CN117398932A - Fluidized bed reaction device, control method thereof and combustion system - Google Patents

Fluidized bed reaction device, control method thereof and combustion system Download PDF

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Publication number
CN117398932A
CN117398932A CN202210806781.8A CN202210806781A CN117398932A CN 117398932 A CN117398932 A CN 117398932A CN 202210806781 A CN202210806781 A CN 202210806781A CN 117398932 A CN117398932 A CN 117398932A
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CN
China
Prior art keywords
fluidized bed
section
bed reaction
reactant
arc
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CN202210806781.8A
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Chinese (zh)
Inventor
朱书骏
吕清刚
欧阳子区
朱建国
李百航
刘敬樟
曾雄伟
朱治平
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Institute of Engineering Thermophysics of CAS
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Institute of Engineering Thermophysics of CAS
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Priority to CN202210806781.8A priority Critical patent/CN117398932A/en
Publication of CN117398932A publication Critical patent/CN117398932A/en
Pending legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B01J8/1827—Feeding of the fluidising gas the fluidising gas being a reactant
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
    • B01J8/38—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it
    • B01J8/384—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only
    • B01J8/388—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed containing a rotatable device or being subject to rotation or to a circulatory movement, i.e. leaving a vessel and subsequently re-entering it being subject to a circulatory movement only externally, i.e. the particles leaving the vessel and subsequently re-entering it
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/002—Fluidised bed combustion apparatus for pulverulent solid fuel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/22—Fuel feeders specially adapted for fluidised bed combustion apparatus
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/24—Devices for removal of material from the bed
    • F23C10/26—Devices for removal of material from the bed combined with devices for partial reintroduction of material into the bed, e.g. after separation of agglomerated parts
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN  A CARRIER GAS OR AIR 
    • F23C10/00—Fluidised bed combustion apparatus
    • F23C10/18—Details; Accessories
    • F23C10/28—Control devices specially adapted for fluidised bed, combustion apparatus

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The present invention relates to a fluidized bed reaction apparatus comprising: a reaction vessel comprising a concave arcuate section at a bottom of the reaction vessel, the reaction vessel defining a reaction space for a fluidized reaction to occur; a reactant outlet provided at the top or upper portion of the reaction vessel; and a reactant inlet disposed obliquely downward so as to be adapted to provide a reactant gas stream into the arcuate segment in an obliquely downward manner. The invention also relates to a combustion system comprising the above-mentioned fluidized bed reaction device, and to a method of controlling the above-mentioned fluidized bed reaction device.

Description

Fluidized bed reaction device, control method thereof and combustion system
Technical Field
Embodiments of the present invention relate to the field of fluidization technology, and more particularly, to a fluidized bed reaction apparatus, a method of controlling a fluidized bed reaction apparatus, and a combustion system including a fluidized bed reaction apparatus.
Background
Fluidized bed reaction devices are widely used in a variety of fields. One typical application is the treatment of solid (powdery) materials, such as the combustion, gasification or pyrolysis of solid fuels. In the case of a main reactor in the thermal reaction field such as combustion and gasification, the particle size of the fuel is usually more than 2mm. When the particle size of the fuel is reduced, for example, the particle size of the fuel is less than 1mm, the specific surface area of the fuel is increased, and the effective reaction area is increased, which is advantageous for enhancing the reaction strength of the fuel with the reactant. At the same time, the reaction intensity of the powdered fuel is increased, so that the residence time in the reaction zone can be suitably reduced, and the size of the reaction apparatus can be reduced. Thus, developing and designing a fluidized bed reactor suitable for powdered fuels is of great benefit in terms of improved fuel utilization and reduced reactor size.
In the prior art, massive or coarser granular fuel is fed into a reaction zone through a screw feeder, and an air distribution plate and an air cap are arranged at the bottom of the reaction zone to provide fluidization air which is mainly used for establishing the fluidization state of materials and is used as a reactant to participate in the chemical reaction of the fuel. The air distribution plate and the hood often bring larger pressure loss, and the running cost of the system is increased.
One of the main problems faced by fluidized bed reactors for thermally utilizing powdered fuel is that existing screw feeders are not capable of stably delivering powdered fuel into the reaction zone, and that it is a suitable means to pneumatically deliver powdered fuel into the reaction zone.
In the prior art, the fluidized bed reaction apparatus is also equipped with a fluidization fan, which requires an additional increase in equipment investment of the powder feeding fan, but this reduces economy. More specifically, in order to ensure that the powdered fuel is stably conveyed into the reaction device, a powder feeding fan and a fluidization fan are required to be simultaneously arranged, so that equipment investment and complicated flow are increased.
Meanwhile, if the reaction air needed by the fluidized bed is divided into fluidization air and powder conveying air, the fluidization air quantity is reduced under the condition of ensuring the total reaction air quantity to be unchanged, so that the bottom fluidization speed is reduced, a reaction dead zone is easy to form at the bottom of the reaction device, and the operation stability and the safety of the reaction device are further affected. More specifically, when the operation load is reduced, the total air quantity required by the reaction is reduced, and in order to keep the powder feeding speed at a certain level, the proportion of the reduced powder feeding air quantity is limited, so that the fluidization air quantity is reduced more, the bottom dead zone is enlarged, the problems of local coking and the like can be caused, and the fluidized bed device cannot safely operate.
Disclosure of Invention
The present invention is directed to at least one aspect of the problems in the prior art.
According to an aspect of an embodiment of the present invention, there is provided a fluidized bed reaction apparatus including:
a reaction vessel comprising a concave arcuate section at a bottom of the reaction vessel, the reaction vessel defining a reaction space for a fluidized reaction to occur;
a reactant outlet provided at the top or upper portion of the reaction vessel; and
a reactant inlet disposed obliquely downward so as to be adapted to provide a reactant gas stream into the arcuate segment in an obliquely downward manner.
According to another aspect of an embodiment of the present invention, there is also provided a combustion system including the above-described fluidized bed reaction apparatus.
According to a further aspect of embodiments of the present invention, there is provided a method of controlling the above fluidized bed reaction apparatus, comprising the steps of: so that the flow rate of the reactant stream entering the reaction space from the reactant inlet is always higher than 10m/s.
Drawings
The above and other aspects and features of the present invention will become apparent from the following description of embodiments taken in conjunction with the accompanying drawings, in which:
FIG. 1 is a schematic view of a circulating fluidized bed reaction apparatus according to an exemplary embodiment of the present invention;
FIGS. 2A and 2B are schematic views of the circulating fluidized bed reaction apparatus of FIG. 1, showing relevant angle and height parameters;
FIG. 3 is a schematic structural view of a bubbling fluidized bed reaction device according to an exemplary embodiment of the present invention;
FIGS. 4A and 4B are schematic diagrams of the bubbling fluidized bed reaction device of FIG. 3, showing relevant angle and height parameters;
FIG. 5 is a schematic view showing the construction of a circulating fluidized bed reaction apparatus according to another exemplary embodiment of the present invention;
fig. 6 is a schematic structural view of a bubbling fluidized bed reaction device according to another exemplary embodiment of the present invention.
Detailed Description
The following description of embodiments of the present invention with reference to the accompanying drawings is intended to illustrate the general inventive concept and should not be taken as limiting the invention.
The fluidized bed reaction apparatus of the present invention is exemplarily described below with reference to fig. 1 to 6.
The present invention provides a fluidized bed reactor in which the bottom of the reactor vessel of the reactor is an ellipsoidal/spherical arcuate segment, and the inlet of the reactant is arranged such that the inlet of the powdered fuel or powdered material is directed obliquely downward, thereby being adapted to provide a reactant stream into the arcuate segment in an obliquely downward manner.
The powdery material can be pulverized coal or biomass powder, and can also be low-volatile fuel such as semicoke fine powder.
One particular application of the above technical solution is a circulating fluidized bed gasification apparatus as powdered fuel. As shown in fig. 1, the fluidized bed reaction apparatus includes a riser 1 (as one form of a reaction vessel), a separator, and a 2-return 3. The upper part of the lifting pipe 1 is connected with a separator 2, the separator 2 is connected with a material returning device 3, the outlet of the material returning device 3 is connected with the cone structure of the lifting pipe 1, and the structure forms a circulating structure. The outlet of the return vessel 3 is connected to the lower middle cone of the riser 1 and the gasification product flows out of the top outlet pipe of the separator 2.
The powder conveying pipeline is divided into two powder conveying pipelines at a position close to the lifting pipe 1, and the two powder conveying pipelines are tangentially connected with the semi-ellipsoidal structure in a downward inclined mode. The powder feeding wind carries the powder fuel to enter the lifting pipe 1 through the powder conveying pipeline, the middle part of the powder feeding wind passes through the lifting pipe 1, the separator 2 and the circulating loop of the returning charge device 3 for several times, and the gasified product flows out from the outlet of the separator.
For the circulating fluidized bed gasification apparatus shown in fig. 1, in one embodiment, the powdered fuel is gasified in a fluidized bed reaction apparatus at an elevated temperature (700-1200 ℃) and the gasification product, including coal gas and fly ash, flows out of the separator outlet.
In the embodiment shown in fig. 1-2B, the powder conveying speed in the total powder conveying pipeline and the two branch powder conveying pipelines is always higher than 10m/s. Further, the upward flow rate of the powder conveying air flow carrying the powdery fuel in the semi-ellipsoidal body is 0.5 to 30m/s, and further 15m/s.
Another specific application of the above technical solution is a bubbling fluidized bed combustion device as powdered fuel. As shown in fig. 3, the reaction vessel 1 comprises a combustion chamber, wherein the upper part of the combustion chamber is cylindrical, the middle lower part starts to be necked down to be of a cone structure, and the bottom is of a semi-ellipsoidal shape. The powder conveying pipeline is divided into two powder conveying pipelines near the combustion chamber, and is tangentially connected with the semi-ellipsoidal structure in an inclined downward direction. The powder-feeding wind carries the powdery fuel to enter the combustion chamber through the powder-feeding pipeline, and the burnt fly ash and flue gas flow out from the top outlet.
In a bubbling fluidized bed combustion apparatus, pulverized fuel is combusted in a fluidized bed reaction apparatus at a high temperature (700-1200 ℃) and combustion products, including fly ash and flue gas, flow out from an outlet at the top of a combustion chamber.
In the embodiment shown in fig. 3-4B, the total powder conveying pipeline and the two branch powder conveying pipelines always have the powder conveying speed higher than 10m/s. Further, the upward flow rate of the powder conveying air flow carrying the powdery fuel in the semi-ellipsoidal body is 0.5 to 20m/s, and further 10m/s.
In the embodiment shown in fig. 1 and 3, the powder conveying pipeline is divided into two powder conveying pipelines with smaller diameters at the position close to the lifting pipe 1, and the two powder conveying pipelines are symmetrically arranged. The invention is not limited to the method, and the powder conveying pipeline can be divided into more powder conveying pipelines which can be arranged at equal intervals along the circumferential direction, more specifically, two paths of symmetrical powder conveying air pipe branches close to the reaction device can be replaced by four paths or six paths of symmetrical branches, the number of tangentially-entering powder feeding pipes connected with the bottom of the reaction device is increased, the flow uniformity of materials at the bottom of a reaction area is further improved, the reaction uniformity is enhanced, and a local high-temperature area is avoided. Although not shown, only one powder delivery line may be provided, which is within the scope of the present invention.
The shape of the bottom of the reaction vessel in the present invention is specifically described below. In the invention, the bottom is a concave arc section. The arcuate segment may be an ellipsoidal arcuate segment or a spherical arcuate segment, and more specifically, may be a 1/2 or 1/4 ellipsoidal structure or a 1/2 or 1/4 spherical structure.
The following specifically describes the inclined downward arrangement of the powder conveying pipeline in the present invention. As shown in fig. 1-4B, the powder conveying pipeline obliquely enters the semi-ellipsoid at a tangential angle, and the line of the plane under the pipe of the powder conveying pipeline coincides with the tangent line of the connection point of the semi-ellipsoid and the cone section on the inner surface of the semi-ellipsoid, i.e. the lower edge line of the channel space of the powder conveying pipeline coincides with the tangent line of the intrados of the arc section of the semi-ellipsoid at the upper edge. However, the above is a very specific arrangement, and the present invention is not limited thereto, as long as the powder conveying pipe is "arranged obliquely downward so as to be adapted to supply the reactant material flow into the arc-shaped section in an obliquely downward manner", which may be "the powder conveying pipe is arranged so as to meet the upper edge of the arc-shaped section and obliquely downward so as to be adapted to supply the reactant material flow into the arc-shaped section in an obliquely downward manner", further "the axis of the powder conveying pipe is arranged in parallel with the tangent line of the intrados surface of the arc-shaped section at the upper edge".
The cone angle of the cone section and the bevel angle of the powder conveying pipeline are exemplarily described below. In one embodiment of the present invention, as shown in FIGS. 2A, 2B and FIGS. 4A, 4B, 60 ° < α < 90 °: the angle of the inclined conical surface of the cone part with the horizontal plane is 60-90 degrees, wherein alpha is the angle of the inclined conical surface of the cone part with the horizontal plane. In one embodiment of the invention, α > β: the angle between the inclined conical surface of the conical part and the horizontal plane is larger than the angle between the tangent line of the connection point of the semi-ellipsoid and the conical section on the semi-ellipsoid and the horizontal plane, wherein beta is the angle between the tangent line of the connection point of the semi-ellipsoid and the conical section on the semi-ellipsoid and the horizontal plane. In one embodiment of the invention, both α and β are acute angles greater than 60 degrees.
The cross-sectional shape of the reaction vessel is specifically described below. In the embodiment shown in fig. 1 and 3, the upper part of the reaction vessel 1 is cylindrical, the middle lower part starts to shrink downwards to form a cone section, and the bottom is semi-ellipsoidal, namely, the reaction vessel 1 comprises a cylindrical section, a cone section and an arc section which are sequentially connected in the vertical direction, the upper edge of the large diameter of the cone section is connected with the cylindrical section, and the lower edge of the small diameter of the cone section is connected with the arc section. However, the present invention is not limited thereto. Referring to fig. 5 and 6, the reaction vessel 1 is integrally formed with a cone section except the bottom, as shown in fig. 5 and 6, the cylindrical structure at the upper part of the reaction device shown in fig. 1 and 3 is omitted, the whole structure at the upper part adopts a cone structure, and the bottom adopts a semi-ellipsoidal structure, so that a speed difference is always formed along the course in the reaction area, thereby being beneficial to the internal circulation of materials and improving the reaction strength.
Furthermore, although not shown, the reaction vessel 1 may be entirely cylindrical or cylindrical except for the bottom, which is also within the scope of the present invention.
The dimensions of the reaction vessel in the vertical direction are exemplified below.
In one embodiment of the present invention, as in FIG. 2A and FIG. 4A show that the total height of the reaction vessel 1 is h, and the height of the cylindrical section is h 1 The height of the cone section is h 2 The height of the arc-shaped section is h 3 And (2) andh＝h 1 +h 2 +h 3 i.e. the starting down-necking position of the lower part of the reaction vessel 1 is 1/3 to 1/2 of the total height of the reaction vessel from the bottom.
In one embodiment of the invention, the reaction vessel has a total height of h and the arcuate segment has a height of h 3 And (2) andthis means that the reaction vessel 1 has a lower part of its middle and a lower part of its structure, which is a variable structure, from the bottom to 1/100 to 1/50 of the total height of the riser.
In one embodiment of the invention, the cone structure upper plane coincides with the cylinder structure lower plane, and in the projection in the up-down direction, the projection of the cone middle lower part is located at the center of the projection of the cylinder upper part. In a further embodiment, the upper plane of the semi-ellipsoidal structure coincides with the lower plane of the conical structure, and in the projection in the up-down direction, the projection of the semi-ellipsoidal bottom is located in the center of the projection of the lower middle of the cone.
In the present invention, the bottom of the reaction vessel 1 may be made free of a plenum or hood by using the above-described inclined downward reactant inlet.
In the invention, the specific surface area of the powdery fuel is larger, the reaction is more sufficient, and the size reduction of the fluidized bed reaction device is facilitated.
In the invention, the powder conveying air flow not only plays a role of fluidizing materials, but also is used as the powder conveying air flow for conveying fuel, thereby simplifying the process flow and improving the operation simplicity of equipment.
In the invention, the symmetrically arranged powder conveying pipelines tangentially enter the semi-ellipsoidal bottom of the reaction area, wherein the generation of dead zones at the bottom of the reaction area can be avoided as much as possible by the symmetrically arranged and tangentially entering carrier fuel gas flow.
In the invention, the fluidization speed in the local area reaches higher flow speed by the reaction area or the middle-lower necking structure of the reaction container, namely, the flow uniformity of materials is enhanced, the local high-temperature area is avoided, and the chemical reaction intensity is improved.
Although not shown, in embodiments of the present invention, the angle formed by the axis of the powder delivery pipe and the horizontal plane can be changed or adjusted; or the axis of the powder conveying pipeline is arranged to form an angle with the vertical section so that the airflow of the reaction material entering the arc-shaped section from the powder conveying pipeline is provided with a rotating direction along the circumferential direction, and further, the angle formed with the vertical section can be adjusted.
As can be appreciated, in the present invention, where not explicitly stated, numerical ranges include the endpoints, and further, in addition to the values already listed, the numerical ranges may be intermediate or 1/3 or 2/3.
The fluidized bed reaction apparatus described above may also be a component of a combustion system, for example, the reaction products formed by the structures shown in fig. 1 and 3 may be injected as fuel into the furnace of a boiler.
Based on the above, the invention provides the following technical scheme:
1. a fluidized bed reaction apparatus comprising:
a reaction vessel comprising a concave arcuate section at a bottom of the reaction vessel, the reaction vessel defining a reaction space for a fluidized reaction to occur;
a reactant outlet provided at the top or upper portion of the reaction vessel; and
a reactant inlet disposed obliquely downward so as to be adapted to provide a reactant gas stream into the arcuate segment in an obliquely downward manner.
2. The fluidized bed reaction apparatus according to 1, wherein:
the reactant inlet is disposed contiguous with the upper edge of the arcuate segment and is inclined downwardly so as to be adapted to provide a reactant gas stream into the arcuate segment in an inclined downwardly manner.
3. The fluidized bed reaction apparatus according to claim 2, wherein:
the axis of the reaction material inlet is parallel to the tangent line of the intrados surface of the arc section at the upper edge.
4. The fluidized bed reaction apparatus according to claim 3, wherein:
the lower edge line of the channel space of the reactant inlet is overlapped with the tangent line of the intrados of the arc section at the upper edge.
5. The fluidized bed reaction apparatus according to 1 or 2, wherein:
the axis of the reactant inlet forms a first angle with the horizontal plane, the first angle being greater than 60 degrees and less than 90 degrees.
6. The fluidized bed reaction apparatus according to 1 or 2, wherein:
the arc-shaped section is an ellipsoidal arc-shaped section or a spherical arc-shaped section.
7. The fluidized bed reaction apparatus according to claim 6, wherein:
the arc-shaped section is of a 1/2 or 1/4 ellipsoidal structure or a 1/2 or 1/4 spherical structure.
8. The fluidized bed reaction apparatus according to any one of claims 1 to 7, wherein:
the reaction vessel comprises a cylindrical section, a conical section and an arc-shaped section which are sequentially connected in the vertical direction, wherein the upper edge of the large diameter of the conical section is connected with the cylindrical section, and the lower edge of the small diameter of the conical section is connected with the arc-shaped section.
9. The fluidized bed reaction apparatus according to 8, wherein:
the upper end of the cone section forms a second angle with the horizontal plane, and the second angle is larger than the first angle; and/or
The total height of the reaction vessel is h, and the height of the cylinder section is h 1 The height of the cone section is h 2 The height of the arc-shaped section is h 3 And (2) andh＝h 1 +h 2 +h 3 。
10. the fluidized bed reaction apparatus according to any one of claims 1 to 7, wherein:
the reaction vessel comprises a cylindrical section and an arc-shaped section which are sequentially connected in the vertical direction, and the top of the cylindrical section defines the top of the reaction vessel; or alternatively
The reaction vessel comprises a conical section and an arc-shaped section which are sequentially connected in the vertical direction, and the top of the conical section defines the top of the reaction vessel.
11. The fluidized bed reaction apparatus according to any one of claims 1 to 10, wherein:
the axis of the reaction vessel passes through the center of the projection of the arc-shaped section in the vertical direction.
12. The fluidized bed reaction apparatus according to any one of claims 1 to 11, wherein:
the total height of the reaction vessel is h, and the height of the arc-shaped section is h 3 And (2) and
13. the fluidized bed reaction apparatus according to any one of claims 1 to 12, wherein:
the fluidized bed reaction device includes a plurality of reactant inlets which are equally spaced in a circumferential direction.
14. The fluidized bed reaction apparatus according to 1 or 2, wherein:
the axis of the reactant inlet and the horizontal plane form a first angle which can be changed and is more than 60 degrees and less than 90 degrees; or alternatively
The axis of the reactant inlet is arranged at an angle to the vertical cross section such that the reactant flow from the reactant inlet into the arcuate section has a rotational direction along the circumferential direction, and further the angle to the vertical cross section is adjustable.
14. The fluidized bed reaction apparatus according to any one of claims 1 to 13, wherein:
the fluidized bed reaction device is a circulating fluidized bed reaction device and further comprises a separator and a return device, the reaction vessel is a riser, the reactant outlet is connected to the separator, and the lower outlet of the separator is communicated with the lower part of the riser through the return device.
15. The fluidized bed reaction apparatus according to claim 14, wherein:
the reaction vessel comprises a cylindrical section, a conical section and an arc section which are sequentially connected in the vertical direction, wherein the upper edge of the large diameter of the conical section is connected with the cylindrical section, and the lower edge of the small diameter of the conical section is connected with the arc section;
the lower outlet of the separator is communicated with the cone section through a material returning device.
16. The fluidized bed reaction apparatus according to any one of claims 1 to 13, wherein:
the fluidized bed reaction device is a bubbling fluidized bed reaction device, the reaction vessel is a combustion chamber, and the reactant outlet is arranged at the top of the combustion chamber.
17. A combustion system, comprising:
the fluidized bed reaction apparatus according to any one of claims 1 to 16.
18. A method of controlling a fluidized bed reaction apparatus according to any one of claims 1 to 16, comprising the steps of:
so that the flow rate of the powdery reactant stream entering the reaction space from the reactant inlet is always higher than 10m/s.
19. The method according to claim 18, wherein:
the fluidized bed reaction device is the fluidized bed reaction device according to 14 or 15, and the method comprises the steps of: so that the upward flow rate of the reactant material gas stream carrying the powdery reactant material in the arc-shaped section is in the range of 0.5-30m/s, and further in the range of 10-20 m/s;
or alternatively
The fluidized bed reaction device is the fluidized bed reaction device according to 16, and the method comprises the steps of: so that the upward flow rate of the reactant stream carrying the powdered reactant in the arcuate segment is in the range of 0.5 to 20m/s, and further in the range of 5 to 15m/s.
Although embodiments of the present invention have been shown and described, it will be understood by those skilled in the art that various changes may be made and equivalents may be made therein without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.

Claims (20)

1. A fluidized bed reaction apparatus comprising:
a reaction vessel comprising a concave arcuate section at a bottom of the reaction vessel, the reaction vessel defining a reaction space for a fluidized reaction to occur;
a reactant outlet provided at the top or upper portion of the reaction vessel; and
a reactant inlet disposed obliquely downward so as to be adapted to provide a reactant gas stream into the arcuate segment in an obliquely downward manner.
2. The fluidized bed reaction apparatus according to claim 1, wherein:
the reactant inlet is disposed contiguous with the upper edge of the arcuate segment and is inclined downwardly so as to be adapted to provide a reactant gas stream into the arcuate segment in an inclined downwardly manner.
3. The fluidized bed reaction apparatus according to claim 2, wherein:
the axis of the reaction material inlet is parallel to the tangent line of the intrados surface of the arc section at the upper edge.
4. A fluidized bed reaction apparatus according to claim 3 wherein:
the lower edge line of the channel space of the reactant inlet is overlapped with the tangent line of the intrados of the arc section at the upper edge.
5. The fluidized bed reaction apparatus according to claim 1 or 2, wherein:
the axis of the reactant inlet forms a first angle with the horizontal plane, the first angle being greater than 60 degrees and less than 90 degrees.
6. The fluidized bed reaction apparatus according to claim 1 or 2, wherein:
the arc-shaped section is an ellipsoidal arc-shaped section or a spherical arc-shaped section.
7. The fluidized bed reaction apparatus according to claim 6, wherein:
the arc-shaped section is of a 1/2 or 1/4 ellipsoidal structure or a 1/2 or 1/4 spherical structure.
8. The fluidized bed reaction apparatus according to any one of claims 1 to 7, wherein:
the reaction vessel comprises a cylindrical section, a conical section and an arc-shaped section which are sequentially connected in the vertical direction, wherein the upper edge of the large diameter of the conical section is connected with the cylindrical section, and the lower edge of the small diameter of the conical section is connected with the arc-shaped section.
9. The fluidized bed reaction apparatus according to claim 8, wherein:
the upper end of the cone section forms a second angle with the horizontal plane, and the second angle is larger than the first angle; and/or
The total height of the reaction vessel is h, and the height of the cylinder section is h 1 The height of the cone section is h 2 The height of the arc-shaped section is h 3 And (2) andh＝h 1 +h 2 +h 3 。
10. the fluidized bed reaction apparatus according to any one of claims 1 to 7, wherein:
the reaction vessel comprises a cylindrical section and an arc-shaped section which are sequentially connected in the vertical direction, and the top of the cylindrical section defines the top of the reaction vessel; or alternatively
The reaction vessel comprises a conical section and an arc-shaped section which are sequentially connected in the vertical direction, and the top of the conical section defines the top of the reaction vessel.
11. The fluidized bed reaction apparatus according to any one of claims 1 to 10, wherein:
the axis of the reaction vessel passes through the center of the projection of the arc-shaped section in the vertical direction.
12. The fluidized bed reaction apparatus according to any one of claims 1 to 11, wherein:
the total height of the reaction vessel is h, and the height of the arc-shaped section is h 3 And (2) and
13. the fluidized bed reaction apparatus according to any one of claims 1 to 12, wherein:
the fluidized bed reaction device includes a plurality of reactant inlets which are equally spaced in a circumferential direction.
14. The fluidized bed reaction apparatus according to claim 1 or 2, wherein:
the axis of the reactant inlet and the horizontal plane form a first angle which can be changed and is more than 60 degrees and less than 90 degrees; or alternatively
The axis of the reactant inlet is arranged at an angle to the vertical cross section such that the reactant flow from the reactant inlet into the arcuate section has a rotational direction along the circumferential direction, and further the angle to the vertical cross section is adjustable.
15. The fluidized bed reaction apparatus according to any one of claims 1 to 13, wherein:
the fluidized bed reaction device is a circulating fluidized bed reaction device and further comprises a separator and a return device, the reaction vessel is a riser, the reactant outlet is connected to the separator, and the lower outlet of the separator is communicated with the lower part of the riser through the return device.
16. The fluidized bed reaction apparatus of claim 15, wherein:
the reaction vessel comprises a cylindrical section, a conical section and an arc section which are sequentially connected in the vertical direction, wherein the upper edge of the large diameter of the conical section is connected with the cylindrical section, and the lower edge of the small diameter of the conical section is connected with the arc section;
the lower outlet of the separator is communicated with the cone section through a material returning device.
17. The fluidized bed reaction apparatus according to any one of claims 1 to 13, wherein:
the fluidized bed reaction device is a bubbling fluidized bed reaction device, the reaction vessel is a combustion chamber, and the reactant outlet is arranged at the top of the combustion chamber.
18. A combustion system, comprising:
the fluidized bed reaction apparatus of any one of claims 1-17.
19. A method of controlling a fluidized bed reaction apparatus according to any one of claims 1 to 17, comprising the steps of:
so that the flow rate of the powdery reactant stream entering the reaction space from the reactant inlet is always higher than 10m/s.
20. The method according to claim 19, wherein:
the fluidized bed reaction device is a fluidized bed reaction device according to claim 15 or 16, and the method comprises the steps of: so that the upward flow rate of the reactant material gas stream carrying the powdery reactant material in the arc-shaped section is in the range of 0.5-30m/s, and further in the range of 10-20 m/s; or alternatively
The fluidized bed reaction device is a fluidized bed reaction device according to claim 17, and the method comprises the steps of: so that the upward flow rate of the reactant stream carrying the powdered reactant in the arcuate segment is in the range of 0.5 to 20m/s, and further in the range of 5 to 15m/s.
CN202210806781.8A 2022-07-08 2022-07-08 Fluidized bed reaction device, control method thereof and combustion system Pending CN117398932A (en)

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Application Number Priority Date Filing Date Title
CN202210806781.8A CN117398932A (en) 2022-07-08 2022-07-08 Fluidized bed reaction device, control method thereof and combustion system

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202210806781.8A CN117398932A (en) 2022-07-08 2022-07-08 Fluidized bed reaction device, control method thereof and combustion system

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CN117398932A true CN117398932A (en) 2024-01-16

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