Integrated process involving direct pyrolysis, stoichiometric combustion and post-combustion and equipment for implementation thereof

Abstract

The invention relates to a process that integrates three techniques or processes, namely direct pyrolysis in a direct flow using heat generated by stoichiometric combustion techniques, in order to perform heat treatment with energy recovery on waste and derivatives thereof, followed by post-combustion of the gases generated in direct pyrolysis and stoichiometric combustion processes to generate heat and utilise the energy thereof. The functional technical composition of the set of integrated equipment (100) for executing the process comprises four basic parts: a means of direct pyrolysis (101) of chlorine-containing waste; a means of stoichiometric combustion (102) of non-pyrolysed and chlorine (Cl)-free waste; a means of post-combustion (103) of combustible gases and vapours generated in the previous processes; and a means of sensing, control and actuation (104).

Description

"INTEGRATED PROCESS OF DIRECT PYROLYSIS, STOICHIOMETRIC COMBUSTION AND POST-COMBUSTION AND EQUIPMENT FOR ITS EXECUTION" Field of invention

[0001] This is a process that integrates three techniques or processes: direct flow pyrolysis using heat generated in stoichiometric combustion techniques, in order to perform thermal treatment with energy recovery in waste and its byproducts; and then, post-combustion of the gases generated in direct pyrolysis and stoichiometric combustion processes to generate heat and utilize its energy.

[0002] The generated gases and vapors then go to an afterburner, generating thermal energy in the form of heated gases, which can be used directly as thermal energy and / or by transforming thermal energy into mechanical energy and, subsequently, into electrical energy.

[0003] Based on this process and its unique processing characteristics, waste with varying moisture, ash, and chlorine content can be treated individually or in blends, without producing air pollutants, as commonly occurs in conventional processes.

[0004] This invention is applicable to any industrial segment that wishes to recover energy from waste and that requires thermal energy, and can be included within the machinery industry, the waste thermal treatment industry, the boiler production industry, as well as the electricity generation industry. Fundamentals of the invention

[0005] The terms and operations used in this document are defined in the following paragraphs, which serve as a glossary for those presented in this document.

[0006] Solid waste is defined as: waste in solid and semi-solid states, resulting from activities of industrial, domestic, hospital, commercial, agricultural, service, street sweeping and basic sanitation origin.

[0007] This definition includes sludge from water treatment systems, sludge generated in pollution control equipment and facilities, as well as certain liquids whose characteristics make their discharge into the public sewage system or water bodies unfeasible, or require technically and economically unviable solutions in light of the best available technology, including volatile liquids and chlorinated or non-chlorinated industrial solvents.

[0008] Energy recovery or energy utilization is defined as: the process of using thermal energy generated from the thermal oxidation of waste destined for combustion, incineration, gasification and / or pyrolysis processes, which fundamentally uses thermal energy for industrial purposes or electricity generation, carried out under controlled conditions and with due environmental control and monitoring.

[0009] The macro-operations of the process defined in the present invention are called: pyrolysis, combustion and, finally, the post-combustion of gases derived from the previous processes.

[0010] In the present invention, the entire combustion process of the combustible materials from the waste is preceded by the pyrolysis process of these wastes, where polymeric materials of vegetable origin, such as cellulosic materials, or synthetic materials such as plastics, fibers, and rubbers, are thermally decomposed by destructive distillation, as it is a process of breaking the chemical bonds of the organic chains by heat.

[0011] Unlike gasification and incineration / combustion, pyrolysis is an endothermic process that requires an external heat source and consists of the thermal degradation of waste in the partial or total absence of an oxidizing agent, oxygen, with process temperatures ranging from 200°C to 600°C and residence time in the reactors depending on the types of polymer chains, particle size and other physical characteristics of the materials.

[0012] In prior art pyrolysis processes, the external heat source applies this heat energy to the material indirectly; that is, the hot gases supplying energy do not touch the materials undergoing pyrolysis, hence the term indirect pyrolysis.

[0013] State-of-the-art pyrolysis processes utilize reactors where heat exchange occurs indirectly, meaning that the heat source does not come into direct contact with the material to be pyrolyzed. Instead, heat from a secondary source warms the outer walls of the reactor, and the reactor walls, in contact with the materials inside the reactor, provide the necessary temperature conditions for the pyrolytic processes.

[0014] Currently, indirect pyrolysis is considered a leading technology for the chemical recycling of plastics, which not only effectively avoids the pollution problems generated in the process of disposing of plastic waste, but also converts plastics into valuable energy and chemical products.

[0015] Unlike the prior art, the process described in this invention involves hot gases acting directly on the material undergoing pyrolysis; that is, the hot gases from stoichiometric combustion come into contact with the material being pyrolyzed, a process known as direct pyrolysis.

[0016] Pyrolysis can produce gases, liquids, waxes, and charcoal, depending on the material being pyrolyzed, the temperature, and the time to which the material is subjected. The process may form all or some of these byproducts.

[0017] The physical phase and chemical composition of the polymeric residues are reversed during this process, as the long-chain polymeric molecules are converted into shorter, less complex molecules.

[0018] The method requires an increase in temperature, a period of time, and the absence of oxygen.

[0019] The design of the pyrolysis reactor is the most crucial factor in determining the pyrolysis product line, where two criteria are critical: maintaining maximum heat transfer and keeping residence time low.

[0020] Pyrolysis is an effective thermochemical method for dismantling or breaking down large polymer molecules into smaller structures with varying boiling points and carbon content.

[0021] In pyrolysis processes, vapors are produced, which are the materials Condensable materials, in the form of liquid oil, solid charcoal, and gases, which are non-condensable materials, vary depending on the type of polymer, degradation temperature, catalyst, and process configuration, with indirect pyrolysis providing higher quality products.

[0022] Many studies have demonstrated the production of high-quality hydrocarbons via pyrolysis from polyethylene (PE), polypropylene (PP), polyethylene terephthalate (PET), and polystyrene (PS).

[0023] However, plastic waste actually contains contaminants, and the presence of other polymers, such as polyvinyl chloride (PVC), can significantly deteriorate the yield and quality of pyrolysis products.

[0024] For example, PVC contains 56.8% chlorine by weight, and the pyrolysis of PVC produces chlorinated hydrocarbons, which poses serious technical challenges to the downstream processing of pyrolysis oil, where, typically, the chlorine content in the cracked oil must be reduced to less than 10 ppm to avoid serious consequences such as corrosion of processing units, poisoning of catalysts, and dioxin emissions into the environment.

[0025] Therefore, reducing the chlorine (Cl) content in pyrolysis oil remains a key challenge for the chemical recycling of mixed plastic waste based on pyrolysis, making the technique prohibitive for materials of unknown origin, such as waste in general.

[0026] Thermogravimetric analysis of PVC typically shows two distinct stages of degradation. The first stage, from 200°C to 340°C, corresponds mainly to the dehydrochlorination reaction that forms HCl and polyene chains. The second stage, from 340°C to 500°C, corresponds to the further degradation of the polyene chain to form carbon and volatile hydrocarbons.

[0027] In this way, the pyrolysis technique presents great potential for the complete degradation of polyvinyl chloride (PVC) present in waste, thus producing gases, liquids and waxes containing chlorine, mainly in the form of hydrogen chloride.

[0028] In this respect, a major technical problem lies in the fact that in the cooling of Gases and vapors after pyrolysis are produced by what is called "de novo" synthesis, where dioxins and furans can be formed through elementary reactions between carbon, hydrogen, oxygen, and chlorine.

[0029] The formation of dioxins, furans, and compounds related to benzene and chlorinated phenols has been observed in residual carbon collected at the exhaust of combustion systems, in a temperature range between 300°C and 400°C, when hydrochloric acid, oxygen, and water are present. These reactions are catalyzed by various metals, metal oxides, and silicates present in the entrained particulate matter, as per: Milligan MS, Altwicker E. The relationship between de novo synthesis of polychlorinated dibenzo-p-dioxins and dibenzofurans and low-temperature carbon gasification in fly ash. Environ Sci Technol 1993; 27:1595-601.

[0030] The experts in the field failed to consider that pyrolysis produces chlorine-free charcoal, since all the chlorine present in the input materials to the pyrolysis reactors has already been volatilized and carried along with the other volatilized byproducts, and that this allows for a subsequent economical combustion of the materials now devoid of chlorine.

[0031] This combustion immediately after pyrolysis becomes much more economical, especially when compared to gasification, which requires much larger equipment.

[0032] The experts in the field also failed to consider that the gases and vapors resulting from pyrolysis and / or combustion can undergo high-temperature combustion, i.e., 1,200°C, transforming the chlorinated materials into hydrochloric acid and elemental chlorine, without the opportunity for "de novo" synthesis to form dioxins and furans.

[0033] In the current state of the art, in order for the vaporized products of pyrolysis to be usable, the heating of the reactors must be done as indirect pyrolysis, that is, when the heating of the reactors is done using hot gases from other combustion processes, these gases cannot come into direct contact with the materials to be pyrolyzed, as this would contaminate these volatiles and require a purification process during the condensation of oils and waxes.

[0034] In the current state of the art, the hot gases used in direct pyrolysis processes have the following technical problems: a) necessary decontamination of oils and waxes; b) dilution of condensable vapors produced in pyrolysis processes in a large mass of hot gases makes the separation of these condensables from the hot gases very expensive and requires large equipment; c) dilution of non-condensable gases produced in pyrolysis processes, and the separation of these non-condensable gases from the hot gases used in the process is much more complex than the separation of condensables, making the direct pyrolysis process unfeasible;d) In the combustion of the material required to produce sufficient heat for pyrolytic endothermic reactions, there will be a need for an excess of oxygen in the combustion, that is, oxygen beyond the stoichiometric level for complete combustion of the fuel, which, in direct pyrolysis systems, may cause the pyrolysis products to burn inside the reactor, making the process unsuitable for producing products with the required quality.

[0035] Unlike conventional methods that involve indirect pyrolysis, the present invention presents an integrated process of direct pyrolysis, stoichiometric combustion, and finally, post-combustion of the generated gases and vapors, where the heat necessary for the pyrolytic reactions enters the pyrolytic reactor through the flow of hot gases from the combustor, making the heat exchange directly, without the need for passage through the walls and / or heat exchangers.

[0036] Direct pyrolysis is possible in the proposed process because the combustible gases and vapors produced in pyrolysis do not need to be of high quality, since they will be immediately consumed in the post-combustion process.

[0037] Remember that gases, that is, non-condensable gases, and vapors, that is, condensable gases, are in counterflow relative to the movement of the waste products.

[0038] The gases and vapors are generated: a) in the combustor by the stoichiometric combustion of the solid products, that is, the chlorine-free coals from pyrolysis; b) in the pyrolysis furnace for the waste.

[0039] From the perspective of experts in the field, stoichiometric combustion is inefficient, a technical problem that does not exist in this invention due to the fact that the gases will be burned in a post-combustion process.

[0040] Another significant difference in the present invention is that a pyrolysis furnace for use with a combustor needs to have a larger passage area so as not to significantly increase the speed of the gases that cause the entrainment of materials in pyrolysis.

[0041] For the sake of clarity, as it is not present in this invention, there is gasification, which can be defined as partial oxidation, that is, with an amount of oxygen below the stoichiometric level, at a high temperature of 500°C to 1400°C and variable pressure between atmospheric pressure and 33 bar, of solid or semi-solid carbonaceous material, such as biomass / wood, waste, coal, among others, into a combustible gas, called synthesis gas, composed mainly of H2 and CO.

[0042] During gasification, most of the feed material is thermally decomposed into gas, but some byproducts are also formed, including tar, charcoal, and ash, and depending on the reactor design and operating conditions, the process can also generate methane and hydrocarbons.

[0043] Incineration, or simply combustion, is any process whose operation is carried out above a minimum temperature of 800°C, capable of promoting total oxidation, that is, the complete burning of waste. This process is usually done with excess air, unlike the combustion process proposed in this invention, which does not use excess air and is better described as a "stoichiometric combustor".

[0044] Incineration or combustion of waste with energy recovery is a fundamental step in the life cycle and management of materials, as it allows for a reduction in the mass and volume of Municipal Solid Waste (MSW), Industrial Solid Waste (ISW), Healthcare Solid Waste (HCW), and Commercial Solid Waste (CW) by up to 95%.

[0045] For this reason, it is considered the most cost-effective approach for waste treatment and landfill area conservation.

[0046] However, conventional reactors and processes invariably produce undesirable and highly toxic byproducts, and the exhaust gases must be treated before being released into the atmosphere.

[0047] The main compounds present in these emissions include: hydrogen chloride (HCl), nitrogen oxides (NOx), carbon monoxide (CO), dioxins such as polychlorinated dibenzo-p-dioxins (PCDD), furans such as polychlorinated dibenzofurans (PCDF), and volatile organic compounds of varying compositions and complexity.

[0048] Conventional incineration plants must be designed and operated in such a way that the combustion gases resulting from the combustion process are subjected to a temperature of at least 800°C for 1.5 seconds, in order to guarantee the proper decomposition of toxic organic substances.

[0049] Temperature requirements increase to 1,100°C for at least two seconds when incinerating hazardous waste with a content exceeding 1% of halogenated organic substances, expressed as chlorine. These conditions are not possible in conventional incineration reactors for processing extremely heterogeneous waste with high moisture content, such as municipal solid waste.

[0050] For this reason, even under these extreme combustion conditions, complex gas treatment processes are necessary in conventional incinerators, that is, those of the state of the art, because due to the large variation in the gravimetric chemical compositions of the waste, which in these reactors are found in all phases during processing, that is, under the same conditions they are present in the solid, liquid and gaseous states, the reactions are heterogeneous.

[0051] With regard to state-of-the-art incinerators, it can be said that they have been widely installed throughout the world, and that the main problem lies in the invariable production of dioxins and furans, resulting from the presence of chlorine in the waste, in addition to the presence of other unburned volatile organic compounds.

[0052] Therefore, in the case of combustion of chlorine-free materials, the combustion process can rely on a much simpler and more economical gas treatment system, both in terms of Capital Expenditures (Capex) and Expenses. Operational, also known as Opex.

[0053] Therefore, removing chlorine from waste before combustion processes presents the greatest technological challenge for applying this energy recovery technique as an environmentally sound solution.

[0054] Afterburn or post-combustion is characterized by a zone exclusively for the combustion or oxidation of combustible gases.

[0055] For post-combustion, oxygen is introduced into a reactor with a specific morphology designed to create high turbulence between the combustible gases and the oxygen oxidant.

[0056] Afterburner chambers, when receiving combustible gases with low or no calorific value, as is the case with stoichiometric combustion gases, require the use of "auxiliary fuels" to provide the carbon and hydrogen necessary to supplement the calorific value of the stoichiometric combustion gases and obtain temperatures capable of promoting the ignition and complete oxidation of unburned fuels in the combustion chamber.

[0057] Therefore, in conventional post-combustion processes, carried out in conventional incinerators, there is a need to inject auxiliary fuels, which ends up increasing the cost of the process and sometimes making it unfeasible due to the high cost of these auxiliary fuels.

[0058] In the afterburner chamber of the process proposed in this document, the auxiliary fuel needed to achieve ideal afterburning conditions is produced in the pyrolysis stage of the integrated process, in the pyrolytic reactions of direct pyrolysis, where the blown oxygen reacts in a combustion reaction with the products of pyrolysis and stoichiometric combustion. This is an exothermic reaction, releasing thermal energy that provides heat to the other stages of the process and mainly produces CO2, H2O, and N2 with high thermal energy.

[0059] For the theoretical stoichiometric combustion of any conventional fuel to occur, according to its composition, a specific quantity is required and The amount of oxygen, typically from the air since it is the common source, needed to theoretically achieve a complete, or stoichiometric, reaction.

[0060] A quantity of oxygen less than the stoichiometric amount will produce incomplete combustion, that is, with a quantity of oxygen below the stoichiometric level and, therefore, a loss of potential heat.

[0061] And, a quantity of oxygen greater than the stoichiometric amount generates excessive losses of combustion gas and temperature.

[0062] Conventional combustion processes require excess oxygen in the reactors, which can reach up to 50% depending on the fuel, in order to compensate for process imperfections and ensure the collisions necessary for the effective occurrence of carbon oxidation chemical reactions.

[0063] Examples of oxygen-deficient or sub-stoichiometric reactions: a) partial oxidation of carbon: C + O2CO ; b) partial oxidation of methane: CH4+ - O2-> CO + 2H2O .

[0064] Examples of stoichiometric reactions: a) complete oxidation of carbon monoxide: CO + O2CO2; b) complete oxidation of methane: CH4 + 2O2 → CO2 + 2H2O.

[0065] Examples of reactions with excess oxygen: a) complete oxidation of carbon monoxide: CO + O2 → CO2 + O2; b) complete oxidation of methane: CH4 + 3O2 → CO2 + 2H2O + O2.

[0066] In this invention, given the mass flow rate of gases and vapors carried to the afterburner, it must have larger dimensions than conventional ones.

[0067] The state of the art presents pyrolysis processes and incineration processes for waste and its byproducts in separate equipment, that is, processes or equipment dedicated to pyrolysis to obtain its byproducts, and, separately, processes or equipment dedicated to incineration to obtain its byproducts.

[0068] All pyrolysis technologies applied to MSW (Municipal Solid Waste) have the technical problem... The decision is to only accept pre-treated MSW, instead of raw MSW in its original state, due to the fact that chlorine contamination present in MSW will also be present in the volatile byproducts of pyrolysis, suggesting that pre-treatment is a necessary step for pyrolysis technology, which makes it economically unviable for the treatment of this type of material.

[0069] Pre-treatment typically includes the separation of undesirable materials, mainly those containing chlorine, and size reduction, sometimes with a drying step prior to the pyrolysis reactor to reduce the moisture content of the materials feeding the reactor.

[0070] The reason why state-of-the-art pyrolysis reactors only accept homogeneous materials or materials with little variation in their gravimetric composition is that the pyrolysis products (oils and coals) depend on the characteristics of the input materials in the reactor. In other words, if materials with known characteristics enter, byproducts with known characteristics will be produced. However, in the case of MSW (Municipal Solid Waste), where there is the technical problem of extreme variation in gravimetry and moisture, the byproducts of this processing only alter their physical and chemical characteristics, but remain waste, since they have no industrial applicability.

[0071] The integrated process presented in this patent application offers solutions for pyrolysis byproducts of heterogeneous materials with high moisture content, such as MSW (Municipal Solid Waste), but it can also receive other residues from other sources, since it presents suitable combustion solutions for total oxidation of both, whether it is the combustion of charcoal derived from pyrolysis or post-combustion in high turbulence for volatiles originating from pyrolysis.

[0072] State-of-the-art incinerators aim to achieve complete combustion by employing temperatures in the range of 800°C to 1,090°C, to capture the generated heat, and to manage emissions through complex and costly pollution controls.

[0073] The ashes produced are typically disposed of in landfills and are often treated as hazardous waste.

[0074] Municipal solid waste incinerators have been the subject of research involving the formation of Air pollutants called Polychlorinated dibenzo-p-dioxins (PCDD) and Polychlorinated dibenzofurans (PCDF), commonly known as dioxins and furans, since their concentrations are found in both fly ash and gas streams from these processes, have values ​​above those permitted by environmental legislation.

[0075] Among the factors that can contribute to the formation of dioxins and furans, provided they are processed simultaneously, are the following: a) carbon source: a carbon source is necessarily required for the formation of dioxins and furans, which may originate from a solid carbon matrix of fly ash, more specifically deformed graphitic structures such as soot, charcoal, sugar coal, or in pyrolysis and gasification products; b) oxidizing atmosphere: molecular oxygen present in the gas stream is essential for the synthesis to occur, however, it is not clear whether O2 is actually incorporated into the structures of dioxins and furans, the most accepted hypothesis is that the oxygen concentration must be around 10% to 15% to favor the synthesis;c) Lower temperatures than combustion zones: they typically form under conditions of incomplete combustion, conditions that favor complex reactions occurring in the fly ash matrix in the presence of chlorinated compounds, catalysts, and a carbon source within a temperature range between 200°C and 500°C; d) Chlorine source: the chlorine sources for the formation of pollutants are possibly derived from organic and inorganic compounds contained in solid waste: a. organic chloride: from PVC, poly(vinyl chloride), pesticides, herbicides, etc.; b. inorganic chloride: NaCl, KCl, among others.

[0076] Unlike the prior art, the present invention, in relation to the previous paragraph, presents: a) in the temperature reduction regions, after the post-combustion zones, all the carbon that existed in the residues was subjected to total oxidation, so that there is no longer any carbon available for "de novo" synthesis that contributes to a) Dioxin production occurs, although the other conditions are present; b) The only zone where excess oxygen is found is in the afterburner chamber; however, this chamber operates at temperatures up to 1,200 °C for a period of up to 2 seconds.Under these temperature conditions, dioxin formation syntheses are not possible, although the other conditions are present; c) temperature conditions, between 200°C and 500°C, occur only in two distinct zones: first, in the pyrolysis furnace region where there is no excess oxygen for dioxin formation, and second, in the gas cooling region after the afterburner chamber, where there is no carbon available for these syntheses, although the other conditions are present; d) all chlorine is evaporated along with the other volatiles from the pyrolytic processes, so that the coals resulting from pyrolysis, upon entering the stoichiometric combustor, are free of this element, and therefore there are no conditions for dioxin formation in this zone of the process, although the other conditions are present.

[0077] It is a fact that the presence of chlorine in urban waste cannot be controlled, and incineration, as is the state of the art, becomes prohibitive in developing countries, mainly due to the high cost of gas treatment for the removal of dioxins and furans.

[0078] These types of equipment commonly require large volumes of waste and its byproducts, with volumes starting at 800 tons / day being economically viable. This is mainly due to the need for greater process stability, since all reactions—drying, pyrolysis, gasification, and combustion—occur in the same chamber and under the same conditions of pressure, temperature, turbulence, and oxidizing agent, i.e., oxygen.

[0079] Municipal solid waste incinerators produce, in addition to normal combustion gases, CO2, H2O, and N2, as well as products of incomplete combustion, such as volatile organic compounds and organic synthesis products, such as dioxins and furans. The treatment of these gases makes the process excessively expensive and unfeasible for small and medium-sized plants, considering a capacity of 100 tons / day for small plants and 400 tons / day for medium plants.

[0080] The integrated process presented in this document offers solutions to the problems of conventional waste incinerators.

[0081] In the state-of-the-art incineration processes described above, conditions exist that lead to the formation of dioxins and furans, requiring complex gas treatment systems comprised of several stages, including the extraction of gaseous pollutants using an activated carbon column.

[0082] These adsorption treatments only remove some of the pollutants from the exhaust gases, but these pollutants are not destroyed and remain in the adsorbent medium. Consequently, they must be sent for treatment and disposal that are costly.

[0083] Thus, complex gas treatment systems required in the state of the art, in addition to representing a very high investment, acquisition and installation cost (capex), also involve operational expenses and expenditures (opex).

[0084] These costs make the incineration process unfeasible in developing countries and even in developed countries, due to the minimum dimensions required for conventional incineration processes without the prior pyrolysis step in a reactor dedicated to this operation, as is the case with this present invention.

[0085] Incineration equipment, incinerators or simply combustors, are furnaces, basically composed of a combustion chamber, where waste is fed at a pre-defined rate and the controlled burning process occurs, and a post-combustion chamber, where the controlled burning of CO and organic substances contained in the gases from the combustion chamber is completed.

[0086] Incineration or combustion furnaces can have the following configurations: a) incineration on fixed or mobile grates: this is the most commonly used for raw MSW, allowing operation with materials of various particle sizes, where, during the movement of the waste on the grate, the material is heated and undergoes drying, resulting in the loss of volatile organic compounds and the combustion of the carbonaceous residue, with air also being introduced above the grate at high temperatures. a) speed for creating a region of high turbulence and promoting its mixing with the gases and vapors generated during combustion; b) circulating or bubbling fluidized beds: these are most commonly used for sewage sludge; the waste, which must be crushed to a diameter equal to or less than 25 mm, is incinerated in suspension in a bed of inert particles such as sand and ash, blown with primary combustion air; c) rotary kiln: this is most commonly used for industrial waste and waste quantities exceeding 24 tons / day.

[0087] Not present in the prior art incineration process is the vibrating grate incineration furnace, which is also included as one of the incineration methods in the present invention.

[0088] The vibrating screen assembly is of the membrane wall type, without the use of cast steel beams that make up the moving screens, and is cooled by the water recirculation system itself, with the perforation for the flow of oxidizing air for incineration being made in the fins.

[0089] The non-use of cast beams, i.e., moving grates, eliminates a focus of maintenance, and the use of recirculating water in counterflow with the processed materials causes the membrane wall of the vibrating grate to operate at a more suitable temperature to promote combustion at various points along the flow of the incinerated material.

[0090] The purpose of water recirculation is to transfer heat from the hotter incineration zones at the end of the vibrating screen to the cooler zones at the beginning of the vibrating screen by recirculating water under the screen through membrane walls.

[0091] Better control of heat distribution in vibrating screens increases the efficiency of the incineration process.

[0092] Combustion processes that include a preliminary pyrolysis step, capable of removing chlorine from waste in a reactor dedicated to this operation, as is the case with this present invention, represent a novel technological solution for an effective, economical, and environmentally sound treatment of the largest environmental liability problem on the planet.

[0093] In the state of the art, the same inventor of the present invention presents invention BR 102022005707-9, entitled "INTEGRATED PROCESS OF DIRECT PYROLYSIS, STOICHIOMETRIC COMBUSTION AND POST-COMBUSTION AND EQUIPMENT FOR ITS REALIZATION", which specifically deals with a process that integrates the pyrolysis process in a rotary kiln with a gasification process on grates.

[0094] This process and equipment present significant problems and limitations regarding the treatment of waste with high chlorine content and in meeting the needs of a market lacking processes with low investment costs.

[0095] Brazilian invention BR 102022005707-9 presents gasification as the main way to generate combustible gases and vapors. Although it is an excellent process from the point of view of waste treatment, its application is limited to waste with high chlorine content, as it does not provide conditions for the formation of dioxins and furans. However, in order to carry out controlled substoichiometric reactions at low temperatures, on average 650 °C, large internal areas are needed in the reactors so that, at these temperatures, these solid and low-density materials can be accommodated for long periods of time until all their contents are gasified.

[0096] The explanation is that in a reactor operating at temperatures of 650 °C, as is the case with gasifiers, the processing speeds of the materials are much lower than in equipment operating at temperatures above 900 °C, as is the case with incinerators, which can reach 1,090 °C. Therefore, with such a low speed, the internal volume required to accommodate the same mass of waste compared to high speeds resulting from higher temperatures is much greater. This makes the implementation cost of a gasifier much higher than that of an incinerator, considering that these reactors operate in aggressive environments and their construction materials are expensive.

[0097] Given the requirement for large-scale equipment for these gasification reactors, the equipment and process of BR 102022005707-9 are very expensive.

[0098] The need for additional construction materials increases the cost of this solution. They are resistant to harsh environments, sometimes making the process economically unfeasible.

[0099] In invention BR 102022005707-9, since the products of pyrolysis, prior to the gasification process, generate coals free of the element chlorine, it is not necessary to implement a complex gasification process and it can be replaced by a stoichiometric combustion process, which is much simpler, more thermodynamically efficient, with much smaller internal areas due to the high processing temperatures, and consequently with much lower costs.

[0100] The process described in BR 102022005707-9 presents a single model of pyrolysis in a rotary drum, moving grate gasifier, limiting the processes to these equipment models and ignoring the fact that other types of equipment can also be integrated into the processes, with greater efficiency and better adapted to certain types of materials.

[0101] For example, pyrolysis is limited to "rotary drum" type reactors, which, although a good process, can be replaced by a drum process with internal augers, better suited to certain types of waste, but not to all of them.

[0102] Regarding the gasification reactor of invention BR 102022005707-9, it is limited to the use of moving grate reactors only, which, although an excellent process, can be replaced by fluidized beds, circulating beds or vibrating grates, which can offer much better conditions for preheated coals from pyrolysis of waste and free of chlorine.

[0103] In the process proposed in the current document, the use of reactors in addition to rotary kilns, as well as helical furnaces, is foreseen for pyrolysis equipment, making the processes much more flexible and suitable for the various types of waste that can be properly processed.

[0104] Also in the proposed process, the equipment for processing pyrolysis coals is expected to use, in addition to moving grate reactors, vibrating grate, fluidized bed or circular bed reactors, depending on the characteristics of the coals produced in the pyrolysis processes, making the processes much more flexible and suitable for the various types of waste that can be properly processed.

[0105] In summary, the unprecedented integrated pyrolysis and combustion process, compared to that presented in BR 102022005707-9, is much more versatile because it is not limited to a single type of pyrolysis reactor model, the rotary drum, nor to a single type of gasification reactor, the moving grate reactor, knowing that the waste can vary in its origin and its physical and chemical characteristics demand processing methods adapted to these characteristics.

[0106] In addition to the possibility of applying different techniques compatible with various types of waste, this integrated pyrolysis and combustion process, compared to that presented in BR 102022005707-9, operates with combustion reactors that operate at much higher speeds, making the equipment much smaller and less expensive to process the same mass of waste in a gasifier.

[0107] The integration of pyrolysis and combustion is much more suitable for meeting the immense demand for waste treatment, which processes materials with very low added value and consequently does not have large investment resources, which, although being one of the biggest environmental challenges, does not actually generate much economic interest.

[0108] The development of new techniques capable of not producing these pollutants presents itself as the only alternative for the effective treatment of urban solid waste in developing countries. Novelty and technical effect achieved

[0109] As stated at the beginning of this document, this invention comprises a process that uniquely integrates three techniques or processes: a) direct flow pyrolysis using heat generated from combustion techniques to perform thermal treatment with energy recovery from waste and its byproducts; and b) post-combustion of gases generated from direct pyrolysis and stoichiometric combustion processes to generate heat and utilize its energy, resulting in: a) an integrated process that allows for the thermal treatment of waste... a) Different origins, in different particle sizes, such as fine, powdered, pasty, sludge and liquid residues that can be treated individually or in blends with other residues such as urban, commercial or industrial solid waste, health and basic sanitation waste, with different contents of the element Chlorine (Cl); b) Elimination of the entry of Chlorine (Cl) and / or chlorinated compounds into the combustor, through the pyrolytic decomposition of materials containing this element in the direct pyrolysis process, so as not to provide conditions for the generation of dioxins and furans during stoichiometric combustion, as commonly occurs in conventional incinerators; c) An integrated process that allows the production of pyrolytic gases and oils from residues containing the element chlorine, without leaving a carbon liability that ends up without being used;d) a solution so that the coal produced in the direct pyrolysis process, once free of chlorine, can be consumed in the downstream stoichiometric combustion process, for the production of thermal energy to be consumed in the direct pyrolysis reactions; e) the operating conditions of both direct pyrolysis and combustion and post-combustion do not provide conditions for the production of dioxins and furans, even in residues with different chlorine contents; f) burning of the gases and vapors produced in the direct pyrolysis chamber mixed with the gases from the stoichiometric combustion in an integrated post-combustion system, ensuring complete combustion and no generation of pollutants;g) a process with perfect post-combustion, which uses pyrolytic gases and vapors as auxiliary fuel, with high turbulence, average temperatures of 1,200°C and a retention time of up to 2 seconds, eliminating the need for complex combustion gas treatment systems, giving greater economic and environmental viability to the process; h) post-combustion with total oxidation of the carbon atoms present in the pyrolytic vapors mixed with the stoichiometric combustion gases in the post-combustion chamber, also eliminates the incidence of graphitic layers; degenerate compounds present in microcrystalline carbons resulting from incomplete combustion, where the absence of these compounds minimizes the conditions for "de novo" synthesis for the formation of dioxins and furans during cooling in energy recovery systems; i) the use of pyrolysis vapors as auxiliary fuel in the afterburner chamber provides excellent combustion conditions without the need to use third-party auxiliary fuel sources; j) the use of rotary or helical furnaces with diameters larger than those for indirect pyrolysis, suitable for receiving heat directly, i.e., in direct contact between the materials to be heated until their pyrolytic degradation and the gaseous fluid containing the thermal energy necessary for these endothermic reactions;k) the material supply system in the direct pyrolysis stage, which includes a set of mechanical valves to ensure sealing against air intake or gas exhaust from the process, since the material intake region coincides with the extraction region of the mixture of combustion gases and vapors containing Chlorine (Cl) from the pyrolysis and combustion processes; l) the connection between the moving parts of the pyrolysis means and the material intake and gas extraction region, as well as the coal outlet and the stoichiometric combustor intake, are designed to ensure a seal so as not to allow gas leakage or false air intake; m) pressure control below local atmospheric pressure, suitable for direct pyrolysis and stoichiometric combustion processes, by an efficient suction system, provided by the gas and vapor extraction means, bringing the pyrolysis and combustion gases and vapors to the post-combustion chamber;n) pressure exerted by the mixture of combustible gases and air that allows this mixture to enter the afterburner chamber with pressure, touching the walls and thus facilitating turbulence and combustion. [001 10] The gases and vapors generated in stoichiometric combustion and direct pyrolysis go to an afterburner, generating thermal energy in the form of heated gases, which can be used directly as thermal energy and / or by transforming thermal energy into mechanical energy and, subsequently, into electrical energy. [001 1 1] Therefore, the present invention, called “INTEGRATED PROCESS OF DIRECT PYROLYSIS, STOICHIOMETRIC COMBUSTION AND POST-COMBUSTION AND EQUIPMENT FOR ITS REALIZATION”, with the integration of the pyrolysis process, which processes the waste before it enters the stoichiometric combustor at inlet gas temperatures of up to 800°C, in a direct process, in counterflow to the movement of the waste, and which under these conditions causes the volatilization of all the chlorine present in the waste, the combustor will process only materials derived from waste and free of chlorine, so that without the presence of this precursor, the synthesis of the pollutants dioxins and furans cannot occur in the combustor, dispensing with complex gas treatment systems. [001 12] The present invention also offers a complete destination for waste processed by the pyrolysis technique, which generates charcoal that ends up having no application or use when derived from waste containing heavy metals or other organic molecules. [001 13] The main novelty of the invention “INTEGRATED PROCESS OF DIRECT PYROLYSIS, STOICHIOMETRIC COMBUSTION AND POST-COMBUSTION AND EQUIPMENT FOR ITS REALIZATION”, comprises the integration of three distinct processes that enable the optimization of the pyrolysis technique, namely the direct pyrolysis process, the stoichiometric combustion process, and the post-combustion process of combustible gases. [001 14] Direct pyrolysis process: pyrolysis, which is commonly used in reactors where heat exchange is done indirectly, is now in the present invention converted to a direct method, where the heating fluid passes through the inside of the reactor, coming into contact with the material being pyrolyzed. [001 15] Such a pyrolysis furnace must be sized to receive a larger volume of gases, mixing with the vapors produced in pyrolytic processes, increasing its efficiency in terms of the effectiveness of the mass of waste treated, decomposing and volatilizing molecules and polymers, including polymers containing the element chlorine, producing solid byproducts free of this element. [001 16] Remember, another significant difference of the present invention is that the oven of Pyrolysis equipment for use with a stoichiometric combustor has a larger passage area to avoid significantly increasing the velocity of the gases that cause material entrainment during pyrolysis. [001 17] Stoichiometric combustion process: the combustion or incineration technique is commonly used in reactors that operate with excess combustion air; in this proposed process, it now becomes a stoichiometric operation, which, due to the fact that it processes chlorine-free materials derived from the pyrolysis process, can operate in less oxidative environments, and in cases where there is not perfect combustion, its gases will still undergo a post-burning process in extreme conditions. [001 18] The post-combustion technique: unlike conventional post-combustion techniques that also operate only with gases, but which commonly use an auxiliary fuel to reach temperatures above 1,100 °C in order to fully degrade volatile organic molecules, this proposed process now uses the pyrolytic vapors produced in the process as an auxiliary fuel. [001 19] Thus, the proposed post-combustion technique guarantees temperature, turbulence, and oxidative environment conditions in which all carbon atoms present in the mixture containing pyrolysis vapors and stoichiometric combustion gases will be fully oxidized to carbon dioxide, and once oxidized, they do not offer the opportunity for the production of dioxins and furans in "de novo" synthesis during the cooling of gases from downstream energy recovery processes, which significantly increases the efficiency of the heat treatment. Brief description of the drawings

[0120] In both the drawings and this descriptive report, the indicative numbers of the elements are divided into: a) numerical reference signals with values ​​less than 100 (one hundred): these are materials that enter or leave the equipment of the processes and stages of modification of these materials within the processes; b) numerical reference signals with values ​​of 100 (one hundred) and above: these are equipment or parts thereof.

[0121] In the diagrams of Figures 1, 2, and 3, the arrows: a) in thick solid lines show the direction of mass flow of waste; b) in medium solid lines show the direction of mass flow of gases and vapors; c) in dashed lines show the direction of mass flow of refrigerant fluid; d) in dashed lines show the direction of flow or heat transfer in thermal exchanges. Figure 1 presents a block diagram of the waste stream. Figure 2 presents a block diagram of the flow of gaseous materials. Figure 3 presents a block diagram of the flow of waste and gaseous materials, as well as the heat flow. Figure 4 shows a schematic drawing of a set of equipment 100. Description of the invention

[0122] In this invention, the set of INTEGRATED EQUIPMENT (100) has its functional technical composition comprising 04 basic parts: a) a direct pyrolysis means (101) of chlorine-containing waste; b) a stoichiometric combustion means (102) of non-pyrolyzed and chlorine-free (Cl) waste; c) a post-combustion means (103) of the combustible gases and vapors generated in the previous processes; d) a sensing, control and actuation means (104).

[0123] Direct pyrolysis means (101) of chlorine-containing waste comprise: a) rotary kiln; b) helical furnace; c) any other direct pyrolysis means currently or in the future may be used.

[0124] In turn, for the invention to provide the desired technical effects, the direct pyrolysis medium (101) used must contain at least: a) a means for loading waste (101.1) that is leak-proof; b) a vacuum gas extraction point (101.2); c) a sealing means (101.31) with the waste loading means (101.1); d) a sealing means (101.32) with the stoichiometric combustion means (102); e) a passage opening (101.4) hermetically connected to the passage opening (102.4) that is: a. for the passage of gases (20.4) from the stoichiometric combustion means (102) to the direct pyrolysis means (101); b. for the passage of waste (10.2) from the direct pyrolysis means (101) to the stoichiometric combustion means (102); f) a means for moving waste (101.5) in direct pyrolysis; (g) at least one sensor kit (101.6) with each kit containing: a. a pressure transmitter (101.6.1); b. a temperature transmitter (101.6.2); c. an O2 analyzer and transmitter (101.6.3).

[0125] Waste loading means (101.1) comprise: a) actuated gate valve; b) rotary valve; c) tilting valve; d) feed screw; e) any other waste loader (101.1), leak-proof when gas leakage is present or may be used in the future.

[0126] The sensor kits (101.6) provide data from the direct pyrolyzer (101) to the control system (104) which acts by actuators: a) in the feed medium (101.1) controlling the volume of waste (10) fed, and; b) in the movement medium (101.5) of the waste in direct pyrolysis controlling the mixing and speed of passage of the waste (10.1); c) in the power of the gas extraction system (103.1).

[0127] The means of moving waste in direct pyrolysis (101.5) depend on the type of pyrolysis furnace (101) adopted, comprising: a) blades or paddles in rotary furnaces; b) rotating propeller in helical furnaces; c) any other waste mover (101.5) currently or in the future may be used.

[0128] The stoichiometric combustion means (102) of pyrolyzed residues comprise: a) moving grate combustor; b) vibrating grate combustor; c) fluidized bed combustor; d) any other stoichiometric combustion means currently or in the future existing may be used.

[0129] In turn, for the invention to provide the desired technical effects, the stoichiometric combustion medium (102) used must contain at least: a) a cooling medium (102.1) for temperature control of the exhaust gases from the stoichiometric combustion medium (102); b) an atmospheric air insufflation medium (102.2); c) a vacuum gas extraction point (101.2); d) a sealing medium (102.3) with the pyrolysis medium; e) a passage opening (102.4) hermetically connected to the passage opening (101.4) that is: a. for the passage of gases (20.4) from the stoichiometric combustion medium (102) to the direct pyrolysis medium (101); b. for the passage of residues (10.2) from the direct pyrolysis medium (101) to the stoichiometric combustion medium (102); f) a means of moving (102.5) the residues in stoichiometric combustion; g) a means of extracting ash (102.6); h) at least one sensor kit (102.8) in the stoichiometric combustion area with: a.a pressure transmitter (102.8.1); b. a temperature transmitter (102.8.2);. c. an O2 analyzer and transmitter (102.8.3). i) a sensor kit (102.9) in the outlet area of ​​the stoichiometric combustor (102) with at least: a. a pressure transmitter (102.9.1); b. a temperature transmitter (102.9.2); c. an O2 analyzer and transmitter (102.9.3).

[0130] The cooling medium (102.1) may be: a) over the entire bed of burning material in the stoichiometric combustion medium (102), removing heat both by conduction of gases and vapors and by radiation from the combustion; b) at the outlet of the stoichiometric combustion medium (102), removing heat only by conduction of gases and vapors.

[0131] The sensor kits (102.8) and (102.9) provide data from the stoichiometric combustor (102) to the control system (104) which acts by actuators: a) in the feed medium (101.1) controlling the volume of residue (10) fed, and; b) in the movements of the moving medium (102.5) of the residues in stoichiometric combustion applied to the residues in combustion (10.3) controlling the mixture and speed of passage of these; c) power of the blower of the gas extraction system (103.1); d) oxygen concentration to ensure that the combustion reactions are stoichiometric.

[0132] The means of moving (102.5) the residues in stoichiometric combustion depend on the type of pyrolysis furnace (101) adopted, comprising: a) moving grates in grate combustors; b) vibration in vibratory combustors; c) solid / air mixture in fluidized beds; d) any other residue mover (102.5) currently or in the future may be used.

[0133] The methods of ash extraction (102.6) from stoichiometric combustion can to be dry sealed with a water seal and comprise: a) screw conveyor; b) Redler type chain conveyor; c) any other ash mover (102.6) currently or in the future may be used.

[0134] It is explained in due course that the cooler (102.1) may use any fluids as a heat exchange medium, such as: a) water; b) thermal fluid; c) air; d) any other fluid for direct heat exchange currently or in the future may be used.

[0135] For temperature control of gases (20.4) at the reactor outlet (102), cold fluid (20.1) is introduced and hot fluid (20.2) is introduced, where the energy extracted by the cooler (102.1) can be used in a plant outside the invention or in the invention's own plant, such as for pre-drying residues or preheating for the steam boiler.

[0136] The means of post-combustion (103) of the generated combustible gases and vapors comprise: a) torsional post-combustion chamber; b) any other means of post-combustion currently or in the future may be used.

[0137] In turn, for the invention to provide the desired technical effects, the post-combustion medium (103) used must contain at least: a) an atmospheric air supply medium (103.1); b) a means of extracting combustion gases for their energy recovery (103.1); c) a sensor kit (103.2) in the after-combustion outlet area with at least: a. a pressure transmitter (103.2.1); b. a temperature transmitter (103.2.2); c. an O2 analyzer and transmitter (103.2.3).

[0138] The sensor kit (103.2) provides afterburner data (103) to the control system (104) which acts by actuators on the atmospheric air flow (50) to ensure that combustion reactions are complete and controlled with excess oxygen of at least 3%.

[0139] The gas extraction means (103.1) are those that provide vacuum within the direct pyrolysis medium (101) and stoichiometric combustion medium (102) of the INTEGRATED EQUIPMENT set (100), in order to provide a countercurrent flow of gases and vapors in relation to the movement of the process waste, comprising: a) centrifugal fan (103.12) that fulfills the function of upstream exhaust and downstream blower, promoting at point (101.2) vacuum and exhaust of combustible gases and vapors (20.6) and directing these gases and vapors to the post-combustion means (103), where the gases pass through the inside of the fan; b) Venturi system (103.11) with blower providing atmospheric airflow for the formation of the Venturi effect in the Venturi system, promoting at point (101.2) vacuum and exhaust of combustible gases and vapors (20.6) and directing these gases and vapors to the post-combustion means (103); c) any other means of gas extraction currently or in the future may be used.

[0140] It should be understood that all components of the integrated equipment set (100) must be airtight, preventing unwanted flows, especially of air, gases and vapors, between the environment and their internal parts.

[0141] The following paragraphs describe the flows of solid, pasty and liquid materials in the direct pyrolysis medium (101).

[0142] As shown in Figure 1, the direct pyrolysis medium is continuously fed. (101) with the Waste (10) by means of material feeder and doser and gas removal (101.1).

[0143] In the separation region, residues (10) and combustible gases and vapors (20.5) coexist.

[0144] The material feeding and metering and gas removal means (101.1) allows removal of combustible gases and vapors (20.6) from its upper part and, from the lower part, directing the residues (10) to the beginning of the direct pyrolysis medium (101).

[0145] The mass of gases and vapors (20.5), which are hot and free of oxygen, transfer heat to the mass of waste in direct pyrolysis (10.1), there being no incineration or combustion of the materials due to the absence of oxygen in the environment.

[0146] The non-pyrolyzed residues (10.2) are directed to the stoichiometric combustor (102), where the material becomes what is known as stoichiometric combustion material (10.3).

[0147] At the end of stoichiometric combustion, ash remains (10.4), which is directed out of the equipment by the ash extraction means (102.6) and destined as ash (10.5) for industrial landfill or for use in some other process.

[0148] The flow of gases and vapors in the invention, which is counterflow to the flow of waste, will now be described.

[0149] In the stoichiometric combustor (102) the residue in stoichiometric combustion (10.3), receiving external air (50), enters stoichiometric combustion, an exothermic reaction, which generates oxygen-free gases with high thermal energy (20.3).

[0150] The gases (20.3) at this stage will be at too high a temperature to be used as an energy source for the direct pyrolysis to be carried out in the pyrolysis furnace (101).

[0151] For this reason the stoichiometric combustion gases (20.3) are free of oxygen and must pass through the cooler (102.1) becoming slightly cooled gases (20.4), which are directed to the direct pyrolysis furnace (101).

[0152] In the direct pyrolysis furnace (101) the slightly cooled gases (20.4) both give up thermal energy for direct pyrolysis and receive the gases and vapors (20.5) from this pyrolysis, thus generating a mixture of gases and vapors (20.6).

[0153] Therefore, the composition of gases and vapors (20.6) is the sum of the slightly cooled stoichiometric combustion gases (20.4) with the gases and vapors from direct pyrolysis (20.5).

[0154] The mixed gases and vapors (20.6) are drawn into the upper part of the medium. material feeder and metering and gas removal (101.1) through point (101.2) and then directed to the afterburner (103).

[0155] In the afterburner (103), with the addition of external air (50) to mixed gases and vapors (20.6) the mixture (31) is formed, forming a complete oxygen-rich afterburner, generating hot gases (32) that are free of carbon not fully oxidized to CO2, and may have uses including: a) direct application where heat is required; b) steam generation for: a. processes that require heat from steam; b. processes that require steam for drives; c. turbine drive(s) and electricity generation.

[0156] If the gas extraction method (103.1) is a Venturi system (103.1 1), there will be a prior supply of combustion air (50) by this system, which will reduce the amount of air (50) supplied within the post-combustion chamber.

[0157] The integrated process of direct pyrolysis, stoichiometric combustion of waste and its byproducts, and combustion of generated gases is a continuous process, and therefore all stages occur simultaneously.

[0158] The integrated process of direct pyrolysis, stoichiometric combustion of waste and its byproducts, and post-combustion of generated gases is characterized by comprising the following steps: a) Step 1: dosing and feeding waste (10) into the direct pyrolysis medium (101) via the feed medium (101.1); b) Step 2: in the direct pyrolysis medium (101), carrying out the endothermic reactions of direct pyrolysis of the waste (10), generating at the end of this step the solid byproducts of pyrolysis in the form of charcoal (10.2) and the gaseous byproducts of thermal decomposition in the form of gases and vapors (20.5) with: a. use of the heat from the slightly cooled gases (20.4) originating from the stoichiometric combustion medium (102); b. maintaining the material in direct pyrolysis (10.1) for a certain time. sufficient for the thermal decomposition of these materials producing gaseous and solid byproducts, with the temperature of the materials in the solid state reaching between 200°C and 600°C; c. in the direction of flow of materials in the solid state, direct the non-pyrolyzed residues (10.2) free of chlorine and in the solid state to the stoichiometric combustion medium (102); d. in the direction of flow of materials in the gaseous state, in counterflow to the solid materials, direct the mixture (20.6) carrying all the chlorine content and in the gaseous state, to the post-combustion medium (103); c) step 3: in the stoichiometric combustion medium (102) carry out the exothermic stoichiometric combustion reactions of the non-pyrolyzed and chlorine-free materials, which are in the form of coals, coming from the pyrolysis furnace, generating at the end of this step the ashes (10.4) and the slightly cooled gases (20.4) with: a.a. blowing atmospheric air (50) in the quantity necessary and sufficient for controlled stoichiometric combustion; b. maintaining the material in stoichiometric combustion regime (10.3) for a sufficient passage time for its complete combustion and ash generation, generating oxygen-free combustion gases with a temperature between 800°C and 1200°C; c. passing the gases (20.3) through the cooling medium (102.1), lowering the temperature of the gases to values ​​between 600°C and 800°C, releasing the gases for the next stage slightly cooled (20.4); d. using refrigerant fluid (20.1) at the cooler inlet (102.1) and removing heated refrigerant fluid (20.2) for use in parallel processes or from the air (50); e. collect the ashes (10.4) from within the stoichiometric combustion medium (102) and transport them hermetically outside, storing them for future disposal as ashes (10.5); f. finally direct the slightly cooled gases (20.4) for the direct pyrolysis medium (101); d) step 4: in the direct pyrolysis medium (101), carry out direct pyrolysis on the material (10.1). with: a. heat transfer from the slightly cooled stoichiometric combustion gases (20.4) to the pyrolysis residue (10.1) by direct contact between them; b. thermally decompose the pyrolysis residue (10.1) and produce the gases and vapors (20.5); c. form the mixture of the gases and vapors from direct pyrolysis (20.5) with the slightly cooled stoichiometric combustion gases (20.4) generating the mixture of gases and vapors (20.6); d. at the end, exhaust through the gas extraction means (103.1) directing the combustible gases and vapors (20.6) to the post-combustion medium (103); e) step 5: in the post-combustion medium (103) promote the post-combustion of the combustible gases and vapors (20.6) by adding atmospheric air (50) with: a. by means of exhaust (103.1) to draw out gases and vapors (20.6) at point (101.2) of the pyrolysis medium (101); b. blow gases (20.6) into the post-combustion medium (103), being: i. with the addition of atmospheric air in the extraction medium (103.11) Venturi type, or, ii. without addition of atmospheric air in extraction medium (103.12) exhaust / fan type; c. blow air (50) sufficient for the complete combustion of the combustible gases and vapors (20.6); d. generation of hot gases (32); e. at the end of this stage direct the hot gases (32) for use; f) stage 6: control the entire process by means of a sensing, control and actuation means (104) by: a. receiving data from all sensors: i. from kit 101.6; ii. from kit 102.8; iii. from kit 102.9; and iv. from kit 103.2;. b. computational analysis of data from all sensors; c. action through actuators, where: i. the sensor kits (101.6) provide data from the direct pyrolyzer (101) to the control system (104) which acts through actuators: • in the feeding medium (101.1) controlling the volume of waste (10) fed; • means of moving (101.5) the waste in direct pyrolysis controlling the mixing and speed of passage of the waste (10.1), and; • power of the gas extraction system (103.1); ii. the sensor kits (102.8) and (102.9) provide data from the stoichiometric combustor (102) to the control system (104) which acts via actuators: • in the feeding medium (101.1) controlling the volume of waste (10) fed; • in the movements of the moving medium (102.5) applied to the combustion residues (10.3) controlling the mixture and speed of passage of these; • power of the gas extraction system (103.1); • Oxygen concentration to ensure that combustion reactions are stoichiometric; • power of the coolant movement system of the heat exchangers (102.1) to ensure sufficient stoichiometric heat exchange with the combustion gases to be slightly cooled; ill. the sensor kit (103.2) provides data from the afterburner (103) to the control system (104) which acts by actuators on the atmospheric air flow (50) to ensure that the combustion reactions are complete and controlled with an excess of oxygen of at least 3%.

[0093] The set of INTEGRATED EQUIPMENT (100) required for the execution of the process described above presents its functional technical composition. comprising 3 basic parts: a) a means for direct pyrolysis of waste (101); b) a means for stoichiometric combustion of pyrolyzed waste (102) having a cooling means (102.1); and c) a means for post-combustion (103) of the combustible gases and vapors generated in the previous ones, containing a gas extraction system (103.1) with: a. either a means with a Venturi system (103.11); b. either a means with a fan / blower (103.12); d) a means for sensing, control and actuation (104).

[0159] Direct pyrolysis means (101) of waste has its functional technical composition comprising: a) a waste loading means (101.1) that is leak-proof; b) a vacuum gas extraction point (101.2); c) a sealing means (101.31) with the waste loading means (101.1); d) a sealing means (101.32) with the stoichiometric combustion means (102); e) a passage opening (101.4) hermetically connected to the passage opening (102.4) which is: a. for the passage of gases (20.4) from the stoichiometric combustion means (102) to the direct pyrolysis means (101); b. for the passage of waste (10.2) from the direct pyrolysis means (101) to the stoichiometric combustion means (102); f) a means for moving the waste in direct pyrolysis; (g) at least one sensor kit (101.6) with each kit containing: a. a pressure transmitter (101.6.1); b. a temperature transmitter (101.6.2); c. an O2 analyzer and transmitter (101.6.3).

[0160] Stoichiometric combustion medium (102) has its functional technical composition comprising: a) a cooling medium (102.1) for temperature control of the exhaust gases from the stoichiometric combustion medium (102); b) an atmospheric air insufflation means (102.2); c) a vacuum gas extraction point (101.2); d) a sealing means (102.3) with the pyrolysis means; e) a passage opening (102.4) hermetically connected to the passage opening (101.4) which is: a. for the passage of gases (20.4) from the stoichiometric combustion means (102) to the direct pyrolysis means (101); b. for the passage of residues (10.2) from the direct pyrolysis means (101) to the stoichiometric combustion means (102); f) a means for moving (102.5) the residues in stoichiometric combustion; g) an ash extraction means (102.6); h) at least one sensor kit (102.8) in the stoichiometric combustion area with: a. a pressure transmitter (102.8.1); b. a temperature transmitter (102.8.2); c. an O2 analyzer and transmitter (102.8.3); i) a sensor kit (102.9) in the outlet area of ​​the stoichiometric combustor (102) with at least: a. a pressure transmitter (102.9.1); b. a temperature transmitter (102.9.2); c. an O2 analyzer and transmitter (102.9.3).

[0161] Post-combustion means (103) has its functional technical composition comprising: a) a means of blowing (103.1) of combustible gases (20.6), comprising: a. a Venturi system (103.11) which also blows a portion of air (50), or; b. an exhaust / blower (103.12); b) an atmospheric air blowing means (50); a. a sensor kit (103.2) in the after-combustion outlet area with at least: i. a pressure transmitter (103.2.1); ii. a temperature transmitter (103.2.2); iii. an O2 analyzer and transmitter (103.2.3).

Claims

CLAIMS 1. The integrated process of direct pyrolysis, stoichiometric combustion of waste and its byproducts, and post-combustion of generated gases is characterized by comprising the following steps: a) Step 1: Dosing and feeding waste (10) into the direct pyrolysis medium (101) via the feed medium (101.1); b) Step 2: In the direct pyrolysis medium (101), carrying out the endothermic reactions of direct pyrolysis of the waste (10), generating at the end of this step the solid byproducts of pyrolysis in the form of charcoal (10.2) and the gaseous byproducts of thermal decomposition in the form of gases and vapors (20.5) with: a. use of the heat from the slightly cooled gases (20.4) originating from the stoichiometric combustion medium (102); b. maintenance of the material in direct pyrolysis (10.1) for a sufficient time to thermally decompose these materials producing gaseous and solid byproducts, with the temperature of the materials in the solid state reaching between 200°C and 600°C; c.In the direction of the flow of materials in the solid state, direct the non-pyrolyzed residues (10.2) free of chlorine and in the solid state to the stoichiometric combustion medium (102); d. In the direction of the flow of materials in the gaseous state, in counterflow to the solid materials, direct the mixture (20.6) carrying all the chlorine content and in the gaseous state, to the post-combustion medium (103); c) Step 3: In the stoichiometric combustion medium (102), carry out the exothermic stoichiometric combustion reactions of the non-pyrolyzed and chlorine-free materials, which are in the form of coals, coming from the pyrolysis furnace, generating at the end of this step the ashes (10.4) and the slightly cooled gases (20.4) with: a. insufflation of atmospheric air (50) in the quantity necessary and sufficient for a controlled stoichiometric combustion; b. maintaining the material in a stoichiometric combustion regime (10.3) for a sufficient time to complete its combustion and generate. ashes, generating oxygen-free combustion gases with temperatures between 800°C and 1200°C; c. passage of the gases (20.3) through the cooling medium (102.1), lowering the temperature of the gases to values ​​between 600°C and 800°C, releasing the gases slightly cooled for the next stage (20.4); d. use of refrigerant fluid (20.1) at the cooler inlet (102.1) and removing heated refrigerant fluid (20.2) for use in parallel processes or from the air (50); e. collect the ashes (10.4) from inside the stoichiometric combustion medium (102) and transport them hermetically to the outside, storing them for future disposal as ashes (10.5); f. finally, direct the slightly cooled gases (20.4) to the direct pyrolysis medium (101); d) Step 4: In the direct pyrolysis medium (101), carry out direct pyrolysis on the material (10.1) with: a. heat transfer from the slightly cooled stoichiometric combustion gases (20.4) to the pyrolysis residue (10.1) by direct contact between them; b. thermally decompose the residue in pyrolysis (10.1) and produce the gases and vapors (20.5); c. form the mixture of gases and vapors from direct pyrolysis (20.5) with the slightly cooled stoichiometric combustion gases (20.4) generating the mixture of gases and vapors (20.6); d. at the end exhaust by means of gas extraction (103.1) directing the combustible gases and vapors (20.6) to the post-combustion medium (103); e) step 5: in the post-combustion medium (103) promote the post-combustion of the combustible gases and vapors (20.6) by adding atmospheric air (50) with: a. by means of exhaust (103.1) suction of the gases and vapors (20.6) at point (101.2) of the pyrolysis medium (101); b. blow gases (20.6) into the post-combustion medium (103), being: i. with the addition of atmospheric air into the Venturi type extraction medium (103.1 1 ). or, ii. without the addition of atmospheric air in the extraction medium (103.12) of the exhaust / fan type; c. blowing air (50) sufficient for the complete combustion of the combustible gases and vapors (20.6); d. generation of hot gases (32); e. at the end of this stage directing the hot gases (32) for use; f) stage 6: controlling the entire process by means of a sensing, control and actuation means (104) by: a. receiving data from all sensors: i. from kit 101.6; ii. from kit 102.8; iii. from kit 102.9; and iv. from kit 103.2; b. computational analysis of the data from all sensors; c. action through the actuators, where: i. the sensor kits (101.6) provide data from the direct pyrolyzer (101) to the control system (104) which acts by actuators: • in the feeding medium (101.1) controlling the volume of waste (10) fed; • means of moving (101.5) the waste in direct pyrolysis controlling the mixing and speed of passage of the waste (10.1), and; • power of the gas extraction system (103.1); ii. the sensor kits (102.8) and (102.9) provide data from the stoichiometric combustor (102) to the control system (104) which acts via actuators: • in the feeding medium (101.1) controlling the volume of waste (10) fed; • in the movements of the moving medium (102.5) applied to the residues in stoichiometric combustion (10.3) controlling the mixing and speed of passage of these; • power of the gas extraction system (103.1); • Oxygen concentration to ensure that combustion reactions are stoichiometric; • power of the coolant movement system of the heat exchangers (102.1) to ensure sufficient stoichiometric heat exchange with the combustion gases to be slightly cooled; ill. the sensor kit (103.2) provides data from the afterburner (103) to the control system (104) which acts by actuators on the atmospheric air flow (50) to ensure that the combustion reactions are complete and controlled with an excess of oxygen of at least 3%.

2. Integrated EQUIPMENT set (100), for carrying out the process defined in claim 1, characterized by having its functional technical composition comprising 04 basic parts: a) a means for direct pyrolysis of waste (101); b) a means for combustion of pyrolyzed waste (102) having a cooling means (102.1); and c) a means for post-combustion (103) of the combustible gases and vapors generated in the previous ones, containing a gas extraction system (103.1) with: a. or a means with a Venturi system (103.11); b. or a means with a fan / blower (103.12); d) a means for sensing, control and actuation (104).

3. Direct pyrolysis means (101) of waste, according to claim 2, characterized by comprising: a) a waste loading means (101.1) that is leak-tight; b) a vacuum gas extraction point (101.2); c) a sealing means (101.31) with the waste loading means (101.1); d) a sealing means (101.32) with the stoichiometric combustion means (102); e) a passage opening (101.4) hermetically connected to the passage opening (102.4) which is: a. for the passage of gases (20.4) from the stoichiometric combustion medium (102) to the direct pyrolysis medium (101); b. for the passage of residues (10.2) from the direct pyrolysis medium (101) to the stoichiometric combustion medium (102); f) a means of moving (101.5) the residues in direct pyrolysis; g) at least one sensor kit (101.6) with each kit containing: h) a pressure transmitter (101.6.1); i) a temperature transmitter (101.6.2); j) an O2 analyzer and transmitter (101.6.3).

4. Stoichiometric combustion medium (102), according to claim 2, characterized by comprising: a) a cooling medium (102.1) for temperature control of the exhaust gases from the stoichiometric combustion medium (102); b) an atmospheric air insufflation medium (102.2); c) a vacuum gas extraction point (101.2); d) a sealing medium (102.3) with the pyrolysis medium; e) a passage opening (102.4) hermetically connected to the passage opening (101.4) which is: a. for the passage of gases (20.4) from the stoichiometric combustion medium (102) to the direct pyrolysis medium (101); b. for the passage of residues (10.2) from the direct pyrolysis medium (101) to the stoichiometric combustion medium (102); f) a means of moving (102.5) the residues in stoichiometric combustion; g) a means of extracting ash (102.6); h) at least one sensor kit (102.8) in the stoichiometric combustion area with: a. a pressure transmitter (102.8.1); b.a temperature transmitter (102.8.2); c. an O2 analyzer and transmitter (102.8.3). i) a sensor kit (102.9) in the combustor outlet area (102) with at least: a. a pressure transmitter (102.9.1); b. a temperature transmitter (102.9.2); c. an O2 analyzer and transmitter (102.9.3).

5. Post-combustion means (103), according to claim 2, characterized by comprising: a) a means of blowing (103.1) of combustible gases (20.6), comprising: a. a Venturi system (103.11) which also blows a parcel of air (50), or; b. an exhaust / blower (103.12); b) an atmospheric air blowing means (50); c) a sensor kit (103.2) in the afterburner outlet area with at least: a. a pressure transmitter (103.2.1); b. a temperature transmitter (103.2.2); c. an O2 analyzer and transmitter (103.2.3).

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