel into the tubes of the heat exchanger system, the fuel obtained performs the cleaning of the inside of the tubes synergistically due to the high aromatic content of the fuel. In the current state of the art, a fuel of brown to black color is obtained mainly due to the higher content of carbonaceous material; the fuel obtained by the invention is of amber to brown color, due to the lower content of carbonaceous material. In those state-of-the-art processes that consider post-treatment of the fuel through distillation and / or the use of catalysts, cleaner fuels are obtained; however, to achieve this, a greater investment in equipment must be made, lower performance is obtained, additional waste is generated, and the operational cost increases. The percentage of carbonaceous residues in the fuel of the invention is between 0.8% and 3% by weight, which is comparable to that obtained in the state of the art, but with the application of various post-treatment techniques, such as the use of distillation or catalysts to improve the quality of the fuel, whereas in the invention there is no post-treatment. Furthermore, the invention relates to a thermolysis system for obtaining recovered carbon black and fuel from used tires, comprising the following components: i. a horizontal rotating cylindrical thermolysis reactor (1), which is surrounded by an outer chamber (2), where the reactor (1) receives the crushed material (A) to be treated, obtaining from this assembly (reactor and outer chamber) a gaseous stream of hydrocarbons (B), combustion gases (0) and recovered carbon black (C); ii. a combustion chamber (4), which indirectly heats the reactor (1) with gases (N) which are directed to the outer chamber (2); iii. a Flash distillation vessel (5), which receives the gaseous hydrocarbon stream (B) from the reactor (1), where thanks to the design of the Flash vessel (5) and due to the pressure changes inside it, part of the stream remains in the gaseous phase (D) and another part passes into the liquid state (Bl); ML / a / zuz i / un oí uu iv. a heat exchanger system (6) that receives the gas stream (D) from the Flash vessel (5), where part of the gas stream is condensed and another part is kept in a gaseous state, finally obtaining a two-phase stream (G) at the end of the passage through the heat exchanger system (6); v. a phase separation tank (11) that receives the two-phase stream (G) coming out of the exchanger system (6), where a separation of the condensate from the gas occurs due to the phase difference of the two-phase stream (G), producing a gas-phase stream (I) and a liquid-phase stream (H); vi. a battery of water seals (7) that receives the gaseous phase (I), generating a current (J) that then feeds the combustion chamber (4) to generate the heat needed in the process and make it energy self-sustaining; vii. a filtration system (8) that receives the liquid phase (H) to obtain a filtered fuel stream (K); and viii. a buffer vessel (9) that stores a portion of the filtered fuel stream (K) from the total fuel that is stored (M) for sale in a final storage tank (not shown in the figures). The system also includes a cooling circuit (12), which keeps the process water circulating through the heat exchange system (6) cool.

Claims

1. - A thermolysis process for obtaining recovered carbon black and fuel from used tires, CHARACTERIZED in that it comprises the steps of: a) shredding the used tires (rubber) to a size of between 0.1 and 4 inches (0.25 cm to 10.16 cm); b) feeding the shredded material (A) into a rotating horizontal cylindrical thermolysis reactor (1), which is surrounded by an outer chamber (2); c) closing the reactor (1) and feeding the reactor an inert gas (3), so as to generate an oxygen-free atmosphere; d) indirectly heating the reactor (1) with gases (N) from a combustion chamber (4), which are directed to the outer chamber (2); e) gradually increase the temperature from ambient temperature and maintain it in a range of between 250°C and 350°C for a period of 1 to 4 hours, gasifying the water, all of the lighter hydrocarbons and some of the heavier hydrocarbons;f) raising the temperature again to over 450°C for a period of 2 to 4 hours, achieving the gasification of the heavier hydrocarbons that are still in a liquid state; g) obtaining from the reactor assembly (1) and outer chamber (2) a gaseous stream of hydrocarbons (B), combustion gases (O) and recovered carbon black (C); h) cooling the recovered carbon black (C) inside the reactor (1) and extracting the residual hydrocarbons from the recovered carbon black by entrainment with the inert gas (3) and extracting the recovered carbon black (C) from the reactor (1); i) carrying the gaseous hydrocarbon stream (B) to a Flash distillation vessel (5), where part of the stream is kept in the gaseous phase (D) and another part is converted to a liquid state (Bl);j) passing the gas stream (D) from the Flash vessel (5) to a heat exchanger system (6), where part of the gas stream is condensed and another part is kept in a gaseous state, finally obtaining a two-phase stream (G) at the end of the passage through the heat exchanger system (6); k) taking the two-phase stream (G) that leaves the heat exchanger system (6) to a phase separation tank (11) where a separation of the condensate with the gas occurs due to the phase difference of the two-phase stream (G), producing a gaseous phase stream (I) and a liquid phase stream (H); l) directing the gaseous phase (I) towards a battery of water seals (7), whose stream (J) then feeds the combustion chamber (4) to generate the heat necessary in the process and make it energy self-sustaining;m) directing the liquid phase (H) to a filtration system (8) to obtain a filtered fuel stream (K) that is stored for marketing (M) in a final storage tank, where a portion of this filtered fuel stream (K) remains in a buffer vessel (9); yn) using part of the fuel (L) produced and coming from the buffer vessel (9) in the co-current cleaning (L1, L2...) of the heat exchanger system (6).

2. The process according to claim 1, CHARACTERIZED in that in step c) the inert gas (3) is gaseous nitrogen, and in this step an oxygen-free atmosphere is generated between 99.0% and 99.9% and maintaining a gauge pressure inside the reactor of between 10 and 200 mbar (1 and 20 kPa).

3. The process according to claim 1, CHARACTERIZED in that in stage i) where, thanks to the design of the Flash container (5) and due to the pressure changes inside it, a part of the hydrocarbon gas stream (B) is kept in the gaseous phase (D) and another part passes to the liquid state (Bl). 4 - The process according to claim 1, CHARACTERIZED in that prior to and during stage a) there is an extraction of metals.

5. The process according to claim 4, CHARACTERIZED in that the extraction of metals is carried out by means of a magnetic separator.

6. The process according to claim 1, CHARACTERIZED in that in step e) there is a heat transfer from the external chamber (2) to the reactor (1), where the crushed material (A) is located, which regulates the fuel supply (J) to the combustion chamber (4) through a control loop that takes the temperature signal inside the reactor (1), to avoid violent rubber sublimation processes and preventing the increase of excessive gas flows that carry carbonaceous material.

7. The process according to claim 6, CHARACTERIZED in that a temperature sensor system is provided in the reactor (1) which delivers a signal to a control loop system, thereby regulating, by means of a set temperature, the amount of fuel (J) used in the combustion chamber (4) and, therefore, the amount of combustion gases (N) fed to the outer chamber (2) of the reactor (1). 8.- The process according to claim 1, CHARACTERIZED in that in step e) a liquid bed is maintained where the liquid phase / vapor phase is in equilibrium inside the reactor (1).

9. The process according to claim 1, CHARACTERIZED in that the thermolysis inside the reactor (1) ends when the gas generation ends, after the second temperature increase in stage f), which is monitored through a flow sensor.

10. The process according to claim 1, CHARACTERIZED in that the maximum residence time of the crushed material (A) in the reactor (1) is 12 hours. 11 - The process according to claim 1, CHARACTERIZED in that the combustion chamber (4) works with gaseous or liquid fuels, generating the thermal energy necessary to achieve the operating conditions of the reactor (1) using the combustion gases as a heat source for the reactor. 12.- The process according to claim 1, CHARACTERIZED in that the combustion gases generated (N) in the combustion chamber (4) pass through the outer chamber (2) of the reactor (1) providing the heat necessary to carry out the thermolysis of the crushed rubber material (A).

13. The process according to claim 1, CHARACTERIZED in that the combustion gases (O) exiting the outer chamber (2) are combined with fresh air (P) in a centrifugal blower (13) to generate a stream of fresh combustion gases (Q), wherein part of this stream (Q) of fresh combustion gases is recirculated (Ql) to the combustion chamber (4) so ​​as to improve energy efficiency and ensure complete combustion of the gases, with this air (P) that has been preheated thanks to the combustion gases (O) that came out of the outer chamber (2) of the reactor (1), and the remaining fraction (Q2) is released to the atmosphere (10).The process according to claim 1, CHARACTERIZED in that the Flash distillation vessel (5) has a vertical cylindrical design such that its upper part, where the gaseous phase is located, has a larger volume in relation to its lower part, where the liquid phase accumulates. This allows the return to the reactor (1) of the liquid phase (Bl) separated by the effect of the pressure change in the Flash vessel (5), preventing the entrainment of carbonaceous material in the stream (D) that remains in a gaseous state, due to the reduction in the speed of this flow. With this, the heavy hydrocarbons present in the liquid phase (Bl) are reprocessed since said design has an overflow, which allows the hydrocarbons in the liquid phase (Bl) to return to the reactor, reducing the carbonaceous residues in the final fuel as well as reducing the particulate matter that is deposits inside the tubes (. 14) of the heat exchanger system (6).

15. The process according to claim 1, CHARACTERIZED in that the non-condensed gas (I) from the phase separation tank (11) passes through the water seal battery (7) of stage I) which consists of a series of vertical containers with water, and which act as a safety system to prevent ignition of the gas.

16. The process according to claim 15, CHARACTERIZED in that one of these vertical containers of the water seal battery (7) contains a solution of calcium hydroxide or caustic soda, reducing the sulfur content of the gaseous current (I).

17. The process according to claim 1, CHARACTERIZED in that the cleaning of the heat exchanger system (6) is carried out by the action of the fuel (L) produced, wherein the heat exchanger system (6) comprises at least two tube (14) and shell (15) heat exchangers in series or in parallel.

18. The process according to claim 17, CHARACTERIZED in that, to achieve the cleaning of the inside of the tubes (14), without stopping the operation / process, the following steps are carried out in the heat exchanger system (6) that is used in step j): j1) Introducing into the gas stream (D) coming from the Flash vessel (5) in co-current, part of the generated fuel (L1, L2...), into the inside of the tubes (14), where the fuel recirculation stream (L1, L2...) enters the inside of headers (17) in the tubes (14) by means of injectors (16) oriented in co-current with the flow of the gas stream; j.2) introducing the cooling water stream (F1, F2...) coming from a cooling circuit (12) into the casing (15); and j.3) clean the inside of the tubes (14) thanks to the high pressure with which the recirculated fuel is injected (L1, L2...) and its dissolving capacity, carrying the deposited material inside the tubes (14).

19. The process according to claim 18, CHARACTERIZED in that the number of injectors (16) will be one for every 4 tubes (14) for proper cleaning of the inside of the tubes (14) of the heat exchangers.

20. The process according to claim 18, CHARACTERIZED in that the recirculation of the fuel stream (L1, L2...) is automatically activated when the efficiency in the heat exchange is lost, which occurs when the difference between the inlet and outlet temperatures of the cooling water stream (E, El, E2.) passing through the housings (15) of the heat exchangers is reduced, where said cooling water stream (E, El, E2.) is directed to the cooling circuit (12) to return to the heat exchanger system (6), where said verification is carried out by means of sensors.

21. A thermolysis system for obtaining recovered carbon black and fuel from used tires, CHARACTERIZED in that it comprises: i. a rotating horizontal cylindrical thermolysis reactor (1), which is surrounded by an outer chamber (2), where the reactor (1) receives the crushed material (A) to be treated, obtaining from this assembly of reactor (1) and outer chamber (2), a gaseous stream of hydrocarbons (B), combustion gases (O) and recovered carbon black (C); ii. a combustion chamber (4), which indirectly heats the reactor (1) with gases (N) which are directed to the outer chamber (2); iii. a Flash distillation vessel (5), which receives the gaseous stream of hydrocarbon (B) from the reactor (1), where a part of the gaseous stream of hydrocarbon (B) is kept in the gaseous phase (D) and another part passes to the liquid state (Bl); iv.a heat exchanger system (6) that receives the gas stream (D) from the Flash vessel (5), where part of the gas stream is condensed and another part is kept in a gaseous state, finally obtaining a two-phase stream (G) at the end of the passage through the heat exchanger system (6); v. a phase separation tank (11) that receives the two-phase stream (G) that comes out of the heat exchanger system (6), where a separation of the condensate with the gas occurs due to the phase difference of the two-phase stream (G), producing a gaseous phase stream (I) and a liquid phase stream (H); vi. a battery of water seals (7) that receives the gaseous phase (I), generating a stream (J) that then feeds the combustion chamber (4) to generate the heat necessary in the process and make it energy self-sustaining; vii.a filtration system (8) that receives the liquid phase (H) to obtain a filtered fuel stream (K); and viii. a buffer vessel (9) that stores a portion of the filtered fuel stream (K) from the total fuel that is stored (M) in a final storage tank for marketing.

22. The system according to claim 21, CHARACTERIZED in that it further comprises a cooling circuit (12), which keeps the process water circulating through the heat exchange system (6) cold.

23. The system according to claim 21, CHARACTERIZED in that the Flash distillation vessel (5) has a vertical cylindrical design such that its upper part, where the gaseous phase is located, has a larger volume in relation to its lower part, where the liquid phase accumulates. This allows the return to the reactor (1) of the liquid phase (Bl) separated by the effect of the pressure change in the Flash vessel (5), preventing the entrainment of carbonaceous material in the stream (D) that remains in a gaseous state, due to the reduction in the speed of this flow. With this, the heavy hydrocarbons present in the liquid phase (Bl) are reprocessed since said design has an overflow, which allows the hydrocarbons in the liquid phase to return (Bl) to the reactor, reducing the carbonaceous residues in the final fuel as well as reducing the particulate matter that is deposited inside the tubes (14) of the heat exchanger system (6). 24.- The system according to claim 21, CHARACTERIZED in that the water seal battery (7) consists of a series of vertical containers with water through which the non-condensed gas (I) passes, acting as a safety system to prevent ignition of the gas.

25. The system according to claim 21, CHARACTERIZED in that the heat exchanger system (6) comprises at least two shell and tube (14) heat exchangers (15) in series or in parallel.

26. The system according to claim 21, CHARACTERIZED in that the system has various sensors, wherein the reactor (1) has a temperature sensor system that delivers a signal to a process control loop system, whereby, by means of a set temperature, the amount of fuel (J) used in the combustion chamber (4) and thus the amount of combustion gases (N) fed to the outer chamber (2) of the reactor (1) are regulated; and furthermore, the reactor (1) has a flow sensor to monitor the completion of thermolysis inside the reactor (1) by registering when gas generation ends.