BRPI1001589B1 - CIRCULATING FLUIDIZED BED GASIFICATION EQUIPMENT AND PROCESS - Google Patents

Abstract

circulating fluidized bed gasification equipment and process. The present invention relates to an equipment and a circulating fluidized bed gasification process which belongs to the field of chemical and mechanical engineering, said equipment consisting of a reactor (2) of vertical cylindrical structure whose lower tremor is provided. of a plenum (3) superimposed by a grid (18), and inside said reactor (2) is installed an internal cyclone (4) capable of increasing the processing levels inside the reactor, and mainly reducing the emission of compounds that affect the environment.

Description

Field of Invention [001] The present invention belongs to the field of chemical and mechanical engineering and aims at a circulating fluidized bed gasifier equipment, as well as a circulating fluidized bed gasification process, pressurized or not, whose fuel used for this The end presents “carbonaceous” elements in its composition, such as mineral coal and biomass.

[002] More preferably, the present invention relates to a gasification equipment that comprises a reactor within which a pressurized environment with a high temperature is created, where carbonaceous materials are gasified in order to form gas flows conducive to industrial use, for example, for power generation, or in processes for obtaining chemicals.

[003] The main importance of the gasifier, according to the present invention, is the fact that it allows the processing of a very wide variety of materials, in order to provide the reduction of the generation of residues harmful to the environment and to man.

[004] Still, it is the objective of the present invention, to provide a process associated with the aerator equipment that offers low cost for its industrial feasibility, combined with the requirements of robustness, economy, reliability and utility practicality, offering an option in relation to the gasification plants conventional.

Background of the invention [005] As should be appreciated by those skilled in the art, the gasification process is carried out by the partial oxidation of a fuel that generates as a product a mixture of combustible gases such as H2, CO, CH4,

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2/19 heavier CnHm gases in smaller quantities and inert gases such as CO2 and N2 and impurities.

[006] By the direct use of the air / steam mixture, in the gasifier, there is a low calorific gas from 1,100 to 1,500 kcal / Nm ³ . This gas can be used in industrial processes that require thermal energy and, if properly cleaned, it can be used in an electric power generation unit, such as in electric motor generators or turbines coupled to electric generators or, still, in industrial applications for the production of chemicals.

[007] Fossil fuels that can be gasified are: mineral coal, anthracite or bituminous, tars, shale, heavy oils derived from petroleum etc., normally rich in C and H2, O2, S, with or without significant ash .

[008] Biomasses are also liable to be gasified, such as wood and derivatives, peat, vegetable or animal oils, sludge, part of urban waste, etc., and which have a high concentration of C, H2, O2, little or none S, but with a greater tendency to form tar, generally with high humidity (52% bu for bagasse) and heterogeneity.

[009] The gasifying agents can be air, naturally composed of oxygen (20-21%), nitrogen (78-80%) and other gases such as water vapor.

[0010] The main gasification reactions that occur in a circulating fluidized bed reactor are:

1) Exothermic reaction (combustion reaction, formation of carbon dioxide):

C (solid) + O2 (gas) <=> CO (gas)

2) Exothermic reaction (partial combustion, formation of monoxide

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3/19 carbon):

C (solid) + ¹ Z. O2 (gas) <=> CO2 (gas)

3) Endothermic reaction (gas-water “fasel” reaction):

C (solid) + H2O (gas) <=> CO (gas) + H2 (gas)

4) Exothermic reaction (gas-water reaction “phase 2”):

CO (gas) + H2O (gas) <=> CO2 (gas) + H2 (gas)

5) Exothermic reaction (water vapor formation reaction):

H2 (gas) + ¹ Z. O2 (gas) <=> H2O (gas)

6) Endothermic reaction (Boudouard reaction):

C (solid) + CO2 (gas) <=> 2 CO (gas)

7) Exothermic reaction (methanization reaction 1):

C (solid) + 2 H2 (gas) <=> CH4 (gas)

8) Exothermic reaction (methanization reaction 2):

CO (gas) +3 H2 (gas) <=> CH4 (gas) + H2O (gas) [0011] One of the drawbacks found in gasification equipment known in the state of the art and available on the market is in relation to the fact that they present limitations regarding the gasification process, since they are unable to gasify a wide range of carbonaceous fuels, that is, they use only certain materials, such as wood or oils.

[0012] Another very relevant inconvenience is that conventional gasifiers known in the state of the art, produce a very low level of gasification of the fuel, that is, there is a surplus of residues not fully involved in gasification, so that not all chemical reactions are effective.

[0013] Such a condition of partial gasification results in the formation of gases with high levels of compounds such as tars, acids and aldehydes, which are often toxic and harmful to the environment.

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4/19

Description of the invention [0014] In order to solve and / or reduce the aforementioned drawbacks in relation to the state of the art, it is the objective of the present invention to provide an aerator equipment that improves the conversion of the fuel to be aerated, considerably reducing the levels of waste harmful to the environment.

[0015] More particularly, the objective of the present invention is a gasifying equipment of cylindrical structure in stainless steel coated internally with material of low thermal conductivity, where several carbonaceous materials are gasified.

[0016] Advantageously, the gasifying equipment, according to the present invention, internally comprises a series of systems to activate the upward and downward flow of gases and particulate material at high temperature, in order to guarantee that all chemical reactions of an extensive chain take place.

[0017] Also, inside the aforementioned gasifying equipment, a specially designed cyclone is installed which aims to recycle the unconverted carbons and assist in the cracking of gas-driven tars in the fuel pyrolysis process.

[0018] The gasifying equipment, object of the present invention, works in conjunction with several other automatic devices for the supply of raw material, such as valves, filtration systems, multicyclones, among other support items.

[0019] Still, the objective of the present invention is a gasification process whose steps are conducted by means of the equipment as mentioned above, being able to reduce the number of components necessary for the proper processing of the fuel, which are conveniently configured and arranged for perform their duties

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5/19 with efficiency and versatility.

Brief Description of the Drawings [0020] These and other objectives, technical effects and advantages of the gasifying equipment, as well as the gasification process, according to the present invention, will be apparent to those skilled in the art from the attached schematic figures, which illustrate exemplary achievements , and not limiting, of the present invention, which:

[0021] Figure 1 - Top perspective view of the circulating fluidized bed gasifier equipment, according to the present invention.

[0022] Figure 2 - Perspective view of the circulating fluidized bed gasifier equipment illustrated in Figure 1, with the secondary air exchanger illustrated in Figures 10 and 11.

[0023] Figure 3 - Top exploded view of the circulating fluidized bed gasifier equipment, according to the present invention.

[0024] Figure 4 - Top exploded view of the circulating fluidized bed gasification equipment, where the internal cyclone can be seen.

[0025] Figure 5 - Top perspective view of the hopper used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0026] Figure 6 - Top perspective view of the extractor conveyor used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0027] Figure 7 - Top perspective view of the feed valve used in the circulating fluidized bed gasifier equipment, according to the present invention.

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6/19 [0028] Figure 8 - Top perspective view of the limestone feed thread used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0029] Figure 9 - Top perspective view of the ash extractor used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0030] Figure 10 - Top perspective view of the secondary preheater exchanger for process air / steam used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0031] Figure 11 - Top perspective view of the secondary preheater exchanger for the process air / steam illustrated in Figure 10 from another angle.

[0032] Figure 12 - Top perspective view of the multicyclone used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0033] Figure 13 - Bottom perspective view of the multicyclone illustrated in Figure 12.

[0034] Figure 14 - Top perspective view of the primary process air / steam exchanger used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0035] Figure 15 - Top perspective view of the primary process air / steam exchanger illustrated in Figure 14.

[0036] Figure 16 - Perspective view of the steam generating exchanger.

[0037] Figure 17 - Top perspective view of the "boiler" used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0038] Figure 18 - Top perspective view of the “boiler”

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7/19 used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0039] Figure 19 - Front perspective view of the line pressure regulating valve used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0040] Figure 20 - Rear perspective view of the line pressure regulating valve illustrated in Figure 19.

[0041] Figure 21 - Perspective view of the “flare” used in the circulating fluidized bed gasifier equipment, according to the present invention.

[0042] Figure 22 - Top perspective view of the “flare” used in the circulating fluidized bed gasifier equipment, illustrated in Figure 21 from another angle.

Description of Realizations of the Invention [0043] According to the figures indicated above, particularly with respect to Figures 1, 2, 3 and 4, the circulating fluidized bed gasifier equipment 1, object of the present invention, consists of a reactor 2 of vertical cylindrical configuration, built in carbon steel and lined internally with refractory material. The dimensions of said cylindrical structure, such as height and diameter, are determined according to the capacity and type of fuel to be gasified.

[0044] In a preferred embodiment, the entire structure of reactor 2 is coated with refractories, which allows the internal temperature to be maintained between 750 and 1050 ° C, reducing heat loss to the environment.

[0045] The base of the cylindrical structure is equipped with a Plenum ”3, whose purpose is to stabilize the air pressures, during the gasification processes, through the feeding of a grid 18, on which the chemical reactions mentioned above occur.

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8/19 [0046] Preferably, said grid 18 is intended to serve as a support for the bed, to distribute all the air uniformly throughout the reactor area, to eliminate ashes and sintering stones that are formed during the process, as well as how to eliminate any stones and tailings that come with the fuel. The grid is equipped with nozzle orifices to provide uniform distribution of air in the bed, and the configuration of these nozzles is calculated according to the operating condition designed by the technicians in the subject.

[0047] In a preferred embodiment of the present invention, the preheated air, at a temperature of 100 to 600 ° C, is blown through the grid with a constant pressure between 0.15 bar and 2.00 bar, allowing for a distribution homogeneous through each injection nozzle.

[0048] The diameter of the nozzle orifices should be adjusted so that an air velocity inside the nozzle is obtained, between 100 to 150 m / s, which causes turbulence inside the reactor 2.

[0049] In a preferred embodiment, said grid 18 has a tapered profile and presents a pressure loss between 300 to 600mmCA.

[0050] As you can see in figures 1-4, the air preheated with temperature between 100 to 600 ° C is supplied through an air tubing 5, which is responsible for transferring the preheated air from the reactor head ( heat exchanger) for said Plenum ”3.

[0051] Internally, the reactor 2 comprises an internal cyclone 4 whose purpose is to separate the solid particulate materials present in the gas, returning them to the reactor bed. In addition, said internal cyclone constitutes a heated surface in order to cause the cracking of tars.

[0052] The internal cyclone is designed to retain materials

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9/19 particles above 80pm, which are returned to the bed, in order to provide the recirculation of unconverted carbonaceous materials. In a preferred embodiment, the structure of said internal cyclone 4 is made of refractory stainless steel to withstand internal temperatures in the range of 850 to 1050 ° C.

[0053] Thus, it appears that through the said internal cyclone 4, the gasifying equipment, according to the present invention, allows the recycling of products entrained by the gas causing a circulation or reconduction of the non-converted carbonaceous materials into the bed , with this, it is possible to increase the efficiency of the gasification process.

[0054] In a particularly advantageous embodiment, the internal temperature of the reactor body 2 remains between 750 to 1050 ° C, and the gases formed travel through the entire body until the entrance of internal cyclone 4 at a speed of 1 to 2 m / s pressure between 0.15 to 2.00 bar.

[0055] The formation gases must remain inside the reactor for approximately 5-7 seconds, so that the chemical reactions gas-gas / solid-gas, occur with a high degree of conversion, as well as to obtain the cracking of the tar.

[0056] Due to high temperatures, low speeds and a relatively long residence time, the tar generated in the bed, during the pyrolysis phase, is broken or cracked into shorter chains, due to the reactor body and the internal cyclone, resulting in gases considered heavier, such as CnHm.

[0057] The gasifying equipment, object of the present invention comprises a feeding system, whose purpose is to provide fuel to the reactor, particularly within the bed. As an example, in small reactors the fuel is inserted into the reactor by a thread without

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10/19 end, which is located at a height just above the bed. As should be appreciated by those skilled in the art, other ways of conducting fuel can be adopted without thereby departing from the scope of the present invention.

[0058] In a preferred embodiment, the feeding system is mostly made of refractory stainless steel, in order to withstand internal temperatures in the range of 850 to 1050 ° C. In addition, having the ability to allow fuel to enter the reactor, without the escape of combustible gases into the atmosphere.

[0059] In a preferred embodiment, the fluidized oil, according to the present invention, consists of a mixture of solids and gases at a temperature of 850 to 1050 ° C. Said mixture is maintained in a fluidized state, by the flow of heated air from “Plenum” 3, through grid 18. On the one hand, the solid portion is composed of quartz, fuel ashes, unconverted carbon and the fuel itself. On the other hand, the gaseous portion is mainly composed of CO, CO2, CH4, H2O and N2.

[0060] This bed is where the main chemical reactions and mass transfers between the solid and gaseous phase occur. This is because the movement in the bed is disordered and turbulent, characteristics that promote the intense contact of the solid carbon of the fuel with the gases, providing mass transfer and heat exchanges. This disordered and turbulent movement causes the particles of the bed to have the characteristics of a fluid or a fluidized bed.

[0061] The atmospheric air inflated has temperatures between 100 to 600 ° C depending on the fuel to be used. In this temperature range, the air increases its volume, improving fluidization, and the oxygen concentration remains below the stoichiometric, because as

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11/19 cited, the gasification process is characterized by partial oxidation of carbon.

[0062] The carbon present in the fuel must remain in the bed between 30-90 minutes for all chemical reactions to occur, as previously indicated.

[0063] Additionally, as shown in the other Figures 522, the circulating fluidized bed gasifier equipment 1, according to the present invention, is connected to a gasification plant that comprises complementary equipment whose purposes are to provide an automated, low complexity and also with high performance.

[0064] In preferred embodiments, said gasification plant is composed, among other accessories, of the following components:

Moega [0065] As illustrated in Figure 5, the hopper 6 comprises a structure that makes it possible to automatically receive all the fuel to be gasified, that is, all the raw material that will be supplied to the gasifying equipment of the present invention.

[0066] Said material is dumped through transport carts without the intervention of a worker. In addition, in a preferred embodiment, the dimensioning of said hopper 6 is determined in order to provide a material storage capacity sufficient to meet at least 10 hours of operation of the gasification plant.

Extractor Conveyor [0067] Figure 6 illustrates an extractor conveyor 7 of the raw material stored in said hopper 6. More particularly, said extractor conveyor 7 is installed under the hopper 6, in order to allow the extraction, conduction and feeding of the raw material in the equipment

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12/19 aerator.

[0068] The said extractor conveyor comprises a conveyor, supported by rollers, which are properly dimensioned, and positioned at the bottom of the hopper 6, with frequency inverters being installed to allow the determination of the amount of raw material to be extracted and which will be conducted to supply gasification equipment 1.

Crusher feeder conveyor [0069] Coupled to said extractor conveyor 7, there is a conveyor belt that feeds a crusher. In other words, this conveyor receives the raw material that is carried by the extractor conveyor 7 and unloads it in a crusher.

Crusher [0070] This crusher receives the raw material supplied by the feeder conveyor and processes the material, which is ground until it reaches a uniform granulometry and less than 5mm.

Feeding silo loading conveyor [0071] After processing in said crusher, the resulting grains are loaded by a conveyor that transfers them from the crusher to a feeding silo.

Feeder SILO [0072] A feeder silo is installed in the upper part of the reactor 2, and allows to store the raw material already with the appropriate granulometry adjusted. In a preferably advantageous embodiment, the storage capacity of said silo must be sufficient to meet at least 8 hours of nominal consumption of the plant.

Dosing conveyor [0073] At the exit of said feeder silo, a dosing conveyor is installed, particularly under said silo, in order to

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13/19 extract the stored material and automatically determine the appropriate dosage for feeding said reactor 2.

Feeding valves [0074] Figure 7 illustrates a feeding valve 8. According to a preferred embodiment, the gasifier equipment 1 is coupled with a set of 4 valves 8, which receive the raw material from the dosing conveyor and introduces it into the reactor 2.

[0075] In a particularly advantageous manner, said feeder valves 8 are provided with hydraulic actuation and operate in such a way that 2 valves are always in the closed state. This is because this arrangement prevents combustible gases from inside reactor 2 from leaking into the atmosphere.

Feeder thread [0076] In an alternative embodiment, especially when referring to smaller gasification plants, it is possible to adopt a helical thread 9, which receives the raw material from the feeder valves 8 and introduces it inside the reactor 2.

[0077] In projects in which the gasification plants are larger and large, it is common for the raw material to be fed on top of the reactor, by gravity.

Secondary air exchanger [0078] Figures 10 and 11 illustrate a secondary air exchanger 12 whose purpose is to conduct the gases generated in the reactor 2, in order to recover part of the sensitive heat of these gases and heat the process air, which is conducted in the preheated form to Plenum ”3. Thus, the gases generated leave the reactor at a temperature close to 700 ° C to 850 ° C, depending on the temperature chosen for operation of the reactor, and then heat the air that will feed the process.

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14/19

Multicyclones [0079] Figures 12 and 13 illustrate the set of multicyclones 10, which receives the gas from the secondary exchanger, separates the fines carried by the gases and sends them back to the reactor through two hydraulically controlled valves. These valves prevent gases from escaping from inside the reactor to the gas line.

PRIMARY AIR EXCHANGER [0080] Figures 14 and 15 illustrate a primary air exchanger 11, whose purpose is similar to the secondary air exchanger 12, but at a later time. More particularly, said secondary air exchanger 12 captures the gases that are expelled by the multicyclones 10 in order to recover part of the sensitive heat of the gases and heat the process air.

STEAM GENERATOR EXCHANGER [0081] Additionally, as shown in Figure 16, it is possible to have a steam generator exchanger 17 at the outlet of said primary air exchanger 11.

[0082] This aforementioned steam generator exchanger is basically a gas / water heat exchanger that recovers even more sensitive heat from the gases and is also capable of generating steam for the process, since steam can be a of the aerating elements. This steam generator exchanger 17 works with a pressure of 3 to 5 bar, and has the capacity to generate 30% by weight of the product mass introduced in the system when in normal working regime.

Boiler [0083] Figures 17 and 18 illustrate a boiler 13, which comprises a reservoir that is constructed of carbon steel. The function of the said boiler 13 is to collect the steam produced in the steam generator exchanger 17, in order to store it to promote the separation between the saturated steam and the

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15/19 condensed steam. This is so that, at a later time, the condensed steam returns to the valves of the primary air exchanger, and the saturated steam is used to supply other equipment, for example, energy generators.

Ash extractor [0084] Figure 9 illustrates an ash extractor 14 comprised of a structure that is installed in the lower region of the reactor 2, in order to collect the ash discharged from the bed, and transport it out of the reactor.

[0085] Preferably, there is a container called "ash cooler" that also receives steam, in order to cause the cooling of these ashes. Then a helical thread can transport the ash out of the reactor.

[0086] In one embodiment, a valve is arranged before and another after the mentioned ash cooler, both hydraulically controlled, and make it possible for the ashes to leave the reactor without gases escaping into the atmosphere.

Gas line pressure regulating valve [0087] According to Figures 19 and 20, it appears that the gasification plant comprises, in one embodiment, a pressure regulating valve 15 whose purpose is to guarantee the pressure of the gas line even with the change in demand by the user.

[0088] More particularly, said valve 15 is automatic and pneumatically or hydropneumatically controlled, so that, in addition to ensuring the stability of the line pressure, it provides that, if the demand should fall below the minimum limit of the plant, part of gas is diverted to a “flare” 16.

Flare [0089] Figures 21 and 22 illustrate said flare 16, which is comprised of a burner installed at the gas outlet, in order to

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16/19 to burn them when the gas consumption is low, thus allowing the low flow not to affect the fluidization of the bed.

[0090] In addition, flare 16 has the function of burning the gases formed at the beginning of the process that are not yet in conditions of use in the processing. Thus, said flare 16 has an auxiliary LPG burner that lights up at the beginning of the operation and then goes out when the flare is in steady state, or deactivated.

Desulfurization system [0091] In a preferred embodiment, the gasifying equipment 1 can also be coupled to a plant equipped with a desulfurization system, which is essential in cases where the raw material has sulfur and requires removal H2S produced in the bed.

[0092] This system is comprised of a limestone storage and dosing silo capable of providing the dosage of limestone to the product in a controlled manner, via a frequency inverter.

[0093] The amount of lime is dosed according to the amount of sulfur in the product. A chemical reaction occurs inside the reactor bed, which produces calcium sulfide (CaS), which is precipitated and then discarded with ashes, namely:

CaCOa + H2S CaS + H2O + CO2.

Gasification agent [0094] In accordance with the present invention, the gasification agent enters said primary air exchanger 11, and begins a heating process in the opposite direction to that of the gas, until it reaches the reactor head 2. At the head from the reactor 2 the mixture is heated to a temperature above 500 ° C, and through the air duct or pipe 5 it feeds the Plenum ”3.

Process air [0095] Process air according to the present invention is

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17/19 compressed in air compressors (type blowers for pressures up to 0.25 bar; and turbo compressors for pressures above, and up to 1.3 bar). It passes through a “lung” reservoir, for equalizing and regulating pressures, and then goes to a pressure regulating valve that feeds the gasification process.

Gas cleaning system [0096] Also, in an embodiment of the present invention, it is also possible to have a gas cleaning system, in which the fuel gas, after passing through the steam generator exchanger, undergoes a process to remove the particulates, through 2 washers, one scrubber type scrubber and another type “Ventury” type, guaranteeing 99% cleaning.

[0097] The washing water with the particulates falls into a metallic tank, and later, by decantation, the fines are removed by a drag conveyor.

[0098] The waters are taken by pumps to a cooling tower, and complete the cycle, returning to the washers properly cooled to 35 ° C.

[0099] As previously mentioned, the present invention also relates to a gasification process, which is conducted preferably through the gasifying equipment described above.

[00100] The gasification process, according to the present invention, begins with the heating of the reactor 2 operating in combustion regime. Said reactor 2 is fed with inert material, such as sand, to form the primary bed. This inert material is accommodated in the mentioned bed until it reaches a height of up to 300mm above the last line of the nozzles.

[00101] From this moment on, an auxiliary burner operating with LPG / oxygen is introduced in the Plenum ”3, together with the air injection

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18/19 atmospheric. This step promotes the elevation of the temperature of the primary bed, up to approximately 300 ° C, when the dosage of fuel in small proportions begins, and until the desired temperature is reached.

[00102] In preferred embodiments, the desired temperature in this step varies between 750 to 1050 ° C, and will depend directly on the type and nature of fuel that will be gasified.

[00103] When the temperature reaches a value of approximately 200 ° C below the desired temperature for gasification, automatic fuel dosing (coal, waste or biomass) begins, which is supplied in controlled quantities until the bed remains at a constant working temperature, preferably between 750 to 1050 ° C.

[00104] The fuel dosage is done in an automated way, and the reactor 2 will remain in this regime until the whole system (equipment and piping) is at a temperature between 150-180 ° C.

[00105] The gasification process consists of obtaining, inside the reactor, the conditions of pressure, temperature and fluidization mentioned above, in order to allow the chemical reactions associated with the process to be carried out properly.

[00106] Preferably, all the control of dosage and feeding of raw material / fuel is monitored and controlled by means of specific software capable of adjusting the exact and necessary quantity for the processing and gasification of the raw material / fuel.

[00107] In this sense, in a preferably advantageous embodiment of the present invention, the gasification process is basically comprised of the following steps:

a) heating of reactor 2 in the combustion process;

b) supply of reactor 2 with inert material to form a

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19/19 primary bed, preferably up to a height, close to 300mm above the last line of the nozzles;

c) activation of the auxiliary burner, introduced in Plenum ”3, together with the injection of atmospheric air, raising the temperature of the primary bed, to about 300 ° C,

d) dosing and feeding small portions of fuel, until reaching the desired temperature,

e) dosing and automatic fuel supply, until the bed remains at a constant working temperature.

[00108] The present invention has been described in order to define possible realizations of equipment and a gasification process of carbonaceous materials, such description being of an exemplary, non-limiting nature, and, therefore, a technician in the subject will know how to explore the possible variations they must also be incorporated as equivalent variants of the invention, which are incorporated into the scope of protection defined by the appended claims.

Claims (8)

Claims 1. CIRCULATING FLUIDIZED FLUIDIZING EQUIPMENT, comprising a reactor (2) with vertical cylindrical configuration, a vertical cylindrical structure, in which the lower end of the reactor connects with a plenum (3) for stabilizing air pressure , between the said reactor (2) and the “plenum” (3) there is a grid (18) provided with holes for air injector nozzles, inside the said reactor (2) an internal cyclone (4) is installed, in which the reactor (2) and the internal cyclone are made of stainless steel coated with refractory material, characterized by the fact that a base of the vertical cylindrical structure is provided with the plenum (3), the grid being arranged separating the plenum (3 ) of the reactor (2); the equipment also comprises an air pipe (5) that transfers preheated air from the reactor (2) to the plenum (3); and the refractory material of the internal cyclone comprises a heated surface, where the heated surface is adapted for cracking. 2. FLUIDIZED GAS EQUIPMENT EQUIPMENT CIRCULANT, according to claim 1, characterized by the fact that the grid has a conical profile with a head loss between 300 and 600mmCA, and the diameter of the nozzle orifices are designed in order to obtain an air outlet speed between 100 and 150m / s. 3. FLUIDIZED GAS EQUIPMENT CIRCULANT according to claim 1, characterized by the fact that it comprises an automated fuel supply system, the fuel supply system being an endless thread (9) and being arranged at a height just above the bed. 4. FLUIDIZED GAS EQUIPMENT EQUIPMENT CURRENT, according to claim 1, characterized by the fact that Petition 870180072751, of 08/20/2018, p. 12/14 2/3 also includes feeder valves (8) equipped with hydraulic actuation. 5. CIRCULATING FLUIDIZED GAS EQUIPMENT, according to claim 1, characterized by the fact that it is installed in an automated gasification plant consisting of a hopper (6), raw material / fuel conveyors, a crusher, feed silo, threads feeders (9), primary (11) and secondary (12) heat exchangers, multicyclones (10), steam generator exchanger (17), steam storage boiler (13), ash extractor (14) with ash cooler , a gas flare (16). 6. CIRCULATING FLUIDIZED FLUID GASIFICATION EQUIPMENT, according to claim 5, characterized by the fact that it additionally comprises a gas cleaning system disposed after the steam generating exchanger (17), as well as a desulfurization system. 7. CIRCULATING FLUIDIZED BED GASIFICATION PROCESS, characterized by the fact that it is carried out using a gasifying equipment as defined in any of claims 1 to 6, by means of the following steps: a) heating of the reactor (2) in the combustion process, b) feeding the reactor (2) with inert material to form a primary bed, preferably up to a height, close to 300mm above the last line of the nozzles, c) introduction of an auxiliary burner in the plenum, together with injection of atmospheric air, and raising the temperature of the primary bed to a temperature of 300 ° C; d) dosing and feeding small portions of fuel, until reaching a temperature between 750 and 1050 ° C, e) dosing and automatic fuel supply, until the Petition 870180072751, of 08/20/2018, p. 13/14 3/3 bed remains at a constant working temperature. 8. PROCESS, according to claim 7, characterized by the fact that step (e) starts from the moment when a temperature of 200 ° C below the desired working temperature is reached, being that said temperature desired working range is between 750 and 1050 ° C.