CN113717756A - Air distribution method and air distribution device - Google Patents

Air distribution method and air distribution device Download PDF

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Publication number
CN113717756A
CN113717756A CN202111046526.XA CN202111046526A CN113717756A CN 113717756 A CN113717756 A CN 113717756A CN 202111046526 A CN202111046526 A CN 202111046526A CN 113717756 A CN113717756 A CN 113717756A
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air
hearth
furnace
port
gasification furnace
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CN113717756B (en
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董鹏飞
张海霞
王东宇
朱治平
湛月平
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Institute of Engineering Thermophysics of CAS
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Institute of Engineering Thermophysics of CAS
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/50—Fuel charging devices
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C10J2300/0936—Coal fines for producing producer gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

One aspect of the present invention provides a wind distribution method, including: determining the estimated average grain diameter of the fuel entering the furnace according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel; determining a first air supply speed, a first air supply oxygen concentration, a second air supply operation frequency and a second air supply operation time according to the calculated average particle size in the furnace; feeding the fuel and the gasifying agent into the hearth of the gasification furnace so that the fuel and the gasifying agent are subjected to gasification reaction in the hearth of the gasification furnace; wherein, the gasification agent includes primary air and impulse wind, sends the gasification agent into gasifier furnace and includes: the primary air is sent into the hearth of the gasification furnace through the primary air port arranged at the bottom of the hearth of the gasification furnace according to the first air supply speed and the first air supply oxygen concentration, and the pulse air is sent into the hearth of the gasification furnace through the pulse air port according to the second air supply operation frequency and the second air supply operation duration through the pulse air port arranged at the bottom of the hearth of the gasification furnace.

Description

Air distribution method and air distribution device
Technical Field
The invention belongs to the technical field of fuel gasification, and particularly relates to an air distribution method and an air distribution device.
Background
Coal gasification is one of core technologies of clean and efficient utilization technologies of coal, and is the basis for developing coal-based chemical products, coal-based clean fuels, industrial gas, poly-generation systems and other coal chemical process industries. The fluidized bed gasification technology has the advantages of strong coal adaptability, full gas-solid mixing, high gasification strength, no tar and phenols in coal gas, no black water and the like, and is widely applied to the fields of industrial gas and synthetic ammonia.
The thermal stability of coal refers to the property that the coal keeps the original particle size in the high-temperature combustion or gasification process, generally, the recommended particle size of the coal as fired of the fluidized bed gasification furnace is 0-6 mm or 0-10 mm, and the coal as fired in the particle size range can meet the good gas-solid flow and reaction state in the fluidized bed gasification furnace. However, the above particle size ranges are mainly used for bituminous coal (belonging to medium-high or high thermal stability) with better thermal stability as the coal as fired, and when lignite and the like with poorer Thermal Stability (TS) are adopted+6Less than or equal to 60 percent) of coal as fired coal, the adoption of the particle size range causes that a stable dense-phase area and material circulation can not be formed in the circulating fluidized bed, and the fly ash has large amount and high carbon content, which deviate from the design range. Therefore, the particle size of the coal as fired is enlarged in the related art, and for example, lump coal of 20-50 mm is used as the coal as fired. From the operation result, the problem of unstable dense-phase region and material circulation of a fluidized bed hearth caused by the coal as fired with poor thermal stability can be solved by increasing the particle size of the coal as fired, but the problems of easy slagging of the hearth, high carbon content of bottom slag and the like are caused at the same time.
Disclosure of Invention
Technical problem to be solved
In view of the above, the present invention provides a wind distribution method and a wind distribution device to at least partially solve the above technical problems.
(II) technical scheme
One aspect of the present invention provides a wind distribution method, including:
determining the estimated average grain diameter of the fuel entering the furnace according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel; the estimated average particle size in the furnace is a weight average particle size within a certain particle size range.
Determining a first air supply speed, a first air supply oxygen concentration, a second air supply operation frequency and a second air supply operation time according to the calculated average particle size in the furnace;
feeding the fuel and the gasifying agent into the hearth of the gasification furnace so that the fuel and the gasifying agent are subjected to gasification reaction in the hearth of the gasification furnace;
wherein, the gasification agent includes primary air and impulse wind, sends the gasification agent into gasifier furnace and includes:
through a primary air port arranged at the bottom of the hearth of the gasification furnace, primary air is fed into the hearth of the gasification furnace through the primary air port according to the first air supply speed and the first air supply oxygen concentration, and
and sending the pulse air into the hearth of the gasification furnace through the pulse air port by the pulse air port arranged at the bottom of the hearth of the gasification furnace according to the second air supply operation frequency and the second air supply operation time.
According to an embodiment of the invention, wherein: the air outlets of the primary air port and the pulse air port are positioned at the same height.
According to an embodiment of the present invention, wherein the gasifying agent further comprises secondary air, and the feeding of the gasifying agent into the hearth of the gasifier further comprises:
sending secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; wherein the feeding port arranged on the gasification furnace hearth is higher than the material returning port arranged on the gasification furnace hearth, and the air outlet of the secondary air port is higher than the material returning port and lower than the feeding port;
the secondary air comprises at least one of: oxygen-enriched air, oxygen, water vapor and CO2；
The apparent furnace-entering wind speed of the secondary wind entering the hearth of the cross section is 3-4 m/s;
the oxygen concentration of the secondary air is 30-70%.
According to an embodiment of the present invention, wherein the gasification agent further includes secondary air and secondary auxiliary air, and the feeding the gasification agent into the hearth of the gasification furnace further includes:
sending secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; and
sending secondary auxiliary air into a hearth of the gasification furnace through a secondary auxiliary air port;
wherein, a return material port is arranged on the gasification furnace hearth, and a feed inlet is arranged on the return material port; the air outlet of the secondary air port is higher than the material returning port, the secondary auxiliary air port and the material returning port are arranged at the same height, and the secondary auxiliary air port is communicated with the hearth of the gasification furnace along the horizontal direction;
the secondary air and the secondary auxiliary air comprise at least one of the following air: oxygen-enriched air, oxygen, water vapor and CO2；
The apparent wind speed of the secondary air introduced into the hearth at the section is 3-4 m/s;
the oxygen concentration of the secondary air is 30-70%;
the furnace entering speed of the secondary auxiliary air is 60-100 m/s;
the oxygen concentration of the secondary auxiliary air is 10-30%.
According to an embodiment of the present invention, wherein determining the first supply air velocity and the first supply air oxygen concentration based on the estimated average particle size in furnace includes:
under the condition that the estimated average grain size range in furnace charging is 1.25 mm-3 mm, the first air supply speed is 30 m/s-45 m/s, and the first air supply oxygen concentration is 20% -50%;
under the condition that the estimated average grain size range in furnace charging is 3-10 mm, the first air supply speed is 40-50 m/s, and the first air supply oxygen concentration is 20-40%;
under the condition that the estimated average grain size range of the furnace is 10 mm-20 mm, the first air supply speed is 50 m/s-100 m/s, and the first air supply oxygen concentration is 20% -35%.
According to an embodiment of the present invention, wherein determining the second blast operation frequency and the second blast operation time period based on the estimated furnace charge particle size includes:
under the condition that the estimated average grain size range of the air in the furnace is 1.25-3 mm, the second air supply operation frequency is 24 hours for 1 time, and the second air supply operation time is 15-30 s;
under the condition that the estimated average grain size range of the air in the furnace is 3-10 mm, the second air supply operation frequency is 12 hours for 1 time, and the second air supply operation time length is 15-30 s;
and under the condition that the estimated average grain size in the furnace entering range is 10-20 mm, the second air supply operation frequency is 2 hours for 1 time, and the second air supply operation time length is 15-30 s.
The invention also provides an air distribution device for realizing the air distribution method, which comprises a primary air port and a pulse air port.
The primary air port is arranged at the bottom of the hearth of the gasification furnace and used for feeding primary air into the hearth of the gasification furnace according to the first air feeding speed and the first air feeding oxygen concentration; and the pulse air port is arranged at the bottom of the hearth of the gasification furnace and used for feeding pulse air into the hearth of the gasification furnace according to the second air supply operation frequency and the second air supply operation time length.
The first air supply speed, the first air supply oxygen concentration, the second air supply operation frequency and the second air supply operation time length are determined according to the estimated average particle size of the fed fuel, wherein the estimated average particle size of the fed fuel is determined according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel.
According to an embodiment of the present invention, the apparatus further includes: the secondary air port is used for sending secondary air into a hearth of the gasification furnace; wherein gasifier furnace is equipped with feed inlet and returning charge mouth, and the feed inlet is higher than the returning charge mouth, and the air outlet of secondary air port is higher than the returning charge mouth and is less than the feed inlet.
According to the embodiment of the invention, the device further comprises a secondary air port and a secondary auxiliary air port.
Wherein, the secondary air port is used for sending secondary air into a hearth of the gasification furnace;
the secondary auxiliary air port is used for sending secondary auxiliary air into a hearth of the gasification furnace;
wherein, a return material port is arranged on the gasification furnace hearth, and a feed inlet is arranged on the return material port; the air outlet of the secondary air port is higher than the material returning port, the secondary auxiliary air port and the material returning port are arranged at the same height, and the secondary auxiliary air port is communicated with the hearth of the gasification furnace along the horizontal direction.
According to an embodiment of the invention, wherein:
the primary air port comprises a plurality of air distribution units which are distributed at the bottom of the hearth of the gasification furnace in a circular array; the air distribution unit comprises a primary air pipe positioned in the center of the air distribution unit and a plurality of air caps surrounding the primary air pipe, and the primary air pipe is communicated with the air caps; the primary air enters the hearth of the gasification furnace through the air outlet of the blast cap, and the air outlet of the blast cap is positioned on the side wall of the blast cap;
the pulse tuyere is horizontally intersected and connected with a hearth of the gasification furnace;
the air outlet of the blast cap and the air outlet of the pulse air port are positioned at the same height.
(III) advantageous effects
The air distribution method provided by the embodiment of the invention establishes the relationship between the thermal stability of the fuel and the calculated average particle size of the fed fuel, further forms a fluidized bed air distribution operation regulation and control method suitable for the situation that different thermal stability fuels are used as the fed fuel, and solves the problems of unstable circulation of a dense-phase region and materials of a hearth, large fly ash amount, high carbon content of fly ash or slag formation at the bottom of the hearth, high carbon content of bottom slag and the like existing when the thermal stability difference between the running coal type and the designed coal type of the conventional fluidized bed gasification furnace is large.
According to the air distribution method provided by the embodiment of the invention, classified air distribution is adopted for different coal with thermal stability, different air supply operation parameters are respectively set for primary air and pulse air according to different grade ranges of the average particle size calculated by entering the furnace, and different differential operation modes with different intensities, impact crushing areas, temperature distribution and different axial directions of the furnace chamber are formed, so that the particle crushing of the coal with different thermal stability in the furnace chamber is matched with gas-solid flow and gasification reaction, and the stable dense-phase area and material circulation of the coal with different thermal stability in the gasification process are realized.
Drawings
Fig. 1 is a schematic structural diagram of a wind distribution device for implementing a wind distribution method according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of a gasification apparatus including an air distribution device according to an embodiment of the present invention;
fig. 3 schematically shows a structural schematic view of a wind distribution device of another embodiment of the invention;
FIG. 4 schematically shows a distribution diagram of an air distribution unit at the bottom of a gasifier hearth according to an embodiment of the invention;
fig. 5 schematically shows a top view of a wind distribution unit according to an embodiment of the invention;
fig. 6 schematically shows a distribution diagram of an air distribution unit at the bottom of a gasifier hearth according to another embodiment of the present invention.
Description of reference numerals:
1. a hearth of the gasification furnace;
2. a gas-solid separator;
3. a material returning device;
11. a primary tuyere;
110. a wind distribution unit;
111. a primary air duct;
112. a hood;
12. a slag discharge port;
13. returning the material port;
14. a secondary tuyere;
141. a secondary auxiliary tuyere;
15. a feed port;
16. a pulse tuyere;
17. the side wall of the hearth;
a1, primary air;
a2, secondary air;
a3, pulse wind;
a4, secondary auxiliary wind;
m, fuel.
Detailed Description
In order that the objects, technical solutions and advantages of the present invention will become more apparent, the present invention will be further described in detail with reference to the accompanying drawings in conjunction with the following specific embodiments.
Hereinafter, embodiments of the present disclosure will be described with reference to the accompanying drawings. It should be understood that the description is illustrative only and is not intended to limit the scope of the present disclosure. In the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the disclosure. It may be evident, however, that one or more embodiments may be practiced without these specific details. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present disclosure.
The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of the disclosure. The terms "comprises," "comprising," and the like, as used herein, specify the presence of stated features, steps, operations, and/or components, but do not preclude the presence or addition of one or more other features, steps, operations, or components.
All terms (including technical and scientific terms) used herein have the same meaning as commonly understood by one of ordinary skill in the art unless otherwise defined. It is noted that the terms used herein should be interpreted as having a meaning that is consistent with the context of this specification and should not be interpreted in an idealized or overly formal sense.
Where a convention analogous to "at least one of A, B and C, etc." is used, in general such a construction is intended in the sense one having skill in the art would understand the convention (e.g., "a system having at least one of A, B and C" would include but not be limited to systems that have a alone, B alone, C alone, a and B together, a and C together, B and C together, and/or A, B, C together, etc.). Where a convention analogous to "A, B or at least one of C, etc." is used, in general such a construction is intended in the sense one having skill in the art would understand the convention (e.g., "a system having at least one of A, B or C" would include but not be limited to systems that have a alone, B alone, C alone, a and B together, a and C together, B and C together, and/or A, B, C together, etc.).
The thermal stability of coal refers to the property that coal keeps the original granularity in the high-temperature combustion or gasification process, and according to the thermal stability index of coal, the coal can be divided into four types according to the standard MT/T560-2008: TS +6 is less than or equal to 60 percent, and the thermal stability is low; the heat stability is more than 60 percent and less than or equal to 70 percent of TS + 6; TS +6 is more than 70% and less than or equal to 80, and the medium-high thermal stability is obtained; TS +6 > 80% is highly heat stable.
In the process of implementing the invention, the conventional fluidized bed gasification furnace is generally designed by taking coal with a certain specific thermal stability range as design coal, when the thermal stability of the coal as fired is greatly changed, the problems of unstable dense-phase region and material circulation of a hearth, large fly ash amount, high fly ash carbon content, slag bonding at the bottom of the hearth, high bottom slag carbon content and the like are easy to occur.
The above problems are present when the conventional fluidized bed gasification furnace is used for treating coal with different thermal stability, and the main reason is that the crushing process of the coal is not matched with the combustion gasification reaction and gas-solid flow of the coal in the fluidized bed. The coal with poor thermal stability adopts a conventional particle size range, and the coal crushing speed is higher than the combustion and gasification reaction speed, so that the coal as fired is quickly crushed into fly ash, the cyclone separator cannot capture a large amount of fly ash and then returns to a hearth through a material returning device to construct material circulation, the fly ash amount is large, the carbon content of the fly ash is high, and the hearth cannot establish a stable dense-phase region.
If coarse-grain coal is adopted, the crushing speed of the whole coal as fired is matched with the combustion gasification reaction and gas-solid flow in the circulating fluidized bed, a relatively stable dense-phase region and material circulation can be established, but the coarse grains are easy to settle, an air distribution device of the conventional fluidized bed gasification furnace cannot rapidly crush or fluidize the coarse grains, local over-temperature slagging is caused, the settled coarse grains are discharged out of the system after the reaction is finished, and the carbon content of bottom slag is high.
In view of the above, the invention provides an air distribution method, which is used for designing a targeted air supply scheme according to the thermal stability difference of different coal types, and solving the problems of unstable material circulation and fly ash circulation, large fly ash amount, high fly ash carbon content, slag bonding at the bottom of a hearth, high bottom slag carbon content and the like in a dense-phase region of the hearth.
The air distribution method comprises the following steps:
determining the estimated average grain diameter of the fuel entering the furnace according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel;
determining a first air supply speed, a first air supply oxygen concentration, a second air supply operation frequency and a second air supply operation time according to the calculated average particle size in the furnace; and feeding the fuel and the gasifying agent into the hearth of the gasification furnace so that the fuel and the gasifying agent are subjected to gasification reaction in the hearth of the gasification furnace.
Wherein, the gasification agent includes primary air and impulse wind, sends the gasification agent into gasifier furnace and includes: the primary air is sent into the hearth of the gasification furnace through the primary air port arranged at the bottom of the hearth of the gasification furnace according to the first air supply speed and the first air supply oxygen concentration, and the pulse air is sent into the hearth of the gasification furnace through the pulse air port according to the second air supply operation frequency and the second air supply operation duration through the pulse air port arranged at the bottom of the hearth of the gasification furnace. The first air supply speed is the air outlet speed of the primary air port, and the structure of the primary air port is determined according to the structural form of the air distribution device adopted by the gasification furnace. For example, the primary air outlet may include a plurality of air distribution units, each of which may include a plurality of hoods, and the first supply air speed is the air speed at the air outlet of the hood.
According to the embodiment of the invention, the estimated average grain diameter of the furnace is the grain diameter parameter according to which the air supply parameter is determined, and corresponds to the average grain diameter of the actual furnace coal grain diameter range, and the estimated average grain diameter of the furnace is increased along with the increase of the actual furnace grain diameter of the fuel according to the experimental result. The determination of the parameters comprehensively considers the influence of factors such as the thermal stability of the fuel, the crushing rate of the fuel, the carbon dioxide reduction rate of the fuel and the like on the air supply parameters.
According to an embodiment of the present invention, in the above method, the determined estimated mean particle diameter of the fuel entering the furnace according to the thermal stability index of the fuel, the crushing rate of the fuel, and the carbon dioxide reduction rate of the fuel may be expressed as the following formula (one) and formula (two):
Y＝X-Aformula (I)
Figure BDA0003250226570000081
Wherein, the fuel is coal fuel, Y is the average grain diameter (mm) of coal as fired; x is the thermal stability index TS +6 value of the coal as fired; a is an influence factor which is influenced by the breaking velocity upsilon of the coal as fired in the fluidized bed and the carbon dioxide reduction rate alpha of the coal as firedCO2The influence factor decreases with increasing fragmentation rate and increases with increasing carbon dioxide reactivity. The constant b can be obtained by performing data fitting on test data of coal gasification reaction of different coal types, and the value range of the constant b can be 0.15-1.25. As can be seen from the formulas (I) and (II), the coal with poorer thermal stability has larger estimated average particle size of the coal as fired.
According to the embodiment of the invention, the thermal stability index of the coal as fired is determined by the following method (according to the national standard GB/T1573-2001): measuring a coal sample with the particle size of 6-13 mm, insulating air in a muffle furnace at the temperature of (850 +/-15) DEG C, heating for 30min, weighing, screening, and taking the percentage of the residual coke mass with the particle size of more than 6mm to the sum of the residual coke masses at all levels as a thermal stability index TS + 6.
According to the embodiment of the invention, the method for measuring the crushing rate of the coal as fired in the fluidized bed comprises the following steps: measuring a coal sample with the particle size of 6-13 mm, and introducing CO into a fluidized bed at the temperature of (950 +/-15) ° C2Gasifying for 30min, with the apparent wind speed of the fluidized bed being 1.5m/s, taking out the gasified coke sample, weighing, sieving, and taking the percentage of the mass of the coke sample with the granularity less than 6mm in the sum of the mass of each coke sample as the crushing amount. The crushing rate is obtained by dividing the crushing amount by the gasification time.
According to the embodiment of the invention, the carbon dioxide reduction rate measurement method is obtained by measuring the value of 950 ℃ according to GB/T220-2018.
According to the embodiment of the invention, the average grain diameter calculated in the furnace is the grain diameter parameter according to which the air supply parameter is determined, the determination of the parameter comprehensively considers the influence of factors such as the thermal stability of the fuel, the crushing rate of the fuel, the carbon dioxide reduction rate of the fuel and the like on the air supply parameter, and air is supplied under the air supply parameter condition established by the method according to the difference of the fuel characteristics, so that the crushing process of the fuel can be ensured to be matched with the combustion gasification reaction and the gas-solid flow in the fluidized bed, and the problems of large fly ash content and high fly ash carbon content are avoided; the air is supplied under the condition of the air supply parameters established by the method, so that combustion products with larger particles can be quickly crushed or fluidized, and local overtemperature slagging is avoided.
According to the embodiment of the invention, the pulse wind and the primary wind are arranged simultaneously, the pulse wind is used as the supplement of the primary wind to disturb the bottom-sinking coarse particles at the position where the primary wind is not fluidized sufficiently, and further prevent the coarse particles from being oxidized to form a local high-temperature area to form slag bonding.
According to the embodiment of the present invention, in the above operation, the first supply air speed, the first supply air oxygen concentration, and the second supply operation frequency and the second supply operation time period of the pulsating air of the primary air are determined according to the estimated average particle diameter of the furnace entering, and specifically, may be:
firstly, classifying the fuel entering the furnace into three grades of 1.25-3 mm, 3-10 mm and 10-20 mm according to the obtained estimated average particle size data of the fuel entering the furnace, and secondly, respectively determining air supply parameters in each grade range.
According to an embodiment of the present invention, specifically, determining the first supply air speed and the first supply air oxygen concentration based on the estimated average particle size in the furnace includes:
under the condition that the estimated average grain size range in furnace charging is 1.25 mm-3 mm, the first air supply speed is 30 m/s-45 m/s, and the first air supply oxygen concentration is 20% -50%;
under the condition that the estimated average grain size range in furnace charging is 3-10 mm, the first air supply speed is 40-50 m/s, and the first air supply oxygen concentration is 20-40%;
under the condition that the estimated average grain size range of the furnace is 10 mm-20 mm, the first air supply speed is 50 m/s-100 m/s, and the first air supply oxygen concentration is 20% -35%.
According to the embodiment of the invention, the primary air can be air, oxygen-enriched air, oxygen and water vapor, CO2The ratio of the primary air to the total amount of the gasification agent can be in the range of 50-100%.
According to an embodiment of the present invention, specifically, determining the second blast operation frequency and the second blast operation time period of the pulse wind based on the estimated average particle diameter at the furnace entrance includes:
under the condition that the estimated average grain size range of the air in the furnace is 1.25-3 mm, the second air supply operation frequency is 24 hours for 1 time, and the second air supply operation time is 15-30 s;
under the condition that the estimated average grain size range of the air in the furnace is 3-10 mm, the second air supply operation frequency is 12 hours for 1 time, and the second air supply operation time length is 15-30 s;
and under the condition that the estimated average grain size in the furnace entering range is 10-20 mm, the second air supply operation frequency is 2 hours for 1 time, and the second air supply operation time length is 15-30 s.
According to the embodiment of the invention, when the fluidized bed gasification furnace enters the gasification operation working condition and slag is not stably discharged, the operation frequency of the pulse wind can be improved by 1-3 times. The pulse wind source can be nitrogen, water vapor and CO2Or a mixture of the three.
According to the embodiment of the invention, different primary air supply wind speeds are determined according to the estimated average particle size of the fed furnace, and the wind speed can meet the impact capability of the primary air on particles with different particle sizes along with the increase of the estimated average particle size of the fed furnace, so that the bottom of a hearth forms a plurality of impact crushing areas to quickly crush coarse particles with uneven bottom sinking and fluidization, and simultaneously, the mass transfer, heat transfer and reaction between the coarse particles and a gasifying agent are strengthened, and local over-temperature slagging is avoided. The air supply oxygen concentration corresponding to different particle size ranges is determined according to the estimated average particle size in the furnace, and the air supply oxygen concentration is too high and easy to slag for the fuel with larger particles, so that the air supply oxygen concentration is reduced along with the increase of the estimated average particle size in the furnace, and the local over-temperature slag can be avoided.
According to the embodiment of the invention, the air outlet directions of the pulse air and the primary air are mutually staggered on the horizontal plane projection, the pulse air is used as the supplement of the primary air, and the pulse air mainly and regularly disturbs the bottom-sinking coarse particles at the position where the primary air is insufficiently fluidized, so that the coarse particles are further prevented from being oxidized to form a local high-temperature area and slag bonding.
Therefore, the air distribution method provided by the embodiment of the invention establishes the relationship between the thermal stability of the fuel and the calculated average particle size of the fed fuel, further forms a fluidized bed air distribution operation regulation and control method suitable for the situation that different thermal stability fuels are used as the fed fuel, and solves the problems of unstable hearth dense-phase region and material circulation, large fly ash amount, high fly ash carbon content, slag formation at the bottom of a hearth, high bottom slag carbon content and the like existing when the thermal stability difference between the running coal type and the designed coal type of the conventional fluidized bed gasification furnace is large.
According to the air distribution method provided by the embodiment of the invention, classified air distribution is adopted for different coal with thermal stability, different air supply operation parameters are respectively set for primary air and pulse air according to different grade ranges of the grain diameter calculated by entering the furnace, and different differential operation modes with different intensities, impact crushing areas, temperature distribution and different axial directions of the furnace chamber are formed, so that the grain crushing of the coal with different thermal stability in the furnace chamber is matched with gas-solid flow and gasification reaction, and stable dense-phase areas and material circulation are formed in the gasification process of the coal with different thermal stability.
According to the embodiment of the invention, the following steps can be set: the air outlets of the primary air port and the pulse air port are positioned at the same height with the slag discharging port of the hearth of the gasification furnace, and the air outlets of the primary air port and the pulse air port can be arranged near the slag discharging port due to the fact that the quantity of granular fuels with larger grain diameters near the slag discharging port is larger. More preferably, the outlet directions of the pulse wind and the primary wind are staggered with each other on the horizontal plane projection, the pulse wind is used as the supplement of the primary wind, and mainly and regularly disturbs the bottom-sinking coarse particles at the position where the primary wind is insufficiently fluidized, so that the coarse particles are further prevented from being oxidized to form a local high-temperature region and being slagging.
According to an embodiment of the present invention, wherein the gasifying agent further comprises secondary air, and the feeding of the gasifying agent into the hearth of the gasifier further comprises: sending secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; wherein the feed inlet of setting at gasifier furnace is higher than the returning charge mouth of setting at gasifier furnace, and the air outlet of secondary tuyere is higher than the returning charge mouth and is less than the feed inlet.
The secondary air comprises at least one of: oxygen-enriched air, oxygen and water vapor, CO 2; the apparent wind speed of the secondary air introduced into the hearth at the section is 3-4 m/s, and the wind speed range at the bottom of the hearth can be controlled to be 3-8 m/s; the oxygen concentration of the secondary air is 30-70%.
According to another embodiment of the present invention, wherein the gasifying agent further comprises secondary air and secondary auxiliary air, and the feeding the gasifying agent into the hearth of the gasification furnace further comprises: sending secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; and sending the secondary auxiliary air into the hearth of the gasification furnace through the secondary auxiliary air port.
Wherein, a return material port is arranged on the gasification furnace hearth, and a feed inlet is arranged on the return material port; the air outlet of the secondary air port is higher than the material returning port, the secondary auxiliary air port and the material returning port are arranged at the same height, and the secondary auxiliary air port is communicated with the hearth of the gasification furnace along the horizontal direction.
The secondary air and the secondary auxiliary air comprise at least one of the following air: oxygen-enriched air, oxygen, water vapor and CO2(ii) a The apparent wind speed of the secondary air introduced into the hearth at the section is 3-4 m/s; the oxygen concentration of the secondary air is 30-70%; the furnace entering speed of the secondary auxiliary air is 60-100 m/s; the oxygen concentration of the secondary auxiliary air is 10-30%.
According to the embodiment of the invention, the secondary air and the secondary auxiliary air are additionally arranged, the fed raw materials entering the furnace can be quickly dispersed in the circulating materials, the heating rate is high, the pyrolysis and crushing rate is high, the secondary auxiliary air port and the material returning port are arranged at the same height, the raw materials entering the furnace are entrained by the secondary auxiliary air and are horizontally blown into the hearth, and coarse particles can be quickly dispersed in the dilute-dense phase transition region, so that a large number of coarse particles are prevented from sinking into the bottom of the hearth under the action of inertia force, and the risk of slag bonding of the coarse particles at the bottom of the hearth is further avoided.
Another aspect of the present invention provides a wind distribution device for implementing the wind distribution method.
Fig. 1 schematically shows a structural diagram of a wind distribution device for implementing a wind distribution method according to an embodiment of the present invention. The device according to the embodiment of the present invention can be understood by referring to fig. 1, and meanwhile, the position relationship of each stage of the wind distribution structure can be more intuitively embodied due to the structure of the device, so that the position relationship of each stage of the wind supply in the wind distribution method according to the embodiment of the present invention can be further understood by referring to fig. 1.
As shown in fig. 1, the air distribution device includes a primary air port 11 and a pulse air port 16.
The primary air port 11 is arranged at the bottom of the gasifier hearth 1 and used for sending primary air A1 into the gasifier hearth 1 according to the first air supply speed and the first air supply oxygen concentration; and the pulse air port 16 is arranged at the bottom of the gasification furnace hearth 1 and used for sending pulse air A3 into the gasification furnace hearth 1 according to the second air supply operation frequency and the second air supply operation time length.
The first air supply speed, the first air supply oxygen concentration, the second air supply operation frequency and the second air supply operation time length are determined according to the estimated average particle size of the fed fuel, wherein the estimated average particle size of the fed fuel is determined according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel.
The above-mentioned device still includes: and the secondary air port 14 is used for sending secondary air A2 into the hearth 1 of the gasification furnace.
Fig. 2 schematically shows a structural schematic diagram of a gasification device including the air distribution device according to the above-described embodiment of the present invention. As shown in fig. 2, the gasification apparatus includes a gasification furnace hearth 1, a gas-solid separator 2, and a material returning device 3.
The gasification furnace hearth 1 is a variable cross-section hearth, the bottom of the hearth is a cone structure with a small lower part and a big upper part, and the cone angle d is 10-40 degrees. The air distribution device is positioned at the bottom of the hearth 1 of the gasification furnace and is arranged in three stages along the axial direction, and comprises primary air A1, pulse air A3 and secondary air A2.
Wherein gasifier furnace 1 is equipped with feed inlet 15, row cinder notch 12 and returning charge mouth 13, and feed inlet 15 is higher than returning charge mouth 13, and the air outlet of secondary air port 14 is higher than returning charge mouth 13 and is less than feed inlet 15.
The pulse tuyere 16 is horizontally intersected and connected with the hearth 1 of the gasification furnace; the air outlet of the primary tuyere 11 and the air outlet of the pulse tuyere 16 are positioned at the same height as the slag discharge port 12 of the gasifier hearth 1.
The fuel M is fed from the feeding port 15, the gasifying agent is respectively fed from the primary tuyere 11, the pulse tuyere 16 and the secondary tuyere 14, after the fuel and the gasifying agent are subjected to gasification reaction in the hearth, the mixture of the coal gas G and the fly ash AS is discharged through the gas-solid separator 2, and large-particle ash and slag separated by the gas-solid separator 2 returns to the hearth 1 of the gasification furnace through the material returning device 3 to continue the reaction.
As can be seen from fig. 1 and 2, in the air distribution device according to this embodiment, the primary air port 11 and the pulse air port 16 are disposed at the same height, and are both disposed in the dense phase region near the slag discharge port, and the pulse air and the primary air are staggered with each other in the horizontal plane projection. The pulse wind is used as the supplement of the primary wind, the bottom-sinking coarse particles at the position where the primary wind fluidization is insufficient are disturbed regularly, and the coarse particles are further prevented from being oxidized to form a local high-temperature area and being slagging.
The air outlet of the secondary air port 14 is higher than the material returning port 13 and lower than the feeding port 15, and is arranged in the transition region between the dense-phase region and the dilute-phase region of the fluidized bed, and the secondary air port 14 is formed by uniformly distributing air pipes. Through addding the overgrate air, the income stove raw materials of feeding can the fast dispersion in circulating material, and rate of heating is high, and pyrolysis and broken speed are fast, and coarse grain can the fast dispersion in rare dense phase transition region, has consequently avoided a large amount of coarse grains to receive inertial force to sink into the furnace bottom, has further avoided the risk of coarse grain slagging scorification in the furnace bottom.
Fig. 3 schematically shows a structural diagram of a wind distribution device according to another embodiment of the present invention.
The air distribution device in the embodiment is different from the air distribution device shown in fig. 1 in that:
when the target products of the coal gas generated by the gasification of the fluidized bed are CO and H2Meanwhile, the device also comprises a secondary auxiliary air port 141 used for sending secondary auxiliary air A4 into the hearth of the gasification furnace; wherein, the gasification furnace hearth 1 is provided with a material returning port 13, the material returning port 13 is intersected with the gasification furnace hearth 1 in the horizontal direction, and the material returning port 13 is provided with a material feeding port 15; the air outlet of the secondary air port 14 is higher than the material returning port 13, the secondary auxiliary air port 141 and the material returning port 13 are arranged at the same height, and the secondary auxiliary air port 141 is arranged along the horizontal directionAnd is communicated with the hearth 1 of the gasification furnace, and a single air pipe can be arranged at the bottom of the horizontal pipe of the material returning opening 13 to be used as a secondary auxiliary air port 141.
By adopting the structure, the fed furnace-entering raw materials can be quickly dispersed in the circulating materials, the heating rate is high, the pyrolysis and crushing rate is high, the raw materials enter the hearth through horizontal gas entrainment, and the coarse particles can be quickly dispersed on the interface of a dilute dense phase region, so that the phenomenon that a large amount of coarse particles sink into the bottom of the hearth under the action of inertia force is avoided, and the risk of slag bonding of the coarse particles at the bottom of the hearth is further avoided.
According to an embodiment of the invention, wherein: the primary air port comprises a plurality of air distribution units which are distributed at the bottom of the hearth of the gasification furnace in a circular array. Fig. 4 schematically shows a distribution diagram of the air distribution unit at the bottom of the gasifier hearth according to an embodiment of the invention. As shown in fig. 4, the air distribution units 110 are arranged in a radial star-shaped centrosymmetric arrangement at the bottom of the furnace (the area inside the furnace side wall 17).
Fig. 5 schematically shows a top view structural diagram of a wind distribution unit according to an embodiment of the invention.
As shown in fig. 5, the air distribution unit 110 includes a primary air pipe 111 located at the center of the air distribution unit 110, and a plurality of hoods 112 surrounding the primary air pipe, and the primary air pipe 111 is communicated with the hoods 112; for example, the wind distribution unit 110 shown in fig. 5 may include 3 wind caps 112, and the wind caps 112 are arranged in a triangle in the wind distribution unit 110. The primary air enters the hearth of the gasification furnace through the air outlet of the blast cap 112, and the air outlet of the blast cap 112 is positioned on the side wall of the blast cap 112, so that air is discharged in the horizontal direction.
According to an embodiment of the present invention, the secondary tuyere may be constituted by a uniformly arranged blast pipe. The pulse tuyere can be composed of a plurality of fine air pipes which are arranged in a branch shape at the tail end of the main air pipe by the main air pipe, wherein the fine air pipes are communicated with a hearth of the gasification furnace.
According to the embodiment of the invention, further, the air outlet of the blast cap 112 and the air outlet of the pulse tuyere are positioned at the same height as the slag discharge port of the hearth of the gasification furnace. Because the quantity of the granular fuel with larger grain diameter near the slag discharging port is larger, the air outlets of the primary air port and the pulse air port can be arranged near the slag discharging port. The pulse air which is formed by a plurality of branch-shaped fine air pipes and can be provided with the pulse air port is mutually staggered with the outlet air of the primary air blown out by the air cap of the primary air port on the horizontal plane projection, the pulse air is used as the supplement of the primary air to regularly disturb the bottom-sinking coarse particles at the position where the primary air fluidization is insufficient, and the coarse particles are further prevented from being oxidized to form a local high-temperature area and slagging.
Through optimizing furnace bottom air distribution structure, form a series of broken regions of impact and even air distribution field in furnace bottom, can quick breakage and the fluidization with the coarse granule of sinking the end, set up the periodic disturbance of coarse granule in this region at the regional pulse wind that the air distribution unit can not fully fluidize. The broken area formed by the air distribution unit and the periodic disturbance formed by the pulse air avoid the slag bonding of the bottom-sinking coarse particles, and improve the stable operation period of the fluidized bed gasification device. The differential bed fluidization state formed by combining grading air distribution with a cone structure at the bottom of the hearth strengthens the internal circulation of the dense-phase zone, the stability of the dense-phase zone and the stability of the particle size distribution. By adopting the air distribution device, the fluidized bed can adapt to lignite with poor thermal stability and adopts coarse grain size as coal as fired, so that the screening and crushing of the fired raw materials can be simplified, and the energy consumption of coal preparation is reduced.
Fig. 6 schematically shows a distribution diagram of an air distribution unit at the bottom of a gasifier hearth according to another embodiment of the present invention.
As shown in fig. 6, the air distribution unit is different from the air distribution unit shown in fig. 4 in that a single hood 112 is adopted at the center of the primary air port air distribution structure at the bottom of the furnace to replace a group of air distribution units 110, and this layout is suitable for the situation that the sectional area of the bottom of the furnace is relatively small, so that the air distribution is more symmetrical and uniform.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. A method of distributing wind, comprising:
determining the estimated average grain diameter of the fuel entering a furnace according to the thermal stability index of the fuel, the crushing rate of the fuel and the carbon dioxide reduction rate of the fuel;
determining a first air supply speed, a first air supply oxygen concentration, a second air supply operation frequency and a second air supply operation time according to the calculated average grain diameter in the furnace;
sending a gasifying agent into a hearth of a gasification furnace so that the fuel and the gasifying agent are subjected to gasification reaction in the hearth of the gasification furnace;
wherein, the gasification agent includes primary air and impulse air, send the gasification agent into gasifier furnace includes:
sending the primary air into the hearth of the gasification furnace through a primary air port arranged at the bottom of the hearth of the gasification furnace and according to the first air supply speed and the first air supply oxygen concentration, and
and sending the pulse air into the hearth of the gasification furnace through a pulse air port arranged at the bottom of the hearth of the gasification furnace according to the second air supply operation frequency and the second air supply operation time length by passing the pulse air port.
2. The wind distribution method of claim 1, wherein:
and the air outlets of the primary air port and the pulse air port are positioned at the same height.
3. The air distribution method of claim 1, wherein the gasifying agent further comprises secondary air, and the feeding the gasifying agent into the gasifier hearth further comprises:
sending the secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; the air outlet of the secondary air port is higher than the return port and lower than the feeding port;
the apparent wind speed of the secondary air introduced into the hearth at the section is 3-4 m/s;
the oxygen concentration of the secondary air is 30-70%.
4. The air distribution method of claim 1, wherein the gasification agent further comprises secondary air and secondary auxiliary air, and the feeding the gasification agent into the gasifier hearth further comprises:
sending the secondary air into the hearth of the gasification furnace through a secondary air port arranged in the hearth of the gasification furnace; and
sending the secondary auxiliary air into the hearth of the gasification furnace through a secondary auxiliary air port;
the gasifier hearth is provided with a material return port, and the material return port is provided with a material feeding port; the air outlet of the secondary air port is higher than the return port, the secondary auxiliary air port and the return port are arranged at the same height, and the secondary auxiliary air port is communicated with the hearth of the gasification furnace along the horizontal direction;
the apparent wind speed of the secondary air introduced into the hearth at the section is 3-4 m/s;
the oxygen concentration of the secondary air is 30-70%;
the furnace inlet speed of the secondary auxiliary air is 60-10 Om/s;
the oxygen concentration of the secondary auxiliary air is 10-30%.
5. The method of claim 1, wherein determining a first supply air velocity and a first supply air oxygen concentration based on the estimated average particle size for furnace entry comprises:
under the condition that the estimated average grain size range of the furnace entering is 1.25 mm-3 mm, the first air supply speed is 30 m/s-45 m/s, and the first air supply oxygen concentration is 20% -50%;
under the condition that the estimated average grain size range of the furnace entering is 3-10 mm, the first air supply speed is 40-50 m/s, and the first air supply oxygen concentration is 20-40%;
when the estimated average grain size range of the furnace inlet is 10-20 mm, the first air supply speed is 50-100 m/s, and the first air supply oxygen concentration is 20-35%.
6. The air distribution method of claim 1, wherein determining a second supply air operating frequency and a second supply air operating duration based on the estimated furnace entry average particle size comprises:
under the condition that the estimated average grain size range of the furnace entering is 1.25-3 mm, the second air supply operation frequency is 24 hours for 1 time, and the second air supply operation time length is 15-30 s;
under the condition that the estimated average grain size range of the furnace entering is 3-10 mm, the second air supply operation frequency is 12 hours for 1 time, and the second air supply operation time is 15-30 s;
and under the condition that the estimated average grain size range of the furnace entering is 10-20 mm, the second air supply operation frequency is 2 hours for 1 time, and the second air supply operation time is 15-30 s.
7. A wind distribution device for implementing the wind distribution method of any one of claims 1 to 6, comprising:
the primary air port is arranged at the bottom of the hearth of the gasification furnace and used for feeding primary air into the hearth of the gasification furnace according to the first air feeding speed and the first air feeding oxygen concentration;
the pulse air port is arranged at the bottom of the gasification furnace hearth and used for sending pulse air into the gasification furnace hearth according to a second air supply operation frequency and a second air supply operation time length;
and determining the first air supply speed, the first air supply oxygen concentration, the second air supply operation frequency and the second air supply operation time length according to a furnace entering estimated average particle size, wherein the furnace entering estimated average particle size is determined according to a fuel thermal stability index, a fuel crushing rate and a fuel carbon dioxide reduction rate.
8. The wind distribution device of claim 7, further comprising:
the secondary air port is used for sending secondary air into the hearth of the gasification furnace; the gasifier furnace is provided with a feed inlet and a return port, the feed inlet is higher than the return port, and the air outlet of the secondary air port is higher than the return port and lower than the feed inlet.
9. The wind distribution device of claim 7, further comprising:
the secondary air port is used for sending secondary air into the hearth of the gasification furnace;
the secondary auxiliary air port is used for sending secondary auxiliary air into the hearth of the gasification furnace;
the gasifier hearth is provided with a material return port, and the material return port is provided with a material feeding port; the air outlet of the secondary air port is higher than the material return port, the secondary auxiliary air port and the material return port are arranged at the same height, and the secondary auxiliary air port is communicated with the hearth of the gasification furnace along the horizontal direction.
10. The wind distribution device of claim 7, wherein:
the primary air port comprises a plurality of air distribution units which are distributed at the bottom of the hearth of the gasification furnace in a circular array; the air distribution unit comprises a primary air pipe positioned in the center of the air distribution unit and a plurality of air caps surrounding the primary air pipe, and the primary air pipe is communicated with the air caps; the primary air enters the hearth of the gasification furnace through the air outlet of the blast cap, and the air outlet of the blast cap is positioned on the side wall of the blast cap;
the pulse tuyere is horizontally intersected and connected with the hearth of the gasification furnace;
the air outlet of the blast cap and the air outlet of the pulse tuyere are positioned at the same height with the slag discharge port of the hearth of the gasification furnace.
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