CN105861069B - Solid fuel double fluidized bed thermal partial gasification staged conversion device and method - Google Patents
Solid fuel double fluidized bed thermal partial gasification staged conversion device and method Download PDFInfo
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- CN105861069B CN105861069B CN201610355483.6A CN201610355483A CN105861069B CN 105861069 B CN105861069 B CN 105861069B CN 201610355483 A CN201610355483 A CN 201610355483A CN 105861069 B CN105861069 B CN 105861069B
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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
- C10J3/72—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
- C10J2300/0916—Biomass
-
- 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
- C10J2300/0916—Biomass
- C10J2300/092—Wood, cellulose
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1637—Char combustion
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
- C10J2300/1656—Conversion of synthesis gas to chemicals
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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
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
- C10J2300/1675—Integration of gasification processes with another plant or parts within the plant with the production of electricity making use of a steam turbine
-
- 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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Abstract
The present invention relates to solid fuel producing synthesis gas technologies, it is desirable to provide a kind of solid fuel double fluidized bed thermal partial gasification staged conversion device and method.The device is made of normal pressure or pressurized fluidized bed gasifier and fluid-bed combustion furnace, and pressure is 0.1-5MPa when pressurization is run.This method is that first solid fuel is gasified in fluidized-bed gasification furnace using oxygen, vapor or carbon dioxide as gasifying agent, generates synthesis gas, then the semicoke that gasification generates is sent and is burnt into fluid-bed combustion furnace.The present invention uses double-fluidized-bed while generating synthesis gas and high-temperature flue gas, realizes the staged conversion of solid fuel；With stronger fuel tolerance, pollutant emission is low, easy to operate, and treating capacity is big, it is easy to accomplish large-scale production.Tar content is few in the synthesis gas of generation, and calorific value is higher.Compared with the technology of being gasified totally, excessively high efficiency of carbon con version is not emphasized, and requisite oxygen consumption significantly reduces, while can reduce reaction, reduces equipment manufacturing cost, has greater advantages in economy.
Description
Technical field
The present invention relates to solid fuel producing synthesis gas technology, in particular to a kind of solid fuel double fluidized bed thermal partial gasification
Staged conversion device and method.
Background technique
The energy resource structure in China is rich coal, few oil, deficency.Rich coal resources in China, yield is huge, and coal accounts for China's energy
The 70% of source total quantity consumed；But the direct burning of coal leads to serious environmental pollution, to national economy sustainable development and
People's lives all cause large effect.In addition, the biomass resource as one of clean reproducible energy, the storage in China
Measure also very abundant.Therefore, the more clean Coal Gasification Technology of utilization, will the solids combustion such as coal relatively abundant, biomass
Material is for power generation and synthesis gas production, it is possible to reduce the pollution of environment, while the pressure of China's natural gas import is alleviated, therefore
It has important practical significance.
However, existing gasification technology needs to reach under conditions of high temperature and pressure substantially all using the mode that is gasified totally
High efficiency of carbon con version, harsh reaction condition greatly improve the manufacturing cost and maintenance cost of reaction equipment.Meanwhile it is complete
The oxygen demand of full gasification technology is big, needs to be equipped with large-scale air gas separation unit, construction cost greatly increases.
Summary of the invention
The technical problem to be solved by the present invention is to overcome the deficiencies of the prior art and provide a kind of solid fuel double fluidized bed thermal
Partial gasification staged conversion device and method.
In order to solve the technical problem, solution of the invention is:
A kind of solid fuel double fluidized bed thermal partial gasification staged conversion device, including fluid-bed combustion furnace and fluidized bed are provided
Gasification furnace；
The bottom of the fluidized-bed gasification furnace sets gasification agent inlet, and middle and lower part sets solid fuel feedstock mouth, and middle part sets overflow
Mouthful, top sets syngas outlet；The bottom of the fluid-bed combustion furnace sets air intake, and middle and lower part sets semicoke material inlet, top
Portion sets exhanst gas outlet；The overflow port is connected to semicoke material inlet through the 4th material returning device by pipeline；
On the synthesis gas discharge pipe to connect with syngas outlet, it is equipped with the first cyclone separator；First cyclonic separation
The bottom of device is connected to semicoke material inlet by the first material returning device, or is connected to the recycle stock set on fluidized-bed gasification furnace middle and lower part
Entrance；
The second cyclone separator is equipped on the pipeline to connect with exhanst gas outlet；The bottom of second cyclone separator passes through the
Two material returning devices are connected to semicoke material inlet.
It further include the third whirlwind point on the first cyclone separator top exit synthesis gas discharge pipe in the present invention
From device；Gas discharge pipe is bonded at the top of third cyclone separator, bottom is connected to the pipeline of the first material returning device outlet, or logical
It crosses third material returning device and is connected to semicoke material inlet.
In the present invention, the inside of the fluidized-bed gasification furnace is divided into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Wherein,
Gasification agent inlet is connected with air compartment, and solid fuel feedstock mouth is located in the middle part of emulsion zone, and overflow port is located at the top of emulsion zone, synthesis gas
Outlet is located at the top of dilute-phase zone；The inside of the fluid-bed combustion furnace is divided into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Its
In, air intake is connect with air compartment, and semicoke material inlet is located in the middle part of emulsion zone, and exhanst gas outlet is located at the top of dilute-phase zone.
Invention further provides the solid fuel double fluidized bed thermal partial gasification staged conversion method based on aforementioned device,
Include:
(1) coal dust and/or biomass dry powder are added to fluidized-bed gasification furnace by solid fuel feedstock mouth, in emulsion zone
With the raw gasification reaction of the gasifying agent hybrid concurrency from bottom, synthesis gas is generated；
The mass ratio for controlling solid fuel and gasifying agent makes solid fuel that partial gasification occur；Gasifying agent is water vapour-
Oxygen mixture or carbon dioxide-oxygen mixture；Fluidized-bed gasification furnace is normal pressure or pressurization operation, and pressure is when pressurization is run
0.1-5MPa, running temperature are 900-1000 DEG C；In gasifying agent, the mass ratio of water vapour and solid fuel is 0.1-0.5, oxygen
The mass ratio of gas and solid fuel is 0.3-1, and the mass ratio of carbon dioxide and solid fuel is 0.2-0.8；
(2) synthesis gas of fluidized-bed gasification furnace discharge is then sent to delivery pipe through level-one or two stage cyclone separator dedusting
Road；Separating obtained dust is sent by material returning device to the semicoke material inlet of fluid-bed combustion furnace, or sends the close of fluidized-bed gasification furnace back to
Phase region re-starts reaction；
(3) semicoke material obtained by gasification reaction is discharged from the overflow port at the top of fluidized-bed gasification furnace emulsion zone, and by returning charge
Device is sent to the semicoke material inlet of fluid-bed combustion furnace；Emulsion zone in fluid-bed combustion furnace, semicoke material with come from bottom
Air combustion reaction occurs, generating temperature is 900-950 DEG C of high-temperature flue gas；
The mass ratio for controlling the material of bottom air and semicoke material inlet is 1-1.2, semicoke material occurs complete
Burning；Fluid-bed combustion furnace is normal pressure or pressurization operation, and pressure is 0.1-5MPa when pressurization is run；Running temperature is 900-950
℃；
(4) flue gas of fluid-bed combustion furnace discharge is sent again after being dusted by cyclone separator to discharge pipe, separates institute
The semicoke material inlet that dust is returned to fluid-bed combustion furnace by material returning device is obtained, combustion reaction is re-started.
In the present invention, the biomass dry powder refers to the dry powder of agricultural crop straw, and granularity is 10mm or less；The coal dust
Granularity be 8mm or less.
Inventive principle description:
The chemical structure feature of the solid fuels such as present invention combination coal, biomass wherein activity preferably will be easy to gas first
That changes is partially converted into synthesis gas, and then the generated semicoke for being not easy to gasify burns as raw material, produces high temperature cigarette
Gas for production high-temperature steam in subsequent technique to be used to generate electricity, to realize the partial gasification of the solid fuels such as coal and biomass
Staged conversion.It is compared compared with current being gasified totally or directly burn, solid fuel partial gasification technology is with oxygen demand is low, sets
The advantages that standby low cost.Gas turbine power generation cannot be only used for using the synthesis gas that this method obtains, also can be used as chemical industry synthesis
The raw material of production.
Compared with prior art, the invention has the benefit that
1, the double-fluidized-bed operating method combined using fluidized-bed gasification furnace and fluid-bed combustion furnace, while generating synthesis
Gas and high-temperature flue gas realize the staged conversion of solid fuel.
2, there is stronger fuel tolerance, pollutant emission as reactor using fluidized-bed gasification furnace and combustion furnace
Low, easy to operate, treating capacity is big, it is easy to accomplish large-scale production.
3, solid fuel and oxygen/water steam or water vapour/carbon dioxide gasified reverse are carried out using fluidized-bed gasification furnace
It answers, tar content is few in the synthesis gas of generation, and calorific value is higher, can be used as industry or domestic fuel；Semicoke material is in fluidized bed combustion
It burns in furnace and burns, form high-temperature flue gas, can be used for producing high pressure high temperature vapor to realize power generation.
4, it is not emphasized excessively high compared with the technology of being gasified totally using Fluidized Bed Partial gasification technology processing solid fuel
Efficiency of carbon con version, requisite oxygen consumption significantly reduces, while can reduce reaction, reduces equipment manufacturing cost, has in economy bigger
Advantage.
Detailed description of the invention
Fig. 1 is the schematic diagram of the first implementation of device of the present invention.
Fig. 2 is that the schematic diagram of another implementation of device of the present invention (increases a returning charge in Fig. 1 device
Device).
In figure: solid fuel feedstock mouth 1, gasification agent inlet 2, fluidized-bed gasification furnace 3, the first material returning device 4, the first whirlwind point
From device 5, third cyclone separator 6, synthesis gas discharge pipe 7, the second cyclone separator 8, the second material returning device 9, fluidized bed combustion
Furnace 10, air intake 11, flue gas emission pipeline 12, overflow port 13, third material returning device 14, semicoke material inlet 15, recycle stock
Entrance 16, the 4th material returning device 17.
Specific embodiment
With reference to the accompanying drawing, implementation of the invention is described.
Solid fuel double fluidized bed thermal partial gasification staged conversion device of the present invention, including fluid-bed combustion furnace 10 and stream
Change bed gasification furnace 3.The bottom of fluidized-bed gasification furnace 3 sets gasification agent inlet 2, and middle and lower part sets solid fuel feedstock mouth 1, and middle part sets excessive
Head piece 13, top sets syngas outlet.The bottom of fluid-bed combustion furnace 10 sets air intake 11, and middle and lower part sets semicoke material inlet
15, top sets exhanst gas outlet；The overflow port 13 is connected to semicoke material inlet 15 through the 4th material returning device 14 by pipeline.
On the synthesis gas discharge pipe to connect with syngas outlet, it is equipped with the first cyclone separator 5；First cyclonic separation
The bottom of device 5 is connected to semicoke material inlet 15 (as shown in fig. 1) by the first material returning device 4, or is connected to set on fluidized gasification
The recycle stock entrance 16 (as shown in Figure 2) of 3 middle and lower part of furnace；
The second cyclone separator 8 is equipped on the pipeline to connect with exhanst gas outlet；The bottom of second cyclone separator 8 passes through
Second material returning device 9 is connected to semicoke material inlet 15, top cigarette receiving gas discharge pipe 12.
In order to further separate dust, also can be on 5 top exit synthesis gas discharge pipe of the first cyclone separator
Third cyclone separator 6 is set.The top of third cyclone separator 6 is bonded into gas discharge pipe 7, and bottom is connected to the first returning charge
The pipeline that device 4 exports, the dust of collection is sent to semicoke material inlet 15 (as shown in fig. 1), or is sent to recycle stock entrance
16.It, can also be single in the bottom of third cyclone separator 6 in the case where the first material returning device 4 is connected to recycle stock entrance 16
Solely the 4th material returning device 17 of setting, directly send dust to semicoke material inlet 15 (as shown in Figure 2).
The inside of fluidized-bed gasification furnace 3 is divided into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Wherein, gasification agent inlet 2 with
Air compartment is connected, and solid fuel feedstock mouth 1 is located in the middle part of emulsion zone, and overflow port 13 is located at the top of emulsion zone, and syngas outlet is located at
At the top of dilute-phase zone.The inside of fluid-bed combustion furnace 10 is also classified into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Wherein, air enters
Mouth 11 is connect with air compartment, and semicoke material inlet 15 is located in the middle part of emulsion zone, and exhanst gas outlet is located at the top of dilute-phase zone.
The method for realizing solid fuel double fluidized bed thermal partial gasification staged conversion using above-mentioned apparatus, specifically includes:
(1) coal dust and/or biomass dry powder are added to fluidized-bed gasification furnace 3 by solid fuel feedstock mouth 1, in close phase
Area and the raw gasification reaction of the gasifying agent hybrid concurrency from bottom, generate synthesis gas；
The mass ratio for controlling solid fuel and gasifying agent makes solid fuel that partial gasification occur；Gasifying agent is water vapour-
Oxygen mixture or carbon dioxide-oxygen mixture；Fluidized-bed gasification furnace is normal pressure or pressurization operation, and pressure is when pressurization is run
0.1-5MPa, running temperature are 900-1000 DEG C；In gasifying agent, the mass ratio of water vapour and solid fuel is 0.1-0.5, oxygen
The mass ratio of gas and solid fuel is 0.3-1, and the mass ratio of carbon dioxide and solid fuel is 0.2-0.8；
(2) synthesis gas that fluidized-bed gasification furnace 3 discharges is through level-one or two stage cyclone separator 5,6 dedustings, the row of being then sent to
Put pipeline；Separating obtained dust is sent by the first material returning device 4 or the 4th material returning device 17 to the semicoke material inlet of fluid-bed combustion furnace,
Or it sends the emulsion zone of fluidized-bed gasification furnace 3 back to and re-starts reaction；
(3) semicoke material obtained by gasification reaction is discharged from the overflow port at the top of 3 emulsion zone of fluidized-bed gasification furnace, and by returning charge
Device 14 is sent to the semicoke material inlet of fluid-bed combustion furnace；Emulsion zone in fluid-bed combustion furnace, semicoke material with come from bottom
Combustion reaction occurs for the air in portion, generates the high-temperature flue gas that temperature is 900-950 DEG C；
The mass ratio for controlling the material of bottom air and semicoke material inlet is 1-1.2, semicoke material occurs complete
Burning；Fluid-bed combustion furnace 10 is normal pressure or pressurization operation, and pressure is 0.1-5MPa when pressurization is run；Running temperature is 900-
950℃；
(4) flue gas that fluid-bed combustion furnace 10 discharges is sent after being dusted by cyclone separator 8 again to discharge pipe, separation
Gained dust is returned to the semicoke material inlet 15 of fluid-bed combustion furnace 10 by material returning device 9, re-starts combustion reaction.
In the present invention, biomass dry powder or coal dust can be as solid fuel.Biomass dry powder refers to crops straw
The dry powder of stalk, granularity are 10mm or less；The granularity of coal dust is 8mm or less.
Specific application example:
Coal dust is added into the emulsion zone of fluidized-bed gasification furnace 3 by solid fuel feedstock mouth 1, coal-supplying amount 4320t/d, with
Vapor/oxygen mix from bottom, oxygen coal ratio are 0.46, and steam coal ratio is 0.15.In order to control the tar that gasification generates
Amount, 3 temperature of fluidized-bed gasification furnace are controlled at 980 DEG C or so.Fluidized-bed gasification furnace is that normal pressure or pressurization operation, pressurization are pressed when running
Power is 0.1-5MPa.In fluidized-bed gasification furnace 3, gasification reaction occurs for coal dust and vapor, oxygen, generates synthesis gas.Synthesis
Throughput is 286955.26m3/ h leaves fluidized-bed gasification furnace by two stage cyclone separator.Synthesis gas can be used for generating electricity, the people
With purposes such as coal gas, and the semicoke and flying dust separated through two stage cyclone separator then passes through the first material returning device 4 and is delivered to stream
Fluidized bed combustion furnace 10 burns.The principal feedstock of fluid-bed combustion furnace 10 comes from the semicoke material of fluidized-bed gasification furnace 3.
In fluidized-bed gasification furnace 3, the semicoke material that solid fuel partial gasification generates is overflowed from the overflow port 13 at the top of emulsion zone, and is passed through
Third material returning device 14 is fed directly to fluid-bed combustion furnace 10, and semicoke material inlet amount is 17804.9kg/h.In fluidized bed combustion
In furnace 10, semicoke material and air carry out burning and generate high-temperature flue gas, air mass flow 17804.9-21365.9kg/h, burning
The high-temperature flue gas of generation carries high-temperature material into the second cyclone separator 8, and isolated high-temperature material is through the second returning charge
Device 9 returns to fluid-bed combustion furnace 10.The running temperature of fluid-bed combustion furnace 10 is 900-950 DEG C, is normal pressure or pressurization fortune
Row, pressure is 0.1-5MPa when pressurization is run.
Claims (3)
1. a kind of solid fuel double fluidized bed thermal partial gasification staged conversion device, the fluid-bed combustion furnace including being equipped with slag-drip opening,
It is characterized in that, further including fluidized-bed gasification furnace；
The bottom of the fluidized-bed gasification furnace sets gasification agent inlet, and middle and lower part sets solid fuel feedstock mouth, and middle part sets overflow port, top
Portion sets syngas outlet；The bottom of the fluid-bed combustion furnace sets air intake, and middle and lower part sets semicoke material inlet, and top sets cigarette
Gas outlet；The overflow port is connected to semicoke material inlet through the 4th material returning device by pipeline；
On the synthesis gas discharge pipe to connect with syngas outlet, it is equipped with the first cyclone separator；First cyclone separator
Bottom is connected to semicoke material inlet by the first material returning device, or the recycle stock being connected to set on fluidized-bed gasification furnace middle and lower part enters
Mouthful；
The second cyclone separator is equipped on the pipeline to connect with exhanst gas outlet；It is returned by second the bottom of second cyclone separator
Glassware is connected to semicoke material inlet；
The inside of the fluidized-bed gasification furnace is divided into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Wherein, gasification agent inlet and wind
Room is connected, and solid fuel feedstock mouth is located in the middle part of emulsion zone, and overflow port is located at the top of emulsion zone, and syngas outlet is located at dilute-phase zone
Top；The inside of the fluid-bed combustion furnace is divided into air compartment, emulsion zone and dilute-phase zone from the bottom to top；Wherein, air intake and wind
Room connection, semicoke material inlet are located in the middle part of emulsion zone, and exhanst gas outlet is located at the top of dilute-phase zone；
First cyclone separator top exit synthesis gas discharge pipe is equipped with third cyclone separator；Third cyclone separator
Top is bonded into gas discharge pipe, and bottom is connected to the pipeline of the first material returning device outlet, or is connected to semicoke by third material returning device
Material inlet.
2. the solid fuel double fluidized bed thermal partial gasification staged conversion method based on claim 1 described device, which is characterized in that
Include:
(1) coal dust or biomass dry powder are added to fluidized-bed gasification furnace by solid fuel feedstock mouth, emulsion zone with come from
The raw gasification reaction of the gasifying agent hybrid concurrency of bottom, generates synthesis gas；
The mass ratio for controlling solid fuel and gasifying agent makes solid fuel that partial gasification occur；Gasifying agent is water vapour-oxygen
Mixture or carbon dioxide-oxygen mixture；Fluidized-bed gasification furnace is normal pressure or pressurization operation, and pressure is 0.1- when pressurization is run
5MPa, running temperature are 900-1000 DEG C；In gasifying agent, the mass ratio of water vapour and solid fuel is 0.1-0.5, oxygen with
The mass ratio of solid fuel is 0.3-1, and the mass ratio of carbon dioxide and solid fuel is 0.2-0.8；
(2) synthesis gas of fluidized-bed gasification furnace discharge is then sent to discharge pipe through level-one or two stage cyclone separator dedusting；Point
It is sent by material returning device to the semicoke material inlet of fluid-bed combustion furnace from gained dust, or sends the emulsion zone weight of fluidized-bed gasification furnace back to
Newly reacted；
(3) semicoke material obtained by gasification reaction is from the overflow port discharge at the top of fluidized-bed gasification furnace emulsion zone, and is sent by material returning device
To the semicoke material inlet of fluid-bed combustion furnace；Emulsion zone in fluid-bed combustion furnace, semicoke material and the sky from bottom
Combustion reaction occurs for gas, generates the high-temperature flue gas that temperature is 900-950 DEG C；
The mass ratio for controlling the material of bottom air and semicoke material inlet is 1-1.2, makes semicoke material that completely burned occur；
Fluid-bed combustion furnace is normal pressure or pressurization operation, and pressure is 0.1-5MPa when pressurization is run；Running temperature is 900-950 DEG C；
(4) flue gas of fluid-bed combustion furnace discharge is sent again after being dusted by cyclone separator to discharge pipe, separating obtained powder
Dirt is returned to the semicoke material inlet of fluid-bed combustion furnace by material returning device, re-starts combustion reaction.
3. according to the method described in claim 2, it is characterized in that, the biomass dry powder refers to the dry powder of agricultural crop straw,
Its granularity is 10mm or less；The granularity of the coal dust is 8mm or less.
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