CN108504394B - Catalytic pyrolysis-gasification integrated reaction device and method - Google Patents

Catalytic pyrolysis-gasification integrated reaction device and method Download PDF

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CN108504394B
CN108504394B CN201710099832.7A CN201710099832A CN108504394B CN 108504394 B CN108504394 B CN 108504394B CN 201710099832 A CN201710099832 A CN 201710099832A CN 108504394 B CN108504394 B CN 108504394B
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fluidized bed
conical fluidized
gas
conical
synthesis gas
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CN108504394A (en
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屠功毅
宗弘元
钟思青
霍威
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/02—Multi-step carbonising or coking processes
    • 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
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the 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
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • 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
    • C10J2300/0959—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
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Industrial Gases (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The invention relates to a catalytic pyrolysis-gasification integrated reaction device and method, which solve the problems of high reaction temperature, low heat value of synthesis gas and low comprehensive utilization rate in the prior gasification technology. The invention mainly comprises a conical fluidized bed, a high-efficiency cyclone device, a chilling chamber and a quick response proportional valve with a control unit, wherein a signal generator controls the quick response proportional valve to generate high-frequency pulsating airflow, so that carbon-containing solid fuels with different particle sizes can quickly reach the layered distribution of coarse bottom particles and fine upper particles in the conical fluidized bed, the carbon-containing solid fuels are combusted at the bottom of the conical fluidized bed, catalytic gasification and pyrolysis are carried out at the middle upper part of the conical fluidized bed, the fine particles in the high-efficiency cyclone device continuously undergo pyrolysis reaction, and the synthesis gas, tar and ash residue are separated in the chilling chamber, so that the technical scheme of obtaining the synthesis gas with high heat value and the high-quality tar can be applied to the field of energy.

Description

Catalytic pyrolysis-gasification integrated reaction device and method
Technical Field
The invention relates to a carbon-containing solid fuel catalytic pyrolysis-gasification integrated reaction device and method, belonging to the field of energy and chemical industry.
Background
The low-rank coal such as brown coal in China has abundant reserves, the utilization degree is gradually increased, and the low-rank coal is not suitable for long-distance transportation due to high volatile components, high moisture and low calorific value and can only be consumed locally. In addition, the volatile content of biomass and part of the carbon-containing solid waste is also high. If the energy-saving gas-fired boiler is used for direct combustion power generation, serious environmental pollution and large amount of greenhouse gas emission can be caused, the power generation efficiency is low, and the comprehensive utilization rate of resources is low. The organic matter volatile components and the fixed carbon in the carbon-containing solid fuel are effectively separated through grading utilization, comprehensive processing and utilization are carried out, tar, synthesis gas and chemicals with high added values are obtained, the strategic significance of energy diversification in China is met, and the method has strong competitiveness.
The gasification temperature of the prior mature gasification process is generally above 1000 ℃, and the defects of high reaction temperature, high energy consumption, difficult purification of the synthesis gas, high cooling strength of the synthesis gas, strict equipment requirement and the like exist. The entrained flow bed technology (such as Texaco, Shell, OMB and the like) as described in pages 26-45 of coal gasification technology published by chemical industry Press 2010 has the advantages of large gasification capacity, high carbon conversion efficiency and the like, is an advanced coal gasification technology at present, develops rapidly in recent years, but has high reaction temperature, large energy consumption and low comprehensive utilization rate of coal, and has a plurality of problems when being applied to poor-quality coal with high moisture, high ash content, high ash melting point and the like.
The catalytic gasification can reduce the reaction temperature without influencing the reaction rate, reduce the energy consumption and the equipment requirement, realize the desulfurization and the dust removal in the furnace, and is beneficial to environmental protection. On the other hand, because the gasification temperature is reduced, the composition distribution of outlet gas products can be effectively adjusted, and H in the synthesis gas can be treated2And CH4The selectivity of the product is better, and a plurality of synthetic processes can be carried out simultaneously. Compared with conventional pyrolysis, the catalytic pyrolysis can obtain tar with higher yield and better quality.
Disclosure of Invention
The invention mainly solves the technical problems that the prior gasification technology has high reaction temperature, low heat value of synthesis gas and lower comprehensive utilization rate, and provides a carbon-containing solid fuel catalytic pyrolysis-gasification integrated reaction device which efficiently couples pyrolysis and gasification reactions in a reactor, so that efficient fractional utilization is realized, the reaction temperature is reduced, the heat value of the synthesis gas is improved, and more tar and high-value-added chemicals with better quality are obtained.
The second technical problem to be solved by the invention is to provide a catalytic pyrolysis-gasification integrated reaction method corresponding to the first technical problem.
In order to solve one of the above technical problems, the technical scheme adopted by the invention is as follows: a catalytic pyrolysis-gasification integrated reaction device comprises a conical fluidized bed, a raw material inlet pipe, a gas distributor, a gasification agent inlet pipe, an oxidant inlet pipe, a gas distribution chamber, a central deslagging pipe, a quick response proportional valve, an electromagnetic valve, an outlet bent pipe, a high-efficiency cyclone device, a return valve, a chilling chamber, a sprayer, a synthetic gas distributor and a dust remover;
the raw materials import pipe is located conical fluidized bed well lower part, gas distributor and gas distribution room are located conical fluidized bed bottom, the gasification agent inlet tube is linked together with the gas distribution room, quick response proportional valve I installs in the gasification agent inlet tube, central scum pipe is linked together with the gas distributor, the oxidant inlet tube is linked together with central scum pipe, quick response proportional valve II installs in the oxidant inlet tube, high-efficient cyclone is linked together with the conical fluidized bed through the export return bend, the material returning valve is connected between high-efficient cyclone and conical fluidized bed, the spray thrower is equipped with at chilling chamber top, inside is equipped with the synthetic gas distributor, the synthetic gas distributor is linked together with high-efficient cyclone, the dust remover is linked together with the chilling chamber.
The diameter of the upper end of the conical fluidized bed is 2-8 times of the diameter of the lower end, the preferred range is 4-6 times, and due to different gas flow rates on different sections, the carbon-containing solid fuel can be distributed in the conical fluidized bed in a layered mode with thick bottom particles and thin upper particles, so that the retention time of different particles in the fluidized bed is optimized, the purpose of layered catalytic pyrolysis-gasification is achieved, and the carbon conversion rate of the carbon-containing solid fuel is improved.
The gas distributor is positioned at the bottom of the conical fluidized bed, the included angle of a conical opening of the gas distributor is 30-150 degrees, preferably 60-120 degrees, air holes are formed in the conical surface of the gas distributor, 5-40 circles of the gas distributor are arranged, the aperture ratio is 1-10 percent, the air holes are uniformly distributed along the circumference, the diameter of each circle of the air holes is increased progressively along the radial direction of the distributor, the air hole close to the central slag discharge pipe is the smallest, the smallest air hole is 0.5-1 mm, the largest air hole is 2-10 mm, the design is adopted to facilitate the layered distribution of particles with different thicknesses in the conical fluidized bed, the gas-solid mixing is enhanced, and the emission.
The response time of the quick response proportional valve I and the quick response proportional valve II is less than 5 milliseconds, so that the proportional valves can rapidly change the opening degrees according to signals generated by the signal generator to generate pulsating air flow.
The efficient cyclone device is provided with an outer cylinder and an inner cylinder, wherein the diameter of the inner cylinder is 0.3-0.8 times, preferably 0.5-0.7 times that of the outer cylinder; the diameter of the exhaust pipe is 0.2-0.7 times, preferably 0.4-0.6 times of that of the inner cylinder; by adopting the design, the coarse particles and the fine particles can be respectively separated out from the inner cylinder and the outer cylinder, and the efficient separation efficiency is realized.
The top of the chilling chamber is provided with a sprayer, the interior of the chilling chamber is provided with a synthesis gas distributor, the sprayer is designed in a conical shape, the diameter of the bottom of the sprayer is 2-8 times, preferably 4-6 times, the diameter of the bottom of the sprayer is 2-8 times, the number of the bottom end socket is 5-20 circles, the aperture ratio is 1-10%, and the apertures are uniformly distributed along the circumference; the synthesis gas distributor adopt the design of toper, the bottom diameter is 2 ~ 6 times of top diameter, preferred 3 ~ 5 times, adopts such design to increase the area of contact of synthesis gas with the cooling water, and can not plug up because of the existence of tar, make the synthesis gas distributor, improved the separation efficiency of synthesis gas, tar and fine ash.
In order to solve the second problem, the invention adopts the following technical scheme: a catalytic pyrolysis-gasification integrated reaction method is characterized by mainly comprising the steps that carbon-containing solid fuel and a catalyst are mixed and then enter a conical fluidized bed through a raw material inlet pipe, an oxidant enters the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipe, a gasifying agent enters the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, the quick response proportional valve I is controlled through a signal generator to generate high-frequency pulsating gas flow, so that the carbon-containing solid fuel with different particle sizes can quickly reach the layered distribution of coarse bottom particles and fine upper particles in the conical fluidized bed, the carbon-containing solid fuel is combusted at the bottom of the conical fluidized bed, the catalytic gasification and pyrolysis are carried out at the middle upper part, and large particle ash slag is discharged from the central slag discharge pipe; the generated mixture of the primary synthesis gas and the fine particles enters the high-efficiency cyclone device through the outlet elbow, the fine particles continuously generate pyrolysis reaction in the high-efficiency cyclone device and then reach the material returning valve, an oxidant is introduced into the bottom of the material returning valve to perform low-temperature combustion, and finally the fine particles enter the bottom of the conical fluidized bed, the secondary synthesis gas coming out of the top of the high-efficiency cyclone device enters the chilling chamber through the synthesis gas distributor, cooling water enters the chilling chamber from the top of the chilling chamber through the sprayer, ash is discharged from the bottom after the secondary synthesis gas is washed and separated in the chilling chamber, tar is discharged from the middle of the chilling chamber, and the tertiary synthesis gas is discharged from the top of the chilling chamber through the dust remover.
The carbon-containing solid fuel comprises: various types of coal, petroleum coke, biomass, carbonaceous solid waste or mixtures thereof, preferably low-rank coal, biomass, high volatile solid waste or mixtures thereof.
The oxidant refers to air, oxygen and oxygen-enriched air; the gasifying agent refers to water vapor, carbon dioxide or a mixture of the water vapor and the carbon dioxide and oxygen.
The catalyst comprises alkali metal, alkaline earth metal, transition metal or a mixture thereof, and the preferable technical proposal is that the catalyst comprises at least one of potassium carbonate, sodium carbonate, potassium hydroxide, sodium hydroxide, calcium oxide, ferric nitrate or molybdenum nitrate;
the catalyst is loaded on the carbon-containing solid fuel in a manner of impregnation method, dry mixing method or ion exchange method; the loading amount of the catalyst accounts for 0.1-30% of the mass of the carbon-containing solid fuel.
The signal generator comprises: the equipment for outputting the level signal and the equipment capable of providing electric signals with various frequencies, wave forms and output levels are controlled by an oscilloscope and computer software.
The signal generator controls the quick response proportional valve to generate pulsating airflow, and the waveform of the pulsating airflow can be any form of wave, preferably square wave and sine wave, so that the control is more convenient.
The oxidant is controlled by a quick response proportional valve II from an oxidant inlet pipe to generate pulsating airflow, and the average flow speed of a nozzle at the upper end of a central deslagging pipe is set to be 1-50 m/s, preferably 10-25 m/s; in the fluidization stage, the pulsation frequency is 0.5-100 Hz, preferably 5-25 Hz, and the pulsation amplitude is 1-100%, preferably 10-50% of the average flow velocity; in the deslagging stage, the opening and closing are carried out according to deslagging conditions, and the preferred opening and closing frequency is 0.01-0.1 Hz.
The gasification agent controls the quick response proportional valve I to generate pulsating airflow through the signal generator, the pulsating frequency is 0.5-100 Hz, preferably 5-25 Hz, and the pulsating amplitude is 0-100%, preferably 10-50% of the average flow speed.
The apparent velocity range of the bottom interface of the conical fluidized bed is 1-30 m/s, preferably 5-20 m/s.
The bottom temperature of the conical fluidized bed is controlled to be 900-1100 ℃, the middle temperature is controlled to be 700-900 ℃, the upper temperature is controlled to be 400-700 ℃, the oxygen-carbon ratio of the conical fluidized bed is controlled to be 0.5-0.7 mol/mol, the water-carbon ratio is controlled to be 1-2 mol/mol, and the operating pressure is 0.5-3 MPa.
The temperature of the high-efficiency cyclone device is controlled to be 300-700 ℃.
The temperature of the material returning valve is controlled to be 400-800 ℃, and the oxygen-carbon ratio is controlled to be 0.6-0.8 mol/mol.
According to the technical scheme, the catalytic pyrolysis-gasification integrated reaction is adopted, combustion is carried out at the bottom of the conical fluidized bed, catalytic gasification and pyrolysis are carried out at the middle upper part, and pyrolysis reaction is continuously carried out on fine particles in the high-efficiency cyclone device, so that the synthesis gas and the tar are obtained. The method realizes the high-efficiency graded utilization of the carbon-containing solid fuel, reduces the reaction temperature, improves the heat value of the synthesis gas and the yield and quality of tar, and has good application prospect.
Drawings
1. FIG. 1 is a schematic flow diagram of a catalytic pyrolysis-gasification integrated reaction apparatus:
in FIG. 1, 1 is a conical fluidized bed; 2 is a raw material inlet pipe; 3 is a gas distributor; 4 is a gasification agent inlet pipe; 5 is an oxidant inlet pipe; 6 is a gas distribution chamber; 7 is a central slag discharge pipe; 8(a) is a quick response proportional valve I, 8(b) is a quick response proportional valve II; 9(a), 9(b), 9(c) and 9(d) are all quick response electromagnetic valves; 10 is an outlet elbow; 11 is a high-efficiency cyclone device; 11(a) is an outer cylinder body of the high-efficiency cyclone device; 11(b) is an inner cylinder body of the high-efficiency cyclone device; 12 is a material return valve; 13 is a chilling chamber; 14 is a synthesis gas distributor; 15 is a sprayer; and 16 is a dust remover.
A is a carbon-containing solid fuel; b is a catalyst; c is a gasifying agent; d is an oxidant; e is large-particle ash; f is a mixture of primary synthesis gas and fine particles; g is an oxidant; h is secondary synthesis gas; i is cooling water; j is tar; k is ash; l is three-stage synthesis gas.
After being mixed, the carbon-containing solid fuel A and the catalyst B enter the conical fluidized bed (1) through the raw material inlet pipe (2), the oxidant D enters the conical fluidized bed (1) from the oxidant inlet pipe (5) through the quick response proportional valve II (8B) from the central slag discharge pipe (7), gasifying agent C enters the conical fluidized bed (1) from the gas distributor (3) after passing through a quick response proportional valve I (8a) and a gas distribution chamber (6) from a gasifying agent inlet pipe (4), the signal generator controls the quick response proportional valve I (8a) to generate high-frequency pulsating gas flow, so that the carbon-containing solid fuel A with different grain diameters can quickly reach the layered distribution with coarse bottom grains and fine upper grains in the conical fluidized bed (1), burning at the bottom of the conical fluidized bed (1), carrying out catalytic gasification and pyrolysis at the middle upper part, and discharging large-particle ash residues E from a central slag discharge pipe (7); the generated mixture F of the primary synthesis gas and fine particles enters a high-efficiency cyclone device (11) through an outlet elbow (10), the fine particles continue to generate pyrolysis reaction in the high-efficiency cyclone device (11), then reach a return valve (12), an oxidant G is introduced to the bottom of the return valve (12) for low-temperature combustion, and finally enter the bottom of a conical fluidized bed (1), the secondary synthesis gas H coming out of the top of the high-efficiency cyclone device (11) enters a chilling chamber (13) through a synthesis gas distributor (14), cooling water I enters from the top of the chilling chamber (13) through a sprayer (15), ash K is discharged at the bottom after the secondary synthesis gas H is washed and separated in the chilling chamber (13), tar J is discharged from the middle, and the tertiary synthesis gas L is discharged from the top through a dust remover (16).
The present invention will be further illustrated by the following examples, but is not limited to these examples.
Detailed Description
[ example 1 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 1m and the height of 5m, and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device is 0.6.
Mixing 0-10mm lignite and 10% potassium carbonate, then feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, controlling the quick response proportional valve I through a signal generator to generate high-frequency pulsating gas flow, so that the lignite with different particle sizes can quickly reach the layered distribution of coarse particles at the bottom and fine particles at the upper part in the conical fluidized bed, burning the bottom of the conical fluidized bed, carrying out catalytic gasification and pyrolysis reaction on the middle upper part, controlling the middle temperature of the conical fluidized bed to be about 800 ℃, controlling the pressure of the conical fluidized bed to be 1MPa, and discharging large-particle ash from the; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 8.4% of the coal inlet quality, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 23%, the hydrogen content is 35.3%, the carbon dioxide content is 2.8%, the methane content is 8.9%, and C.nHmThe content of the coal gas is 0.9 percent, and the high heat value of the coal gas is 13.6MJ/m3The overall carbon conversion was 96%.
[ example 2 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.6.
0-10mm brown coal and 10%Potassium carbonate is mixed and then enters a conical fluidized bed through a raw material inlet pipe, an oxidant enters the conical fluidized bed from a central slag discharge pipe through a quick response proportional valve II from an oxidant inlet pipe, a gasifying agent enters the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, a signal generator controls the quick response proportional valve I to generate high-frequency pulsating gas flow, so that lignite with different particle sizes can quickly reach layered distribution with coarse bottom particles and fine upper particles in the conical fluidized bed, combustion is carried out at the bottom of the conical fluidized bed, catalytic gasification and pyrolysis reaction are carried out on the middle upper part, the temperature in the middle of the conical fluidized bed is controlled to be about 800 ℃, the pressure of the conical fluidized bed is 1MPa, and large-particle ash slag is discharged from the central slag discharge; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 12% of the coal mass, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 21%, the hydrogen content is 35.3%, the carbon dioxide content is 3.5%, the methane content is 12%, and C.nHmThe content of the coal gas is 2.1 percent, and the high heat value of the coal gas is 15.6MJ/m3The overall carbon conversion was 98%.
[ example 3 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 4m and the height of 5m, and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device is 0.6.
Mixing 0-10mm lignite and 10% potassium carbonate, feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipeIn the conical fluidized bed, a gasifying agent passes through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe and then enters a conical fluidized bed from a gas distributor, a signal generator controls the quick response proportional valve I to generate high-frequency pulsating gas flow, so that lignite with different particle sizes is quickly layered and distributed in the conical fluidized bed, the lignite is in a form of coarse bottom particles and fine top particles, combustion is carried out at the bottom of the conical fluidized bed, catalytic gasification and pyrolysis reactions are carried out on the middle-upper part of the conical fluidized bed, the temperature in the middle of the conical fluidized bed is controlled to be about 800 ℃, the pressure of the conical fluidized bed is 1MPa, and large-particle ash residues are discharged from a; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 8.2% of the coal mass, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 25.2%, the hydrogen content is 41.3%, the carbon dioxide content is 1.5%, the methane content is 5.8%, and C are contained.nHmThe content of the coal gas is 0.5 percent, and the high heat value of the coal gas is 11.6MJ/m3The overall carbon conversion was 99%.
[ example 4 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.3.
Mixing 0-10mm lignite and 10% potassium carbonate, feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after the gasifying agent passes through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, and feeding the gasifying agent into the conical fluidized bed through a gas distributorThe signal generator controls the quick response proportional valve I to generate high-frequency pulsating airflow, so that lignite with different particle sizes can quickly reach the layered distribution of coarse bottom particles and fine upper particles in the conical fluidized bed, the lignite is combusted at the bottom of the conical fluidized bed, catalytic gasification and pyrolysis reaction are carried out on the middle upper part of the conical fluidized bed, the temperature of the middle part of the conical fluidized bed is controlled to be about 800 ℃, the pressure of the conical fluidized bed is 1MPa, and large-particle ash residues are discharged from the central slag discharge pipe; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 9.2% of the coal mass, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 20.8%, the hydrogen content is 38.3%, the carbon dioxide content is 2.5%, the methane content is 9.2%, and C are contained.nHmThe content of the coal gas is 1.8 percent, and the high heat value of the coal gas is 12.2MJ/m3The overall carbon conversion was 95%.
[ example 5 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.5.
Mixing 0-10mm lignite and 10% potassium carbonate, feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central deslagging pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, controlling the quick response proportional valve I through a signal generator to generate high-frequency pulsating gas flow, and enabling the lignite with different particle sizes to quickly reach the bottom in the conical fluidized bedThe coarse upper part of the particles is in fine particle layered distribution, the combustion is carried out at the bottom of the conical fluidized bed, the catalytic gasification and pyrolysis reaction are carried out at the middle upper part, the temperature of the middle part of the conical fluidized bed is controlled to be about 800 ℃, the pressure of the conical fluidized bed is 1MPa, and large particle ash residues are discharged from a central slag discharge pipe; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 9.6% of the coal inlet quality, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 20.2%, the hydrogen content is 37.2%, the carbon dioxide content is 2.8%, the methane content is 10.8%, and C.nHmThe content of the coal gas is 1.4 percent, and the high heat value of the coal gas is 14.4MJ/m3The overall carbon conversion was 98%.
[ example 6 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.7.
Mixing 0-10mm lignite and 10% potassium carbonate, and then feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from a central deslagging pipe through a quick response proportional valve II from an oxidant inlet pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, controlling the quick response proportional valve I through a signal generator to generate high-frequency pulsating gas flow, so that the lignite with different particle sizes can quickly reach the layered distribution of coarse bottom particles and fine upper particles in the conical fluidized bed, burning the bottom of the conical fluidized bed, carrying out catalytic gasification and pyrolysis on the middle upper part, and controlling the conical fluidized bedThe temperature of the middle part is about 800 ℃, the pressure of the conical fluidized bed is 1MPa, and large-particle ash slag is discharged from the central slag discharge pipe; the generated mixture of the first-grade synthesis gas and the fine particles enters a high-efficiency cyclone device through an outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, the fine particles continuously carry out pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, introducing oxidant into the bottom of the material returning valve, low-temperature burning, finally entering the bottom of the conical fluidized bed, introducing the secondary synthetic gas from the top of the high-efficiency cyclone device into a chilling chamber through a synthetic gas distributor, introducing cooling water from the top of the chilling chamber through a sprayer, washing and separating the secondary synthetic gas in the chilling chamber, the ash is discharged from the bottom, the tar is discharged from the middle, the tar amount is about 10.8% of the coal mass, the third-stage synthesis gas is discharged from the top through a dust remover, the carbon monoxide content of the third-stage synthesis gas product is 21.8%, the hydrogen content is 33.1%, the carbon dioxide content is 3.1%, the methane content is 10.6%, and C are contained.nHmThe content of the coal gas is 1.8 percent, and the high heat value of the coal gas is 13.8MJ/m3The overall carbon conversion was 97%.
[ example 7 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.8.
Mixing 0-10mm lignite and 10% potassium carbonate, then feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, controlling the quick response proportional valve I through a signal generator to generate high-frequency pulsating gas flow, so that the lignite with different particle sizes can quickly reach the layered distribution of coarse particles at the bottom and fine particles at the upper part in the conical fluidized bed, burning the bottom of the conical fluidized bed, carrying out catalytic gasification and pyrolysis reaction on the middle upper part, controlling the middle temperature of the conical fluidized bed to be about 800 ℃, controlling the pressure of the conical fluidized bed to be 1MPa, and discharging large-particle ash from the; the resulting primary syngas and fine particulate mixtureThe high-efficiency synthetic gas enters a high-efficiency cyclone device through an outlet bent pipe, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, fine particles continuously undergo pyrolysis reaction in the high-efficiency cyclone device and then reach a material returning valve, an oxidant is introduced into the bottom of the material returning valve to perform low-temperature combustion, and finally the fine particles enter the bottom of a conical fluidized bed, secondary synthetic gas coming out of the top of the high-efficiency cyclone device enters a chilling chamber through a synthetic gas distributor, cooling water enters the chilling chamber from the top of the chilling chamber through a sprayer, ash is discharged from the bottom after the secondary synthetic gas is washed and separated in the chilling chamber, tar is discharged from the middle of the chilling chamber, the tar amount is about 9.2 percent of the coal inlet quality, tertiary synthetic gas is discharged from the top through a dust remover, the product of the tertiary synthetic gas has the carbon monoxide content of 27.8 percent, the hydrogen content of 33.3 percent, thenHmThe content of the coal gas is 0.8 percent, and the high heat value of the coal gas is 11.8MJ/m3The overall carbon conversion was 94%.
[ example 8 ]
The catalytic pyrolysis-gasification integrated reaction device has the inner diameter of the lower end of a conical fluidized bed of 0.5m, the maximum inner diameter of the upper end of the conical fluidized bed of 2.5m, the height of 5m and the diameter ratio of an inner cylinder body and an outer cylinder body of a high-efficiency cyclone device of 0.6.
Mixing 0-10mm lignite and 10% calcium oxide, then feeding the mixture into a conical fluidized bed through a raw material inlet pipe, feeding an oxidant into the conical fluidized bed from an oxidant inlet pipe through a quick response proportional valve II from a central slag discharge pipe, feeding a gasifying agent into the conical fluidized bed from a gas distributor after passing through a quick response proportional valve I and a gas distribution chamber from a gasifying agent inlet pipe, controlling the quick response proportional valve I through a signal generator to generate high-frequency pulsating gas flow, so that the lignite with different particle sizes can quickly reach the layered distribution of coarse particles at the bottom and fine particles at the upper part in the conical fluidized bed, burning the bottom of the conical fluidized bed, carrying out catalytic gasification and pyrolysis reaction on the middle upper part, controlling the middle temperature of the conical fluidized bed to be about 800 ℃, controlling the pressure of the conical fluidized bed to be 1MPa, and discharging large-particle ash from the central; the generated mixture of the first-grade synthesis gas and the fine particles enters the high-efficiency cyclone device through the outlet elbow, the temperature of the high-efficiency cyclone device is controlled to be about 500 ℃, and the fine particles continuously undergo pyrolysis reaction in the high-efficiency cyclone deviceAnd then the mixture reaches a return valve, an oxidant is introduced into the bottom of the return valve to perform low-temperature combustion, and finally the mixture enters the bottom of a conical fluidized bed, secondary synthetic gas coming out of the top of the high-efficiency cyclone device enters a chilling chamber through a synthetic gas distributor, cooling water enters from the top of the chilling chamber through a sprayer, after the secondary synthetic gas is washed and separated in the chilling chamber, ash is discharged at the bottom, tar is discharged from the middle, the tar amount is about 7.4% of the coal inlet quality, tertiary synthetic gas is discharged from the top through a dust remover, the carbon monoxide content of a product of the tertiary synthetic gas is 28.1%, the hydrogen content is 39.3%, the carbon dioxide content is 0.8%, the methane content is 5.2%, and the carbon content is 39.3%, the carbonnHmThe content of the coal gas is 0.4 percent, and the high heat value of the coal gas is 10.6MJ/m3The overall carbon conversion was 98%.
[ COMPARATIVE EXAMPLE 1 ]
Adopting an ash fusion fluidized bed coal gasification reaction device, selecting lignite of 0-6mm as a raw material, operating pressure of 0.04MPa and average operating temperature of 1000 ℃, and obtaining a synthesis gas product with carbon monoxide content of 21.9%, hydrogen content of 38.6%, methane content of 4.3%, carbon dioxide content of 22%, nitrogen content of 7.11%, and gas heat value of 9.4MJ/m3The carbon conversion was only 90%.
Examples 1 to 8 and comparative example 1 are summarized in Table 1.
TABLE 1
Figure GDA0002443643700000101
Figure GDA0002443643700000111
From the comparison of the process indexes in table 1, it can be seen that the catalytic pyrolysis-gasification integrated reaction apparatus disclosed in the present invention has the best effect in example 2, the carbon conversion rate is increased by approximately 8% compared with comparative example 1, the methane content is increased by approximately 8%, the gas calorific value is increased, and the tar with a high yield is obtained.

Claims (10)

1. A catalytic pyrolysis-gasification integrated reaction device is characterized by comprising a conical fluidized bed (1), a raw material inlet pipe (2), a gas distributor (3), a gasifying agent inlet pipe (4), an oxidant inlet pipe (5), a gas distribution chamber (6), a central slag discharge pipe (7), a quick response proportional valve, an electromagnetic valve, an outlet elbow (10), a high-efficiency cyclone device (11), a material return valve (12), a chilling chamber (13), a synthetic gas distributor (14), a sprayer (15) and a dust remover (16);
the raw material inlet pipe (2) is positioned at the middle lower part of the conical fluidized bed (1), the gas distributor (3) and the gas distribution chamber (6) are positioned at the bottom of the conical fluidized bed (1), the gasifying agent inlet pipe (4) is communicated with the gas distribution chamber (6), the quick response proportional valve I (8a) is installed in the gasifying agent inlet pipe (4), the central deslagging pipe (7) is communicated with the gas distributor (3), the oxidant inlet pipe (5) is communicated with the central deslagging pipe (7), the quick response proportional valve II (8b) is installed in the oxidant inlet pipe (5), the efficient cyclone device (11) is communicated with the conical fluidized bed (1) through an outlet elbow pipe (10), the material return valve (12) is connected between the efficient cyclone device (11) and the conical fluidized bed (1), the top of the chilling chamber (13) is provided with a sprayer (15), and the synthesis gas distributor (14) is installed inside the chilling chamber, the synthesis gas distributor (14) is communicated with the high-efficiency cyclone device (11), and the dust remover (16) is communicated with the chilling chamber (13).
2. The catalytic pyrolysis-gasification integrated reaction apparatus according to claim 1, wherein the diameter of the upper end of the conical fluidized bed (1) is 2 to 8 times of the diameter of the lower end.
3. The catalytic pyrolysis-gasification integrated reaction device according to claim 1, wherein the gas distributor (3) is located at the bottom of the conical fluidized bed (1), the included angle of the conical opening of the gas distributor (3) is 30-150 degrees, 5-40 circles of gas holes are arranged on the conical surface of the gas distributor (3), the aperture ratio is 1-10%, the gas holes are uniformly distributed along the circumference, the diameter of each circle of gas holes increases gradually along the radial direction of the distributor, the gas hole close to the central slag discharge pipe (7) is the smallest, the smallest gas hole is 0.5-1 mm, and the largest gas hole is 2-10 mm.
4. A catalytic pyrolysis-gasification integrated reaction apparatus according to claim 1, wherein the response time of the fast response proportional valve I (8a) and the fast response proportional valve II (8b) is less than 5 ms.
5. The catalytic pyrolysis-gasification integrated reaction device according to claim 1, wherein the high efficiency cyclone device (11) is provided with an outer cylinder (11a) and an inner cylinder (11b), and the diameter (11b) of the inner cylinder is 0.3-0.8 times of the diameter (11a) of the outer cylinder.
6. The catalytic pyrolysis-gasification integrated reaction device according to claim 1, wherein a sprayer (15) is arranged at the top of the chilling chamber (13), a synthesis gas distributor (14) is arranged in the chilling chamber, the sprayer (15) is designed in a conical shape, the diameter of the bottom of the sprayer (15) is 2-8 times of that of the top of the sprayer, a bottom end socket is provided with small holes, 5-20 circles are arranged, the opening rate is 1-10%, and the small holes are uniformly distributed along the circumference; the synthesis gas distributor (14) is designed in a conical mode, and the diameter of the bottom of the synthesis gas distributor is 2-6 times of that of the top of the synthesis gas distributor.
7. A catalytic pyrolysis-gasification integrated reaction method adopts any one of the catalytic pyrolysis-gasification integrated reaction devices of claims 1-6, and is characterized by mainly comprising the following steps: after being mixed, the carbon-containing solid fuel A and the catalyst B enter the conical fluidized bed (1) through the raw material inlet pipe (2), the oxidant D enters the conical fluidized bed (1) from the oxidant inlet pipe (5) through the quick response proportional valve II (8B) from the central slag discharge pipe (7), gasifying agent C enters the conical fluidized bed (1) from the gas distributor (3) after passing through a quick response proportional valve I (8a) and a gas distribution chamber (6) from a gasifying agent inlet pipe (4), the signal generator controls the quick response proportional valve I (8a) to generate high-frequency pulsating gas flow, so that the carbon-containing solid fuel A with different grain diameters can quickly reach the layered distribution with coarse bottom grains and fine upper grains in the conical fluidized bed (1), burning at the bottom of the conical fluidized bed (1), carrying out catalytic gasification and pyrolysis at the middle upper part, and discharging large-particle ash residues E from a central slag discharge pipe (7); the generated mixture F of the primary synthesis gas and fine particles enters a high-efficiency cyclone device (11) through an outlet elbow (10), the fine particles continue to generate pyrolysis reaction in the high-efficiency cyclone device (11), then reach a return valve (12), an oxidant G is introduced to the bottom of the return valve (12) for low-temperature combustion, and finally enter the bottom of a conical fluidized bed (1), the secondary synthesis gas H coming out of the top of the high-efficiency cyclone device (11) enters a chilling chamber (13) through a synthesis gas distributor (14), cooling water I enters from the top of the chilling chamber (13) through a sprayer (15), ash K is discharged at the bottom after the secondary synthesis gas H is washed and separated in the chilling chamber (13), tar J is discharged from the middle, and the tertiary synthesis gas L is discharged from the top through a dust remover (16).
8. The catalytic pyrolysis-gasification integrated reaction method according to claim 7, wherein the gasifying agent C controls the quick response proportional valve I (8a) through a signal generator to generate a pulsating gas flow, the pulsating frequency is 0.5-100 Hz, and the pulsating amplitude is 10-100% of the average flow rate.
9. The catalytic pyrolysis-gasification integrated reaction method according to claim 7, wherein the oxidant D is controlled by a quick response proportional valve II (8b) from an oxidant inlet pipe (5) to generate a pulsating gas flow, and in the fluidizing stage, the pulsating frequency is 0.5-100 Hz, and the pulsation amplitude is 1% -100% of the average flow rate; in the deslagging stage, opening and closing are performed according to deslagging conditions.
10. The catalytic pyrolysis-gasification integrated reaction method according to claim 7, wherein the bottom temperature of the conical fluidized bed (1) is controlled to be 900-1100 ℃, the middle temperature is controlled to be 700-900 ℃, the upper temperature is controlled to be 400-700 ℃, the oxygen-carbon ratio of the conical fluidized bed (1) is controlled to be 0.5-0.7 mol/mol, the water-carbon ratio is controlled to be 1-2 mol/mol, and the operating pressure is 0.5-3 MPa;
the temperature of the high-efficiency cyclone device (11) is controlled to be 300-700 ℃;
the temperature of the material returning valve (12) is controlled to be 400-800 ℃, and the oxygen-carbon ratio is controlled to be 0.6-0.8 mol/mol.
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