BRPI1012377B1 - COAL AND FUEL GAS GENERATION PROCESS, SYSTEM AND METHOD - Google Patents

Abstract

Coal and Fuel Gas Generation Process, System and Method The present invention describes a system for the production of charcoal from lignocellulosic materials. The present invention relates a method for obtaining and reforming combustible gases for use in the generation of electric energy from the control of the charcoal production system. The method of the invention, unlike conventional methods, combines high temperatures, enclosed and pressurized environment, maintenance of these high temperatures for cracking and recovery of gases and average time between 22 and 28 hours. This method results in reduced yields but, on the other hand, results in a very compact material and is therefore better suited for use in steel blast furnaces. The present invention also describes a charcoal production process. According to the present invention, wood and other lignocellulosic materials are converted to charcoal by pyrolysis and the gases from the various process stages are mixed, reformed or cracked in a pressurized environment, saturated with carbon and water vapor, producing combustible gases. non condensable. The carbonization process proposed in the present invention consists of a continuous operation carried out in a system that aggregates a set of horizontal reactors, connected by valve-controlled gas flow barrels, whose operation combines temperature and pressure monitoring. In the process of the invention, the gas flow associated with temperature and pressure, promotes the maintenance of favorable conditions for the heat treatment of lignocellulosic matter, reaching as a final result, high quality carbonaceous material. The system of the invention is continuously fed without interruption of its operation and production. The arrangement of the present system also gives the possibility of subjecting the lognocellulosic material to a combination of pressure and high temperatures through the gas flow.

Description

(54) Title: COAL AND COMBUSTIBLE GAS GENERATION PROCESS, SYSTEM AND METHOD (51) Int.CI .: C10B 53/02; C10B 51/00; C10B 06/31; C10B 21/10; C10B 21/08; C10B 21/20; C10B 21/16; C10B 2/27; C10B 31/08; C10B 33/10; C10B 39/02; C10B 47/16; C10B 47/36; C10B 57/02; C10B 57/08 (73) Holder (s): MARCOS CABRAL FLECHA (72) Inventor (s): MARCOS CABRAL FLECHA; ALDO SARMENTO SOBRINHO; ALFREDO FROES DOLABELA (85) National Phase Start Date: 9/15/2010

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COAL AND FUEL GAS GENERATION PROCESS, SYSTEM AND METHOD

APPLICATION FIELD

The present invention describes a system for the production of charcoal for steel use, from lignocellulosic materials.

This invention reports a method for obtaining and remodeling in combustible gases non-condensable For use at generation in electricity, from of control of system in coal production vegetable.

The method of the invention, unlike conventional methods, combines high temperatures, a pressurized environment and maintenance of these high temperatures for cracking and gas recovery and an average time between 22 and 28 hours. This method results in a highly compacted material and is therefore more suitable for use in steel blast furnaces.

Finally, the method of the present invention dispenses with the treatment of the lignocellulosic material to be administered in the system of the present invention.

The present invention also describes a process for the production of combustible gases and charcoal, making it possible to use it both in small steel blast furnaces and in steel blast furnaces of plants integrated with coke.

According to the process of the present invention, wood and other lignocellulosic materials are converted into charcoal by pyrolysis and the gases from the various stages of the process are mixed, reformed or cracked in a pressurized environment, saturated with carbon and water vapor, being produced non-condensable combustible gases.

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The carbonization process proposed in the present invention consists of a semi-continuous operation, carried out in a system that aggregates a set of horizontal reactors, connected by barrels containing gases, controlled by valves, whose operation combines the monitoring of temperature and pressure. In the process of the invention, the gas flow associated with temperature and pressure, promotes the maintenance of favorable conditions for the thermal treatment of lignocellulosic material, reaching, as a final result, high quality carbonaceous material.

The system of the invention is fed by batch, every hour of operation, without the need to interrupt its operation and production. The arrangement of the present system also provides the possibility of submitting the lignocellulosic material to a combination of pressure and high temperatures through gas flows without loss of characteristics such as density and calorific value.

For a better understanding of the present invention, some concepts have been stipulated and should be used in its implementation. In this sense, charcoal is the material obtained from firewood by the process of carbonization or pyrolysis. Heat treatment is the operation or set of operations carried out in the solid state that includes heating, permanence at certain temperatures and cooling, performed with the purpose of giving the material certain characteristics.

In this invention, this treatment takes place by carbonization, in a process in which the wood is subjected to heating in a closed environment, with a small amount or total exclusion of air and during which gases, water vapors are released, leaving the charcoal as a residue. . For what

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3/30 the process promoted as a result the obtaining of a carbonaceous material of high calorific power, hardness and density necessary for the application both in small blast furnaces with charcoal and in blast furnaces with mineral coke, a system was built. This system constitutes a set of interconnected elements, in order to form an organized whole.

In the procedure for obtaining this carbonaceous material, pyrolysis represents an important phase. Strictly speaking, pyrolysis is the reaction of analysis or decomposition that occurs by the action of high temperatures. There is a disruption of the original molecular structure of a given compound by the action of heat in an environment with little or no oxygen. This transformation allows the release of energy.

As a starting material for processing and obtaining charcoal for steel use, this invention has agreed to use any lignocellulosic materials. Lignocellulosic materials have in their composition basically cellulose, hemicellulose and lignin, in the approximate proportion of 40 to 50%, 20 to 30% and 25 to 30% respectively, varying according to the type of material. These compounds form a complex and compact structure, whose characteristics will also depend on the type of material to be processed (bagasse or straw and different varieties of cane, among others). This concept includes biomasses such as wood, babassu coconut and other biomasses of plant origin. For the present invention, the term carbonaceous material is included in the concept of lignocellulosic material. The term wood is used here widely to include plant materials

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4/30 characterized by their cellulosic fiber structure. In this sense, the term extends to include materials such as tree bark, sawdust, chestnut bark and nuts, fruit stones, including, still, processed cellulosic materials.

This material, after being subjected to the processes and methods described in this invention, and after being processed by the system also object of this invention, allows the use of condensable gases and non-condensable gases and the transformation of non-condensable gases into condensable gases by cracking.

The method for producing H2 derived from hydrocarbons will be treated in this invention as steam reform or gas reform or even as catalytic oxidation.

STATE OF ART

The carbonization or charcoal of lignocellulosic materials consists of the elimination of volatile materials by thermal action. The product resulting from this process is a carbonaceous mass associated with an oxide complex.

In Brazil, this process is carried out in rudimentary furnaces and does not allow the recovery of volatile gases released during the reaction. This also implies obtaining a material low in calorific value and resistance, suitable only for small blast furnaces.

With the improvement of the coal production furnaces, some new processes with better control over the operation were introduced. Among these, the racks and vertical cylindrical ovens stand out.

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The patents listed below form an exemplary set of existing published and developed knowledge.

In PI8301847-6, a continuous carbonization process of 5 lignocellulosic materials in a vertical oven that reveals high quality charcoal with better efficiency is revealed. In this invention, the continuous carbonization of lignocellulosic materials takes place in a vertical oven with metered injection of combustion products of part of the non-condensed volatile materials, which allows, in addition to satisfactory operational control and control, to obtain a high recovery of the volatile materials, with constant yield and quality of the coal. , condensates and non-condensing combustible gases.

In PI0702047-3, in turn, a process for retaining condensable vapors and gases generated during the burning or pyrolysis of biomass is described. In this invention patent the process of retaining condensable vapors and gases generated during the burning or pyrolysis of biomass, occurs through a smoke condensation system. The process applies to smoke that is generated in processes of burning or pyrolysis of biomass, which is pumped through ducts to a condenser (heat exchanger). This exchanger forces the smoke to pass and on the outside there is a flow of water with a high flow to increase the heat exchange efficiency, since the smoke enters the condenser with a high temperature (t> 200 ° c).

US 5,449,438 describes an equipment and method for pyrolysis of compacted organic matter waste. The starting organic material for the pyrolytic process includes tire rubber, processed by decomposition in a

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6/30 bath with temperatures between 450 C and 550 C, in a mixture of volatile and solid constituents, collecting part of these gases for later use.

US 4,472,245 describes a continuous heat treatment process of carbonizable material. These materials become charred at high temperatures. These materials include wood, cellulose, household waste, used tires, plastics, oil, among others. These materials are subjected to heat treatment in an electric furnace that contains electrodes on the ceiling surface. The material is inserted into the furnace to the limit and continuously moved slowly so that the heat is transferred to other parts of the furnace. This procedure makes the charred material highly conductive temporarily while maintaining contact with the electrodes installed on the furnace roof. In these electrodes, electric current passes through the material.

US 6,623,602 describes a method for obtaining volatile and non-volatile products. The method of obtaining comprises pyrolysis polymeric material in a reactor with an oxygen-deficient atmosphere. The polymeric material is simultaneously compressed and heated to a temperature sufficient for pyrolysis of the polymeric material and, thus, producing non-volatile residues and volatile products.

US patent 4,274,941 reports a process for generating combustible gases, liquid coal and superheated steam. The coal grains are placed in a horizontal chamber with solid material for heat exchange. The coal is then subjected to an environment with low levels of nitrogen and oxygen to obtain liquid by-products. In

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7/30 second chamber the material is subjected to fluidization with air and firing. The generated steam is filtered.

In PI0705610-9, it is an equipment that presents itself as a solution for use in reducing the emission of particulates, gases and vapors in the production of charcoal, minimizing the environmental impact such as the greenhouse effect and acid rain. This system produces coal with a high fixed carbon content and high yield in the production of pyroligneous liquor.

PI0503842-1 describes a process that consists, firstly, of harvesting and dragging the wood, which is, after being cut into sheets, stored for natural drying, and after drying it is transported by means of a monorail reason for patent application - up to the oven, where it is then manually placed inside cylindrical steel retorts - mounted on rails, in which the aforementioned retorts roll into the aforementioned oven, when the process itself begins , in order to obtain the coal and the fumes resulting from its carbonization, which happens due to the heat generated in the furnace existing in the refractory masonry furnace - reason for another patent application -, these fumes processed chemically. After the carbonization of the wood, now transformed into coal, the retorts, together with the coal contained inside, are immersed in a tank with refractory paint that adheres to the body of the retorts, forming a protection and promoting its cooling and the coal to the Same time. All coal from the mentioned carbonization is stored in a silo. The operational cycle of this process ends, when the temperature reaches a certain degree of

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8/30 heating, obeying the characteristics of the processed wood such as thickness and its species. The doors of the aforementioned oven open simultaneously, allowing the wood to be charred and the coal resulting from this carbonization to enter, always with the aid of the mentioned retorts. The smoke distillation carried out within this charcoal process is preceded by the condensation of vegetable tar, which occurs in a filling tower, cooperating with the use of catalysts and electrostatic filters in common use. The non-condensed gases in this process are burned in the furnace of the aforementioned furnace, while the resulting pyroligneous acid is sent to the first separation that takes place in towers made of wooden dishes, from which separation is obtained the methanol and the resulting miscella is conducted to be diluted in a suitable solvent and sent to a dish tower for solvent recovery. The acetic acid obtained goes on to be refined and purified in a dish tower. Methanol and acetic acid are subsequently stored for sale.

Patent PI9509631-0 introduces a process for the production of coke from coals. In the invention, coke is continuously produced by heating a moving charge of coal within the annular cross section defined by two concentric tubes. The coking chamber, which includes a large diameter tube and a smaller concentric diameter tube, is forcibly fed with coal, such as metallurgical coal. The coal is bidirectionally heated along a temperature-controlled gradient between the inner wall of the small diameter tube and the outer wall of the large tube

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9/30 diameter. The coal is transformed into coke as it runs longitudinally along the axis of both tubes. Coke is discharged from the chamber at the opposite end to which it was loaded and is cooled before being exposed to the atmosphere. The gases generated during the decoking process are collected and treated. All of these operations are carried out in a closed system to prevent pollution.

PI0210706-6 discloses a process with low energy introduction for the pyrolytic conversion of biomass to charcoal or carbonized charcoal.

The biomass is sealed in a container, pressurized and heated until it ignites by means of bar heaters. Pressure control by introducing air and releasing gases to maintain successively lower pressure levels results in a typical conversion time of less than 30 minutes.

The invention contained in document PI0207428-1 presents a method and apparatus for decreasing gas flow rates in a single flue gas system for a coke oven during at least one initial coking operation after a coke oven has been loaded. with coal. The method includes employing a duct system between a first coke oven that has a first coking chamber and a second coke oven that has a second coking chamber to direct at least a portion of gas from a gas space in the first coking chamber for the second coke oven, thereby reducing a gas flow in the first flue gas system of the first coke oven. The reduction in flow rates of a single flue gas has a beneficial effect

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10/30 in product yield, coke oven life and environmental control of volatile material emissions from coke ovens.

SUMMARY OF THE INVENTION

The central component of the present invention is the valorization of the gaseous waste produced during carbonization, by recovering the energy (2.6x10 ⁶ kgcal / ton of dry wood) not used in the process.

Another characteristic of the present invention and of high relevance comprises the method of obtaining carbonaceous material of high calorific value. This result is due to the temperatures used in the process and the use of pressure in carbonization, which opens the possibility of using this charcoal in blast furnaces replacing mineral coke, due to the high mechanical resistance to compression achieved by the final product, in the order of approximately, 60 kg / cm2.

The use of this method is due to the system, object of this invention. Said system comprises a set of horizontal cylindrical reactors, coated with metal material also refractory, coated connected to with refractory material, whose functions of and drying, directing gases for heating, cooling and reforming and cracking of gases is controlled by valves installed in the barrels. .

Thus, it is the object of the present invention to present an economical process for converting wood or lignocellulosic materials, preferably granulated, into charcoal coke at final carbonization temperatures between 950 ° C and 1,200 ° C, for an estimated period between 22- 28 hours, varying according to the conditions of entry (humidity and

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11/30 temperature) of the wood used for charcoal production.

In the process of the present invention, kegs have different functions depending on the phases to which the material to be converted is subjected. For the heating and drying phases of the material being hung, the kegs direct the gases as a thermal fluid for heat transmission. In order to maintain the system temperature and generate non-condensable gases, in the reform and cracking phase, the kegs direct the gases to the reactors in the final phase of coal production. In another phase, the barrels promote the direction of the gases as a thermal fluid for the cooling of the hanged material.

It is also the object of the present invention a method for obtaining charcoal for steel use, from a closed and interconnected environment, with controlled pressure. This method consists of subjecting the lignocellulosic material to increasing temperatures, with variations between 50 ° C and 1200 ° C, under controlled pressure.

The method of the present invention allows, from a closed system with connections for gas exchange and reform, under the controlled use of pressure, with intervals at -2 bar and maximum pressure (Pmax) of 10 bar, to obtain carbonaceous material with efficiency gravimetric of 26% on a dry basis, with fixed carbon content of around 90% and gravimetric yield on fixed carbon of around 22.5%.

DETAILED DESCRIPTION OF THE INVENTION

The present invention provides a process for the pyrolytic, under pressure, of wood or lignocellulosic granulated on charcoal. Such material material conversion

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12/30 may be used without pre-treatments other than its transformation into chips with a particle size between 20mm and 150mm.

For the present invention, the maximum pressure environment 5 (Pmax) is equivalent to 10 bar. The process of the present invention also contemplates negative pressure phases.

The process described in the present invention requires controlling the humidity of the materials, in order to keep it constant, since the humidity of the materials will determine the total processing time.

The total processing time is estimated between 22 to 28 hours, varying depending on the moisture content of the materials, the heating rates and the cooling rates. The cooling will be done inside the reactor, with energy recovery in the form of heat.

In the process of the present invention, the number of reactors is proportional to the number of hours of the total processing time, that is, from 22 to 28 reactors.

In a more detailed perspective the process of the present invention can be described as follows:

The material, wood in chips, is introduced into the reactors through the use of horizontal, cylindrical metal buckets. The metal buckets are supported on the floor of the reactor, being separated from it by metal chocks to allow the circulation of gases and the exchange of heat.

The drying and heating phase of the material, endothermic phase, will be done by circulating the hot gases produced in the carbonization phase in the reactor. The flow of hot gases through the reactor will be controlled by valves installed in the barrels and will be a function of humidity

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13/30 of the material and the desired rates of heating, which may vary according to the quality of the material hung.

The carbonization phase, exothermic, in turn, can also be controlled, by varying the rate of heating of the hanged material, by controlling the flow of oxygen injection in the reactor. Oxygen for the control of heating rates in this phase may be supplied by atmospheric air or by any production process or concentration of oxygen that may be used.

The production of combustible gases occurs through the treatment of all gases generated in the process of converting lignocellulosic material. In this phase, the kegs direct the gases for mixing and reforming or cracking inside the pyrolysis reactors themselves. The coal already formed, submitted to temperatures between 1,200 ° C and 900 ° C, in an environment with pressure P2 (see fig. 7), which will allow the occurrence of endothermic reactions, according to the following scheme:

H2O + C + HEAT CO2 + C + HEAT

TAR + STEAM + HEAT <=> CO + CO2 + CH4 <=> H2 + 2CO <=> 2CO

Another characteristic of the process of the present invention, comprises the change in shape of the carbonaceous material, with reduced porosity and adsorption power, which translates into improved appearance and use of the resulting product. This phase of reform or cracking of the gases produced in carbonization results in the generation of a gas composed of a mixture of water vapor (H2O), carbon dioxide (CO2), carbon monoxide (CO), hydrogen (H2), methane ( CH4) and

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14/30 nitrogen (N2), with PCI lower calorific value of approximately 4,000Kcal / Nm3.

The present invention also provides for a system composed of a set of horizontal cylindrical metal reactors, coated internally with refractory material, connected to metal barrels coated externally with refractory material. This set of interconnectors in the system allows the circulation of gases resulting from the pyrolysis process.

In the present invention, each barrel is coated externally, in order to promote the thermal insulation of the system.

According to the process of the present invention, up to a temperature of 850 ° C only one outlet keg (BSC) is used.

The general arrangement of the system describes 09 kegs that will be activated during the process according to the following description: BE represents the keg of gases entering the reactor; BSC - represents the reactor gas outlet barrel for circulation in the reactor set; BSA represents the fuel gas output barrel from the reactor to supply the thermoelectric plant, produced in PHASES 6 and 7; B1 - represents the oxygen barrel that injects oxygen into the reactor; B2 - represents the barrel of gas circulation for cooling after the reactor has been muffled; B3 - UTE feeding keg that receives the gases produced in PHASE 6 and PHASE 7, already reformed and cracked, non-condensable; B4 - Exhaust keg for the atmosphere; B5 - Barrel for hot gas injection, containing volatile gases not yet reformed or cracked, which receives the gases produced in the reactors of the

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PHASE 5, to be injected into the reactors where the wood chip material is being dried in PHASE 3; B6 Barrel of circulation of gases for reform, receives the gases produced in the reactors of PHASES 4 and 5 to be reformed and cracked in the reactors in PHASE 8; B7 Barrel for removing non-condensable gases - remaining in the reactor, in PHASE 11, by means of a vacuum, to be injected into the combustible gas cleaning system; B8 Barrel for removing atmospheric air present in the reactor, in PHASE 2; B9 - Barrel for injection of atmospheric air in the reactor - after the end of the process and before opening the door to remove the produced coal, PHASE

12, for the removal of toxic and flammable gases from the reactor.

These interconnected elements that comprise the object of this invention also have a connection with other equipment or machines that assist their operation, as shown in Figure 1.

Table 1 describes the operation of the kegs, according to the phases of the process and functionalization of the various components of the system, object of the present invention. The X marks which barrels are operated during each phase that comprises the process.

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TABLE 1

Phase Operation 1 2 3 B jmle ç you Ç 7 3 3 1 Cescarqa / Carqa BE X BSC X BSA X R z E B'Haaarnentü Air vacuum BE BSC X BSA 3 Hot gas filling BE X BSC BSA u End-stage drying to 230 ⁼ C BE X BSC X BSA Ç L Exothermic tass carbonization from 230 to FFO ⁼ C BE X BSC X BSA Ç Carbonisation exothermic phase from EEO to 3E0 ⁼ C BE X BSC X BSA 7 Carbonization exothermic phase from 3E0 to 1,100 ⁼ C i environment ΙΓΕ BE X BSC BSA X 3 Cracking receives bad gases, injects U ^- E BE X BSC BSA X 3 Smothering BE BSC BSA 10 Then heat circulation in the heat exchanger BE X BSC X BSA 11 Withdrawal of the gas vacuum BE BSC X BSA 12 Ventilation for CO withdrawal BE X BSC X BSA

Table 2 describes the operation of the system and operation of the valves at each stage of the process of the invention.

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TABLE 2

As it appears, each barrel is associated with 5 control and monitoring valves of the system as a whole. The letter A indicates which valves are open and in which phases. Altogether, there are 17 valves per reactor, whose operation can be detailed as follows: Valve

VI controls the flow of gases entering the BE barrel; 10 during the oxygen injection phase, isolates the other barrels, allowing injection only by the BE barrel.

Valve V2 controls the outflow of gases in the BSC barrel. Valve V3 controls the injection of oxygen from barrel Bl into barrels BE. V4 valve controls the entry of gases from barrel B2, coming from the recovery boiler,

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18/30 for the cooling of the produced coal. PHASE 10. Valve V5, controls the entry of gases from barrel B5, coming from the reactors of PHASE 6, in the BE barrel, for drying the material, PHASE 3. Valve V6, controls the entry of gases from barrel B6, coming from reactors of PHASE 4 and PHASE 5, in the BE barrel, for the reform and cracking of the same. Valve V7, controls the injection of gases from the BSC outlet barrel, from the PHASE 7 reactors, into the B5 barrel, to be injected in the drying of the material,

PHASE 4. V8 valve, controls the injection of gases from the BSC outlet barrel, from the PHASES 4 and PHASE 5 reactors, into the B6 barrel, for injection into the PHASE 8 reactors. Valve V9 controls the outflow of gases from the BSC barrel. , of the reactors of PHASE 10, in barrel B2, bound for the recovery boiler. Valve V10, controls the injection of gases from the BSA outlet keg, from the PHASE 7 and PHASE 8 reactors, in the B3 keg, destined for the power generation process, feeding the UTE. Valve V11 controls the removal of fuel gas remaining in the reactor in PHASE 11, for the B7 barrel, by means of a vacuum. Valve V12, controls the removal of atmospheric air remaining in the reactor after closing the door, PHASE 2, to the B8 barrel, by means of a vacuum. V13 valve, controls the access of the BE inlet pipeline to the barrel

Relief to atmosphere B4, from the phase 1 reactor. Valve V14, controls the access of the BSC outlet barrel to the relief tube B4 from the phase 1 reactor. Valve V15 controls the injection of atmospheric air from the barrel B9, in the PHASE 12 reactor. Valve V16 controls the outflow of gases in the BSA barrel. Valve V17, controls the access of the BSA outlet pipe to the

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19/30 atmospheric relief barrel B4 from the PHASE reactor

1.

The system of the present invention also comprises an equipment for measuring pressure and internal temperature of the reactors, gas mixers and two reserve kegs.

Finally, the present invention describes a method of controlling and obtaining material with a high calorific content, density and pressure resistance. These characteristics are due to a correlation of medium intensity between the density of the wood and the friability of the charcoal as well as between the density of the charcoal and its resistance to mechanical compression, once considered the correlation of medium intensity of the wood and the friability of the coal, as well as between the density of the coal and its resistance to mechanical compression.

Wood has greater or lesser density, fundamentally due to four factors: cell size, cell wall thickness, interaction between these two factors and the presence of extracts. In this invention the constructed method allows control of the influence of the heating rate and influence of the carbonization pressure.

In the case of the heating rate, the higher, the greater the yield in condensed liquids. For pressure, the longer the contact time between the volatiles and the solid product, the higher the charcoal yield. The slower the carbonization is carried out, the higher the coal yield will be. The increase in resistance from 500 ° C may be due to: a) Influence of the radial decrease, increasing the number of fibers per unit area; b) Influence of

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20/30 structural rearrangement of carbon, producing a structure of greater resistance.

In this way, the method of the present invention allows that, with a correct operation of the furnaces, it is possible to go from the gravimetric yield from 22-23% to 35%.

The method and process of this invention result in the formation of carbonaceous material with calorific value in the order of 7,800 Kcal / kg, mechanical resistance to compression in the range of 60 kg / cm ² and can replace the use of coal coke in steel furnaces.

Fuel gas also results in the present invention. The combustible gases produced by the reactor set will be directed to feed the combined cycle thermoelectric plant - UTE. In order to obtain a fuel gas resulting from the process with greater calorific value per cubic meter, the present invention describes a phase of injection of a mixture with a minimum of 70% of 02 and a maximum of 30% of N2. This phase contributes to the reduction of nitrogen and increased calorific value.

DESCRIPTION OF THE FIGURES

Figure 1 represents the general arrangement of the reactors, comprising the system, object of the invention.

Figure 2 represents the general arrangement of the system, where, B1 - represents the oxygen barrel; B2 - represents the gas circulation barrel; B3 - UTE feeding keg; B4 - Exhaust keg for the atmosphere; B5 - Hot gas injection barrel; B6 Barrel of circulation of gases for renovation; B7 Barrel for removing non-condensable gases; B8 30 Atmospheric air removal keg; B9 - Barrel of

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21/30 atmospheric air injection. Figure 2 also describes some components of the system, as follows:

- Air supply fan

- Oxygen reservoir

3 - Compressor

- Oxygen PSA system

- Air purge for atmosphere

- Compressor

- Vacuum air tank

8 - Chimney exhaust set furnaces

- Compressor

- Recovery Boiler 2

- Cold combustible gas vacuum tank

- Compressor

13 - Recovery boiler 1

- Compressor

- Cold combustible gas tank

- Gas turbine

- Gas cleaning system

18 - Recovery Boiler 3

- Heat exchanger in the steam circuit

- Steam turbine

Figure 3 represents in detail the BSA output keg for feeding the UTE.

Figure 4 represents in detail the outlet BSC barrel for circulating gases.

Figures 5 represents in detail the BE keg inlet to the reactors.

Figure 6 represents the pressure graph in the operation of the 30 reactors.

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Figure 7 represents the graph of temperature variation during the process.

Figure 8 represents the graph of activation of the kilns during the process of converting lignocellulosic material into carbonaceous material, considering a cycle of 22 hours.

Figure 9 shows a detail of the entry barrels in the BE reactors.

Figure 10 shows a detail of the outlet barrels for feeding the UTE BSA.

Figure 11 shows a detail of the outlet barrels for the circulation of BSC gases.

Figure 12 represents a cross section of one of the BE, BSA and BSC reactors and barrels.

Table 3 presents a legend that must be applied for the analysis of each graph present in the figures listed above.

EXAMPLES

The present invention can be better understood by the examples presented below.

EXAMPLE 1 - DESCRIPTION OF THE STARTING PROCESS

As an example for describing the phases of the conversion process from wood to coal, the total processing time of 22 hours and consequently a total of 22 reactors will be considered.

PHASE 1

REACTOR 1, TIME 22 x N + 0 to 22 x N + 1 - LOADING AND UNLOADING THE REACTOR

End of the carbonization process. The carbonized material has a temperature below 50 ° C and the environment inside the reactor is ventilated with air at atmospheric pressure. Opening of the reactor door. Buckets withdrawal

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23/30 metal loaded with coal by the feeder cart. With the aid of the feeder, cleaning the bottom of the reactor with a vacuum cleaner to remove ash and / or particulate material deposited on the bottom. Loading of the reactor with metal buckets loaded with wood chips by the feeder cart. Reactor door closing.

LEVEL 2

REACTOR 1, TIME 22 x N + 1 to 22 x N + 1.25 - AIR EXTRACTION.

Reactor outlet connected to the B8 barrel - emptying the air inside the reactor by vacuum until a pressure of -2 bar. Reactor output disconnected from B8 barrel.

PHASE 3

REACTOR 1, TIME 22 x N + 1.25 to 22 x N + 1.5 - EQUALIZATION

PRESSURE

Reactor inlet connected to barrel B5 - filling the reactor with gas until pressure P3 (see fig. 7). The reactor outlet remains closed.

PHASE 4

REACTOR 1, TIME 22 x N + 1.5 to 22 x N + 4.5 - DRYING OF THE MATERIAL, ENDOTHERMAL PHASE.

Reactor inlet remains connected to barrel B5. Reactor output is connected to the B6 barrel. The internal pressure of the reactor is maintained at P3. Ventilation in the reactor with controlled flow to increase the temperature at a rate of 80 ° C / h to a final temperature of 280 ° C. End of the endothermic phase. Flow rate varies during the drying phase with the opening of the control valves. The gases entering the reactor and those generated in this phase are sent to reform and cracking.

PHASE 5

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REACTOR 1, TIME 22 x N + 4.5 to 22 x N + 7.5 - CARBONIZATION OF THE MATERIAL, EXOTHERMAL PHASE.

Reactor inlet disconnected from B5 barrel. Reactor inlet connected to barrel B1, - oxygen injection, pressure increase from P3 to Pmax (see fig.7). Reactor output remains connected to the B6 barrel. Temperature rise from 300 to 550 ° C. Oxygen flow control to maintain increasing heating rate. The gases entering the reactor and those generated in this phase are sent to reform and cracking.

PHASE 6

REACTOR 1, TIME 22 x N + 7.5 to 22 x N + 9.5 - MATERIAL CARBONIZATION, EXOTHERMAL PHASE.

Reactor inlet remains connected to barrel B1, 15 oxygen injection. Reactor output disconnected from the barrel

B6. Reactor output connected to B5 barrel. Pressure maintained at Pmax (see fig. 7). Temperature rise from 550 to 850 ° C. Oxygen flow control to maintain increasing heating rate. The gases entering the reactor and those generated in this phase are directed to the previous drying phases.

PHASE 7

REACTOR 1, TIME 22 x N + 9.5 to 22 x N + 11.5 CARBONIZATION OF THE MATERIAL, EXOTHERMAL PHASE.

Reactor inlet remains connected to barrel B1, oxygen injection. Reactor output disconnected from B6 barrel. Reactor output connected to barrel B3. Pressure is maintained at Pmax (see fig. 7). Temperature increase from 850 to 1,200 ° C. Oxygen flow control to maintain increasing heating rate. Material reaches final process temperature. The gases entering the reactor and the

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25/30 generated in this phase are directed to the feed barrel of the power generation process.

PHASE 8

REACTOR 1, TIME 22 x N + 11.5 to 22 x N + 15.5 - PHASE OF REFORM AND GAS CRACKING.

The reactor environment has carbonized material and

temperature of 1. , 100 ° C, at pressure of P2 (see fig. 7). In this environment will be injected the gases generated in phases previous reactors background to Reactor 1, enabling the occurrence of endothermic reactions: TAR + STEAM + HEAT < => CO + CO2 + CH4 H2O + C + HEAT <=> H2 + 2CO CO2 + C + HEAT <=> 2CO

Reactor inlet disconnected from barrel B1. Reactor output remains connected to barrel B3. Pressure reduction from Pmax to P2 (see fig. 7). Reactor inlet connected to barrel B6. Temperature reduction from 1,200 to 900 ° C. The inlet gases in the reactor reformed at this stage are directed to the feed barrel of the power generation process.

PHASE 9

REACTOR 1, HOUR 22 x N + 15.5 to 22 x N + 15.5 - DAMPING OF THE REACTOR. INSTANT PHASE.

Reactor input disconnected from B6 barrel. Reactor output disconnected from barrel B3. Material temperature remains at 900 ° C. The reactor pressure is P2 (see fig. 7).

PHASE 10

REACTOR 1, TIME 22 x N + 15.5 to 22 x N + 21.5 COOL COOLING.

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Reactor output connected to the B2 keg. Reactor inlet connected to barrel B2. The pressure is reduced from P2 to Pl (see fig. 7). Temperature reduction from 900 to 50 ° C.

PHASE 11

REACTOR 1, TIME 22 x N + 21.5 to 22 x N + 21.75 - WITHDRAWAL FROM COLD FUEL GAS.

Reactor environment is filled with combustible gases at 50 ° C, with pressure Pl (see fig. 7). Reactor outlet connected to the B7 barrel, removing the cold combustible gas up to a pressure of -2 bar. Reactor output disconnected from barrel B7.

PHASE 12

REACTOR 1, TIME 22 x N + 21.75 to 22 x N + 22 - FILLING WITH AIR AND VENTILATION FOR WITHDRAWAL OF GASES TOXIC AND FLAMMABLE CO Ε H2. Reactor environment filled with combustible gases The 50 ° C, with a pressure of -2 bar. Output reactor connected at the

barrel 7, removal of the cold fuel gas up to a pressure of -2 bar. Reactor inlet connected to barrel B9.

Pressure in the reactor ranges from -2 bar to atmospheric pressure. Reactor output connected to B4 barrel. Ventilated reactor environment to remove CO and H2. Reactor temperature equal to room temperature. End of the process.

Tables 3 and 3.1 detail the process in progress and the operationalization of each component and control of the variables, system and processes of this invention and should be considered for analysis of the graphs presented in figures 6, 7 and 8.

TABLE 3

BE BSC BSA 1 Unloading and Loading B4 B4 B9

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2 Vacuum air evacuation B8 3 Filling with hot gas B5 4 Endothermic phase drying up to 280 B5 B6 Γ Carbonization exothermic phase from 280 to 550 Bl B6 6 Exothermic phase carbonization from 550 to 850 Bl B5 7 Endothermic phase carbonization of 850 1200 injects UTE Bl B3 8 Cracking receives cold gases injects UTE B6 B3 1 ⁹ Instantaneous muffling 10 Cooling recirculation in exchanger of heat B2 B2 11 Withdrawal of cold gas vacuum gas B7 1 12 Ventilation for CO withdrawal B9

TABLE 3.1

Hurry O Has P 1 Unloading and Loading B 1 Barrel of oxygen Pmax AMB 2 Vacuum emptying air B 2 Barrel of cooling in exchanger heat Pl 900 The 30 3 Filling with gas hot B 3 Barrel of UTE power P2 850 The 120 0 4 Drying phase B ATM barrel ATM AMB

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endothermic up to 280 4 ensures tightness Carbonization phase exothermic from 280 to 550 B 5 Barrel of circulation of hot gas Pmax 550 The 850 6 Carbonization phase exotherm from 550 to 850 B 6 Barrel of circulation for cracking P3 280 The 550 Carbonization phase 850 endothermic 1200 injects UTE B 7 Barrel of gas withdrawal cold vacuum gas -2 30 8 Cracking gets cold gases injects UTE B 8 Barrel of air removal - air vacuum -2 AMB Smothering phase instantaneous B 9 Barrel of ventilation with air 1 AMB

Pmax = lObar

Pmax> P3> P2> Pl

EXAMPLES 2 AND 3

The tests presented below were carried out with reference to the following Brazilian standards: NBR 8112 Charcoal - Immediate Analysis, aimed at determining the contents of moisture, ash, volatile matter and fixed carbon of charcoal; NBR 8633 - Calorific Power Determination, prescribes the method of determining the higher calorific power of charcoal at constant volume, in an adiabatic, isothermal or static calorimetric pump; and NBR 6922 - Determination of Specific Mass

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29/30 (Bulk Density), prescribes the method for determining the specific mass of charcoal as received.

EXAMPLE 2

Loads of eucalyptus wood chips converted into 5 coal and combustible gases are described in Table 4 below and compared with commercial coal. The wood chips have granulometry in the range of 20 to 150 mm.

TABLE 4

description unity Amount Hanged wood (damp) Kg 1,535 Hanged wood (dry) Kg 1,075 Moisture O, % 30 Coal produced Kg 280 Gravimetric yield on coal (dry base) O, % 26 Gases produced - temperature of 900 ° C gas outlet. Kg 1,305 Injected oxygen (gas with 80% 02 20% N2) Kg 50 Processing time H 22

The loss of gases in the connections of the kegs and the doors of the reactors is estimated at 0.5% of the total produced and presented in Table 5. Composition of the gas produced at the outlet temperature of 900 ° C, pressure of P2 and with total calorific value of 4.27 x 10 ⁶ Kgcal.

TABLE 5

description Percentage unity Amount Total gases 100 Kg 1,305 H20 25 Kg 326 C02 33.1 Kg 432 N2 0.8 Kg 10

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H2 3.5 Kg 45.7 CO 22 Kg 287 CH4 15.1 Kg 197 Particulate material 0.5 Kg 7

Example 3

Table 6 describes results of comparison of the characteristics of the charcoal produced in the process with commercial charcoal.

TABLE 6

description unity Coal from process coal commercial Gravimetric yield (dry base) O, % 26 30 Fixed carbon O, % 95 72 Gravimetric yield fixed carbon O, % 23 21 Volatile materials O, % 3.5 25 Ashes O, % 1.5 3 Moisture O, % 3 8 Density Kg / m ³ 320 250 Calorific value Kgcal / kg 7,800 6,500 Compressive strength Kg / cm ² 60 30 Friability Low High Reactivity Low High Fines content O, % AT 10 Granulometry mm 60 to 80 10 to 120

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Claims (10)

1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 124 567 89 10 11 FIGURE 6 Petition 870180018338, of 03/07/2018, p. 50/56 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 21 22 0. OC. Lll V) V)> <CO <OC. 1/10 R1 R3 R5 R7 R9 R11 R13 R15 R17 R19 R21 444 444 H444 444 444 4444 444 4444 444 1 - PROCESS FOR THE GENERATION OF COAL AND COMBUSTIBLE GASES, for the pyrolytic conversion of wood or lignocellulosic materials into coal, continuously, using the system as defined in any one of claims 4 to 7, characterized by presenting Phase 1 - operation of reactor discharge / charge - the reactor is at atmospheric pressure and at room temperature, the gas inlet barrel in the BE reactor is connected to the B9 barrel, the BSA outlet and supply barrel and the BSC outlet and circulation barrel are connected to the barrel B4; Phase 2 - reactor emptying, air vacuum - BE and BSA kegs are closed, BSC keg is connected to B8 keg; Phase 3 - filling the reactor with hot gas - the BSA and BSC kegs are closed, BE keg is connected to the B5 keg; Phase 4 - drying of the hanged material to 280 ° C - the BSA keg is closed, the BE keg is connected to the B5 keg and the BSC keg is connected to the B6 keg; Phase 5 carbonization of the hanged material from 280 ° to 550 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B6 barrel; Phase 6 - carbonization of the material hung from 550 ° to 850 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B5 barrel; Phase 7 - carbonization of the material hung from 850 ° to 1,100 ° C - the gases produced in this phase are directed to the power generation unit, the BSC barrel is closed, the BE barrel is connected to the B1 barrel and the BSA barrel is turned on barrel B3; Phase 8 - cracking of gases from other phases - the gases produced in the other phases are injected into the reactor to crack these, the cracked gases are from 05/25/2018, p. 5/15 2/10 R2 R4 R6 R8 R10 R12 R14 R16 R18 R20 R22 R1 R3 R5 R7 R9 R11 R13 R15 R17 R19 R21 FIGURE 2 Petition 870180018338, of 03/07/2018, p. 48/56 2 - COAL AND COMBUSTIBLE GAS GENERATION PROCESS, for the pyrolytic conversion of wood or lignocellulosic materials into coal, using the system as defined in any one of claims 4 to 7, 10 characterized by obtaining charcoal coke produced at final carbonization temperatures between 900 ° C and 1,200 ° C, in an environment with a maximum pressure of 8 bar, with the total processing time between 22 and 28 hours, with the number of reactors equal to the total time 15 hours of processing, with the use of gases produced in the battery for drying and heating up to 280 ° C of the hanged materials, with the use of non-condensable gases produced for the cooling of carbonized materials, with the use of oxygen in the 20 coal mass for raising the temperature from 550 ° C to the final processing temperature of 1,100 ° C; presenting 12 phases, being Phase 1 - reactor discharge / loading operation - the reactor is at atmospheric pressure and at room temperature, the 25 gas inlet in the BE reactor is connected to the B9 barrel, the BSA outlet and supply barrel and the BSC outlet and circulation barrel are connected to the B4 barrel; Phase 2 - reactor emptying, air vacuum - BE and BSA kegs are closed, BSC keg is turned on 30 to barrel B8; Phase 3 - filling the reactor with hot gas - the BSA and BSC kegs are closed, BE keg is connected to the B5 keg; Phase 4 - drying of the hanged material to 280 ° C - the BSA keg is closed, the Petition 870180044344, of 05/25/2018, p. 7/15 2/11 directed to the power generation unit, the BSC barrel is closed, the BE barrel is connected to the B6 barrel and the BSA barrel is connected to the B3 barrel; Phase 9 - muffling - in this phase the BE kegs, 3/10 BSA BSA FIGURE 3 BSC BSC FIGURE 4 FIGURE 5 Petition 870180018338, of 03/07/2018, p. 49/56 3 - COAL AND COMBUSTIBLE GAS GENERATION PROCESS, for the pyrolytic conversion of wood or lignocellulosic materials into coal, under the conditions of temperature and pressure, according to claim 2, characterized by the use of an input keg in the reactors (BE ), from an outlet barrel in the reactors up to a temperature of 850 ° C (BSC) for circulating gases in the 10 battery and an output barrel in the reactors between the temperatures of 850 ° C and 1,100 ° C (BSA) to feed the thermal power plant; these barrels (BE, BSC and BSA), which are connected to the B1, B2E, B2S, B3, B4 to B9, BE, BSA, BSC, controlled by valves V1 to V17, activated 15 by computer, promote the circulation of gases generated in the total processing of materials. 3/11 non-condensable fuels through a steam reforming process in a pressurized environment, saturated with carbon and water vapor; the non-condensable combustible gases obtained will be used as fuel in 4/10 HOURS 4-44 444 4444 444 4444 444 444 444 444 444 H44 444 4444 444 4444 444 444 444 444 444 R2 R4 R6 R8 R10 R12 R14 R16 R18 R20 R22 FIGURE 1 Petition 870180018338, of 03/07/2018, p. 47/56 4 - SYSTEM for converting pyrolytic wood or lignocellulosic materials into coal, characterized by comprising a set of cylindrical reactors 20 horizontal, internally coated with refractory material, connected to metal kegs (B1, B2E, B2S, B3, B4 to B9, BE, BSA, BSC), externally coated with refractory material, whose functions of directing gases for heating and drying, cooling and reform 25 and gas cracking are controlled by valves (V1 to V17) installed in the barrels; presenting 12 phases, of which, Phase 1 - reactor discharge / loading operation - the reactor is at atmospheric pressure and at room temperature, the gas inlet barrel in the BE reactor 30 is connected to the B9 barrel, the BSA outlet and feed barrel and the BSC outlet and circulation barrel are connected to the B4 barrel; Phase 2 - emptying the Petition 870180044344, of 05/25/2018, p. 9/15 4/11 BE barrel is connected to barrel B5 and barrel BSC is linked to barrel B6; Phase 5 - carbonization of the material hung from 280 ° to 550 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B6 barrel; Phase 6 - carbonization of the material hung from 550 ° to 850 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B5 barrel; Phase 7 carbonization of the material hung from 850 ° to 1,100 ° C - the gases produced in this phase are directed to the power generation unit, the BSC barrel is closed, the BE barrel is connected to the B1 barrel and the BSA barrel is connected to the barrel B3; Phase 8 - cracking of gases from other phases - the gases produced in the other phases are injected into the reactor to crack these, the cracked gases are directed to the power generation unit, the BSC keg is closed, the BE keg is connected to the keg B6 and barrel BSA are connected to barrel B3; Phase 9 - muffling - in this phase the BE, BSA and BSC barrels are closed and the reactor remains pressed; Phase 10 - cooling, recirculation in a heat exchanger - in this phase the hanged material is cooled by gases already cracked in the previous phases, the BSA keg is closed, the BE keg is connected to the B2E keg and the BSC keg is connected to the B2S keg; Phase 11 - cold gas removal, gas vacuum - in this phase the combustible gas present inside the reactor is removed in a vacuum, the BE and BSA kegs are closed and the BSC keg is connected to the B7 keg; Phase 12 - ventilation for CO removal - in this phase the fuel gas still present inside the reactor is removed, the BSA keg is closed, the BE keg is from 05/25/2018, p. 8/15 5/10 HOURS 124 567 89 10 11 FIGURE 7 Petition 870180018338, of 03/07/2018, p. 51/56 5 connected to the B2E barrel and the BSC barrel is connected to the B2S barrel; Phase 11 - cold gas removal, gas vacuum - in this phase the combustible gas present inside the reactor is removed in a vacuum, the BE and BSA kegs are closed and the BSC keg is connected to the B7 keg; Phase 10 12 - ventilation for CO removal - in this phase the fuel gas still present inside the reactor is removed, the BSA keg is closed, the BE keg is connected to the B9 keg and the BSC keg is connected to the B4 keg. 15 9 - METHOD for the pyrolytic conversion of wood or lignocellulosic materials into coal, according to claim 8, characterized by promoting the creation of an environment subjected to controlled pressure, varying between -2 bar and 8 bar, final temperatures between 900 ° C e 20 1,200 ° C and carbonization period between 22 and 28 hours. 10 - METHOD for the pyrolytic conversion of wood or lignocellulosic materials into coal, according to claims 8 and 9 characterized by having a closed system with connections for gas exchange and reform, under the 25 controlled use of pressure, with minimum pressurization intervals of -2 bar and maximum of 8 bar. Petition 870180044344, of 05/25/2018, p. 15/15 5 BE reactor is connected to the B9 barrel, the BSA outlet and supply barrel and the BSC outlet and circulation barrel are connected to the B4 barrel; Phase 2 reactor emptying, air vacuum - BE and BSA barrels are closed, BSC barrel is connected to B8 barrel; 10 Phase 3 - filling the reactor with hot gas - the BSA and BSC kegs are closed, BE keg is connected to the B5 keg; Phase 4 - drying of the hanged material to 280 ° C - the BSA keg is closed, the BE keg is connected to the B5 keg and the BSC keg is connected to the 15 barrel B6; Phase 5 - carbonization of the material hung from 280 ° to 550 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B6 barrel; Phase 6 - carbonization of the material hung from 550 ° to 850 ° C - the BSA barrel is 20 closed, barrel BE is connected to barrel B1 and barrel BSC is connected to barrel B5; Phase 7 carbonization of the material hung from 850 ° to 1,100 ° C - the gases produced in this phase are directed to the power generation unit, the BSC barrel is closed, 25 the BE barrel is connected to the B1 barrel and the BSA barrel is connected to the B3 barrel; Phase 8 - cracking of gases from other phases - gases produced in other phases are injected into the reactor for cracking of these, the cracked gases are directed to unity in 30 power generation, O BSC barrel is closed, O BE barrel is connected to barrel B6 and the barrel BSA are connected to the B3 barrel; Phase 9 - muffling - in this phase the BE, BSA and BSC barrels are closed and the reactor Petition 870180044344, of 05/25/2018, p. 14/15 11/11 remains under pressure; Phase 10 - cooling, recirculation in a heat exchanger - in this phase the hanged material is cooled by gases already cracked in the previous phases, the BSA keg is closed, the BE keg is 5 for the recovery boiler; valve V10 that controls the injection of gases from the BSA outlet barrel, from the carbonization reactors to 1,100 ° C and cracking, in the B3 barrel to feed the UTE; valve V11 that controls the removal of fuel gas remaining in the reactor 10 in withdrawal of cold gas, for the B7 barrel; valve V12 that controls the removal of atmospheric air in the reactor after closing the door, for the B8 barrel; valve V13 that controls the access of the BE inlet pipeline to the B4 of the unloading / loading reactor; 15 valve V14 that controls the access of the pipeline from the outlet BSC to the B4 of the unloading / loading reactor; valve V15 that controls the injection of atmospheric air from the B9 barrel into the reactor to remove CO; V16 valve that controls the outflow of gases in the 20 BSA barrel; valve V17 that controls the access of the piping from the outlet BSA to the B4 of the unloading / loading reactor. 5 - SYSTEM for converting pyrolytic wood or lignocellulosic materials into coal, according to the Claim 4, characterized by using the B9 barrel connected to the air supply fan (1) as additional components; the B1 barrel connected to the oxygen reservoir (2), the compressor (3) and PSA system oxygen equipment (4); O 15 barrel B8 connected to the air purge for atmosphere (5), the compressor (6) and the air vacuum tank (7); the B4 barrel connected to the chimney exhaust set (8); the B3 barrel connected to the compressor (9) and the heat recovery boiler 2 (10); the B7 barrel 20 connected to the cold combustible gas vacuum tank (11) and the Compressor (12); the B2 keg connected to the heat recovery boiler 1 (13), the compressor (14) and the cold fuel gas tank (15); compressor (9) and the cold fuel gas tank (15) connected to the system 25 gas cleaning (17); the gas cleaning system (17) connected to the gas turbine (16); the gas turbine (16) connected to the heat recovery boiler 3 (18), the heat exchanger in the steam circuit (19) and the steam turbine (20); the heat recovery boiler 1 (13) and the 30 heat recovery boiler 2 (10) connected to the heat exchanger in the steam circuit (19). Petition 870180044344, of 05/25/2018, p. 11/15 5 removed, barrel BSA is closed, barrel BE is connected to barrel B9 and barrel BSC is connected to barrel B4. 5 B5; Phase 4 - drying of the hanged material to 280 ° C - the BSA keg is closed, the BE keg is connected to the B5 keg and the BSC keg is connected to the B6 keg; Phase 5 - carbonization of the hanged material from 280 ° to 550 ° C - the BSA barrel is closed, the BE barrel is closed 10 connected to barrel B1 and barrel BSC is connected to barrel B6; Phase 6 - carbonization of the material hung from 550 ° to 850 ° C - the BSA barrel is closed, the BE barrel is connected to the B1 barrel and the BSC barrel is connected to the B5 barrel; Phase 7 - carbonization of 15 material hung from 850 ° to 1,100 ° C - the gases produced in this phase are directed to the power generation unit, the BSC barrel is closed, the BE barrel is connected to the B1 barrel and the BSA barrel is connected to the B3 barrel; Phase 8 - gas cracking 20 from other phases - the gases produced in the other phases are injected into the reactor to crack these, the cracked gases are directed to the power generation unit, the BSC barrel is closed, the BE barrel is connected to the B6 barrel and the BSA barrel 25 are connected to barrel B3; Phase 9 - muffling - in this phase the BE, BSA and BSC barrels are closed and the reactor remains pressed; Phase 10 - cooling, recirculation in a heat exchanger - in this phase the hanged material is cooled by gases already cracked in the phases Previous 30, the BSA barrel is closed, the BE barrel is connected to the B2E barrel and the BSC barrel is connected to the B2S barrel; Phase 11 - removal of cold gas, gas vacuum - in this phase the combustible gas present inside Petition 870180044344, of 05/25/2018, p. 10/15 5/11 connected to barrel B9 and barrel BSC is connected to barrel B4. 5 equipment for electricity generation. 5 BSA and BSC are closed and the reactor remains pressed; Phase 10 - cooling, recirculation in a heat exchanger - in this phase the hanged material is cooled by gases already cracked in the previous phases, the BSA barrel is closed, the BE barrel is connected to the B2E barrel and the 10 BSC keg is connected to the B2S keg; Phase 11 cold gas removal, gas vacuum - in this phase the combustible gas present inside the reactor is removed in a vacuum, the BE and BSA kegs are closed and the BSC keg is connected to the B7 keg; Phase 12 - ventilation for 15 CO removal - in this phase the fuel gas still present inside the reactor is removed, the BSA keg is closed, the BE keg is connected to the B9 keg and the BSC keg is connected to the B4 keg; using a battery of metallic, cylindrical, coated reactors 20 internally by thermal insulating materials, horizontally arranged in pairs, with a number of battery reactors equal to the total processing time in hours of the materials, charged by batch; reactors connected to metal barrels (B1, B2E, B2S, B3, B4 a 25 B9, BE, BSA, BSC), externally coated with thermal insulating materials, for the collection of all gases produced during the drying and carbonization processes of the materials (drying up to 280 ° C; carbonization from 280 ° to 550 ° C; carbonization from 550 ° to 850 ° C; carbonization from 850 ° 30 to 1,100 ° C; and cracking of gases); such kegs direct the gases to mix and homogenize these gases, promoting their use as thermal fluid and transforming them into gases Petition 870180044344, of 05/25/2018, p. 6/15 6/10 HOURS Petition 870180018338, of 03/07/2018, p. 52/56 6 - SYSTEM for the pyrolytic conversion of wood or lignocellulosic materials into coal, according to claims 4 and 5, characterized by promoting in the set of barrels (BE, BSC, BSA, B1 A B9), the direction of the gases as thermal fluid for heat transmission for the heating and drying phases of the material being hung; directing the gases as a thermal fluid to cool the hanged material; the mixture of gases; directing the gases for reform and cracking. 6/11 reactor, air vacuum - BE and BSA barrels are closed, BSC barrel is connected to B8 barrel; Phase 3 - filling the reactor with hot gas - the BSA and BSC kegs are closed, BE keg is connected to the keg 7/10 FIGURE 9 Petition 870180018338, of 03/07/2018, p. 53/56 7 - SYSTEM for the pyrolytic conversion of wood or lignocellulosic materials into coal, according to claims 4 to 6, characterized by having a V1 valve that controls the flow of gases in the BE barrel and isolates the other barrels, allowing the injection of oxygen only through the BE barrel; valve V2 that controls the outflow of gases in the BSC barrel; valve V3 that controls the injection of oxygen from barrel B1 into barrel BE; valve V4 that controls the entry of gases from barrel B2, from the recovery boiler to the cooling of the produced coal; valve V5 that controls the entry of gases from the B5 barrel, from the carbonization reactors from 550 ° to 850 ° C in the BE barrel, for drying the material up to 280 ° C; valve V6 that controls the entry of gases from the B6 barrel, from the reactors drying to 280 ° C and carbonization up to 550 °, in the BE barrel, for reforming and cracking; valve V7 that controls the injection of gases from the BSC outlet barrel, from the carbonization reactors to 1,100 ° C, in the B5 barrel, to be injected into the reactors in material drying up to 280 ° C; V8 valve that controls the injection of gases from the BSC outlet barrel of the reactors in drying up to 280 ° C and from 05/25/2018, p. 12/15 7/11 of the reactor is removed in a vacuum, the BE and BSA barrels are closed and the BSC barrel is connected to the B7 barrel; Phase 12 - ventilation for CO removal - in this phase the combustible gas still present inside the reactor is 8/10 FIGURE 10 Petition 870180018338, of 03/07/2018, p. 54/56 8 - METHOD for converting pyrolytic wood or lignocellulosic materials into coal, according to 25 any one of claims 1, 2 and 3, characterized by promoting electronic control and monitoring and simultaneous operation of the reactor set in order to allow the collection of gases generated in the pyrolysis process, the mixing of these gases and the reform and / or 30 cracking of these gases inside the reactors at temperatures between 1,200 and 900 ° C, in an environment with pressure between 5 and 8 bar to obtain continuous non-condensable combustible gases, for use in the generation of Petition 870180044344, of 05/25/2018, p. 13/15 10/11 electrical energy; referred process presenting 12 phases, being Phase 1 - reactor discharge / loading operation - the reactor is at atmospheric pressure and at room temperature, the gas inlet barrel in the 11/11 9/10 Petition 870180018338, of 03/07/2018, p. 55/56 9/11 carbonization up to 550 ° C, in the B6 barrel, for injection in the cracking reactors; V9 valve that controls the outlet of gases from the BSC keg, from reactors in cooling of the carbonized material, in keg B2, 10/10 FIGURE 12 Petition 870180018338, of 03/07/2018, p. 56/56