CN106247323B - A kind of chemical chain combustion apparatus and its method based on tower bubbling fluidized bed fuel reactor - Google Patents
A kind of chemical chain combustion apparatus and its method based on tower bubbling fluidized bed fuel reactor Download PDFInfo
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- CN106247323B CN106247323B CN201610825016.5A CN201610825016A CN106247323B CN 106247323 B CN106247323 B CN 106247323B CN 201610825016 A CN201610825016 A CN 201610825016A CN 106247323 B CN106247323 B CN 106247323B
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/02—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed
- F23C10/04—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone
- F23C10/08—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases
- F23C10/10—Fluidised bed combustion apparatus with means specially adapted for achieving or promoting a circulating movement of particles within the bed or for a recirculation of particles entrained from the bed the particles being circulated to a section, e.g. a heat-exchange section or a return duct, at least partially shielded from the combustion zone, before being reintroduced into the combustion zone characterised by the arrangement of separation apparatus, e.g. cyclones, for separating particles from the flue gases the separation apparatus being located outside the combustion chamber
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C10/00—Fluidised bed combustion apparatus
- F23C10/18—Details; Accessories
- F23C10/20—Inlets for fluidisation air, e.g. grids; Bottoms
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- 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)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
本发明为一种基于塔式鼓泡流化床燃料反应器的化学链燃烧的装置及其方法，该装置由空气反应器、空气旋风分离器、返料器、塔式燃料反应器、燃料旋风分离器和隔离器组成的一个循环回路；其方法在于塔式燃料反应器内燃料依次向上通过由多个独立布风隔板沿高度方向分隔成的各个小室，与氧化态载氧体进行深度氧化反应，转化为CO2和H2O排出，还原态载氧体经燃料旋风分离器和隔离器进入空气反应器进行载氧体再生反应，生成氧化态载氧体，经空气旋风分离器分离后，通过返料器进入燃料反应器；固体燃料在燃料反应器下部小室内进行气化反应后进行氧化反应。本装置及方法可以有效改善燃料反应器内气固流动状态，提高化学链燃烧效率。
The present invention relates to a device and method for chemical chain combustion based on a tower-type bubbling fluidized bed fuel reactor. A circulation loop composed of a separator and an isolator; the method is that the fuel in the tower fuel reactor passes upward in turn through each chamber divided by a plurality of independent air distribution baffles in the height direction, and carries out deep oxidation with the oxidized oxygen carrier. The reaction is converted into CO 2 and H 2 O and discharged. The reduced oxygen carrier enters the air reactor through the fuel cyclone separator and isolator for the oxygen carrier regeneration reaction to generate the oxidized oxygen carrier, which is separated by the air cyclone separator. , enter the fuel reactor through the return material; the solid fuel undergoes gasification reaction in the lower chamber of the fuel reactor and then undergoes oxidation reaction. The device and method can effectively improve the gas-solid flow state in the fuel reactor and improve the combustion efficiency of the chemical chain.
Description
Technical field
The present invention relates to a kind of devices and methods therefors of the burning chemistry chains of tower bubbling fluidized bed fuel reactor, specifically
Improve gas-solid admixture in fuel reactor to realize, inhibit bubble parameters, increases solid particle and stopped in fuel reactor
Time improves efficiency of combustion, completes chemical chain combustion apparatus and method that carbon dioxide is separated in combustion process.
Background technique
Burning chemistry chains are a kind of New combustion techniques, by oxygen carrier between air reactor and fuel reactor into
The alternate oxidation-reduction reaction of row, realizes the transmitting of oxygen, contacts so as to avoid fuel with the direct of air, completes turning sludge into fuel
Learn the conversion of energy, principle is: reduction-state oxygen carrier carries out oxidation reaction with air in air reactor and generates oxidation state load
Oxysome；The oxygen carrier of oxidation state enters fuel reactor, carries out reduction reaction with fuel, generates reduction-state oxygen carrier；Reduction-state
Oxygen carrier enters back into air reactor and carries out oxidation reaction, is recycled with this, to realize the burning of fuel and complete oxygen carrier
Regeneration.Wherein, the dry gas product of air reactor outlet only has N2With extra O2；The gaseous product of fuel reactor outlet
For CO2And H2O obtains high-purity CO after simply condensing and drying2, to realize CO2Interior separation.
Burning chemistry chains reactor must reach following design requirement: higher mass transfer ability, thus in fuel reactor
The high conversion for realizing fuel completes the regeneration of oxygen carrier, in certain temperature and pressure limit, oxygen carrier in air reactor
Body must have sufficiently fast chemical reaction rate；Higher heat-transfer capability can pass through oxygen carrier for the heat of air reactor
It is transmitted to fuel reactor, maintains heat required for the endothermic reaction of fuel reactor；Collaborating between two reactors is prevented,
Reduce CO2It is revealed from fuel reactor to air reactor；In the burning of solid fuel chemistry chain, flying dust and uncombusted solid can be made
Fluid fuel is efficiently separated with oxygen carrier.
During gaseous fuel burning chemistry chains, alternating oxygen of the oxygen carrier between air reactor and fuel reactor
Change-reduction reaction, fluidized state difference will lead to oxygen carrier granule and be sintered, and reduce the reactivity of oxygen carrier；On the other hand,
During burning chemistry chains in fuel reactor gaseous fuel transformation efficiency by oxygen carrier reactivity restriction, carry
The reactivity of oxysome is lower, and the combustable gas concentration of non-complete oxidation is higher in fuel reactor exit gas, leads to chemistry
Chain efficiency of combustion reduces.Solid fuel is first and gasifying medium in solid fuel chemistry chain combustion process, in fuel reactor
Gasification reaction is carried out, gasification product is oxidized the oxygen carrier oxidating of state, generates carbon dioxide and vapor.The oxidation of oxygen carrier is anti-
Answer rate much higher than reduction reaction rate, air reactor can satisfy requirement using flashing reactor.In fuel reactor,
It is compared with the reduction reaction of oxygen carrier, the gasification reaction of solid fuel is very slow, is the pass for controlling the rate of entire burning chemistry chains
Key process, it is necessary to take steps to improve residence time of the fuel in fuel reactor, to guarantee the abundant reaction of fuel；
Otherwise it has more subtle coke granule not to be gasified totally, fuel reactor is carried from by air-flow, leads to solid fuel
Learning chain efficiency of combustion reduces.In addition, in conventional bubbling fluidized bed reactor bubble presence, be unfavorable for gas-solid contact, reduce
The efficiency of reaction, needing to adopt an effective measure improves Gas-solid Flow Characteristics in bubbling fluidized bed.
Therefore, the transformation efficiency for how improving fuel reactor fuel guarantees good fluidized state, increases solid
Grain residence time in fuel reactor, is the critical issue for improving burning chemistry chains efficiency, and technology has extensive society
Benefit and prospects for commercial application.
Summary of the invention
Goal of the invention: in order to overcome the deficiencies in the prior art, the present invention is provided in a kind of raising fuel reactor
The transformation efficiency of fuel improves the devices and methods therefor of the burning chemistry chains of Gas-particle Flows state in fuel reactor.
A kind of the technical solution adopted by the present invention are as follows: burning chemistry chains dress based on tower bubbling fluidized bed fuel reactor
It sets, according to oxygen carrier flow direction successively by air reactor, vortex of air separator, material returning device, tower fuel reactor, combustion
The circular response device that material cyclone separator and isolator are composed in series；The tower fuel reactor is along gas flow direction
Several cells are separated by multiple independent cloth wind partitions, are interconnected between each cell.
The air reactor is fast fluidized bed reactor.
The tower fuel reactor is bubbling fluidized bed reactor.
The cloth wind partition includes porous cloth wind partition or blast cap cloth wind partition.
A kind of method of the chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor, fuel enter
Tower fuel reactor bottom passes through the oxygen carrier alternately oxygen between air reactor and tower fuel reactor respectively
The chemical energy conversion of fuel is realized in change-reduction process；Specific method the following steps are included:
1) oxidation reaction: gasification product or gaseous fuel and the oxidation state oxygen carrier granule in air reactor are under
Each cell of the tower fuel reactor is passed sequentially through upwards, carries out oxidation reaction, and oxidation state oxygen carrier granule is reduced
At reduction-state oxygen carrier granule, gaseous fuel or gasification product are oxidized and generate vapor and carbon dioxide, reduction-state oxygen carrier
Particle and vapor and carbon dioxide enter fuel cyclone separator together and carry out gas solid separation, vapor and carbon dioxide row
Out, the reduction-state oxygen carrier granule separated is entered in air reactor by isolator；The gasification product is solid
Fuel enters the small indoor fluidizing gas gasification reaction with entrance in tower fuel reactor bottom and obtains；The solid fuel is
Containing hydrocarbon solid fuel；The gaseous fuel is reducibility gas；
2) oxygen carrier regenerative response: into the reduction-state oxygen carrier granule in air reactor, with air reactor bottom
The air of entrance carries out oxidation reaction, generates oxidation state oxygen carrier granule, completes the regeneration of oxygen carrier, the oxidation state oxygen carrier
Particle brings vortex of air separator by air-flow, carries out gas solid separation, the oxygen denuded air discharge after reaction, the oxidation separated
State oxygen carrier granule reenters tower fuel reactor by material returning device and carries out reduction reaction.
The gas of residual solid fuel or non-complete oxidation that the small interior in tower fuel reactor bottom is not gasified totally
Fluid fuel is entered in tower fuel reactor in one layer of cell by cloth wind partition, further progress gasification or oxidation reaction, most
It is converted into carbon dioxide and vapor eventually.
Reaction temperature in the air reactor is 850~1100 DEG C；Reaction temperature in the tower fuel reactor
Degree is 600~1000 DEG C.
The solid fuel includes coal, biomass, domestic sludge, and the gaseous fuel includes CO, H2、CH4。
The material returning device, tower fuel reactor and isolator add fluidizing gas, the fluidized gas by bottom respectively
Body is vapor and/or carbon dioxide gas.
The utility model has the advantages that a kind of chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor provided by the invention
And method, applicable fuel are not limited to solid fuel, oxygen carrier granule is with air-flow from bottom to up by tower fuel reactor
The each cell being separated by cloth wind partition constitutes a closed circulation by fuel reactor and air reactor；The present invention
Bed height by increasing tower fuel reactor stops in fuel reactor come the time of contact for increasing gas-solid and fuel
The time is stayed, but flowing can occur for bed height increase unevenly, plug flow section gushes the equal undesirable state of gas-solid mixings, therefore is
The present invention that solves the above problems use with multiple independent cloth wind partitions fuel reactor is divided into along short transverse it is several
The method of cell improves gas-solid mixing situation in fuel reactor, and flowing is made uniformly to reinforce reducibility gas and oxygen carrier
The contact of grain is conducive to improve fuel conversion；For solid fuel, invention increases solid fuels in fuel reactor
Residence time so that solid fuel sufficiently gasifies, gasification product is oxidized the oxygen carrier oxidating of state, generates carbon dioxide and water
Steam discharge, improves the transformation efficiency of fuel reactor fuel；In tower bubbling fluidized bed fuel reactor, along height side
It can guarantee that the stable operation of bubbling fluidized bed effectively inhibits bubble in reactor to multiple independent cloth wind partitions of arrangement
It grows up, makes to flow stable and uniform, reduce because bubbles burst causes the elutriation of coke granule, increase subtle coke granule in reactor
The interior residence time guarantees the efficiency of combustion of solid fuel chemistry chain burning；On the other hand, reduce in reaction process due to flowing
The case where unevenness sintering causes oxygen carrier reactivity to reduce, effectively improving flow regime prevents oxygen carrier sintering deactivation from helping
In being normally carried out for burning chemistry chains reaction, technology has extensive social benefit and prospects for commercial application.
Detailed description of the invention
Fig. 1 is the device of the invention structural schematic diagram.
Wherein there are air reactor 1, vortex of air separator 2, material returning device 3, tower fuel reactor 4, reduction-state oxygen carrier
Body particle 4.1, cloth wind partition 4.2, fuel cyclone separator 5, isolator 6.
Fig. 2 is the curve that indoor pressure tap the 4th small from the bottom up obtains in tower fuel reactor in embodiment 3.
Fig. 3 is the differential pressure curve figure in the entire tower fuel reactor of embodiment 3.
Specific embodiment
The present invention will be further explained with reference to the accompanying drawing.
It is as shown in Figure 1 a kind of chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor, including air
Reactor, vortex of air separator, material returning device, tower fuel reactor, fuel cyclone separator and isolator are sequentially connected in series group
At single cycle reaction unit.
Further, in the present invention, the tower fuel reactor is by several independent cloth wind partitions along height side
To being separated into several cells, cloth wind partition can be used the cloth wind of the structure types such as porous cloth wind partition or blast cap cloth wind partition every
Plate, several cells are sequentially communicated by the cloth wind partition.The effect of cloth wind partition is to make tower fuel anti-under high bed
It answers Gas-particle Flows in device uniform, while supporting each small indoor particulate bed material of fuel reactor.
In the present invention, the air reactor 1 passes through vortex of air separator 2 and material returning device 3 and the tower fuel
Reactor 4 connects；The outlet on 1 top of air reactor is connected with the upper feed inlet of the vortex of air separator 2,
The lower part discharge port of the vortex of air separator 2 is connected with the top feed mouth of the material returning device 3.The tower fuel is anti-
Device 4 is answered to connect by fuel cyclone separator 5 and isolator 6 with the air reactor 1；In the tower fuel reactor 4
The outlet in portion is connected with the upper feed inlet of the fuel cyclone separator 5, the lower part discharging of the fuel cyclone separator 5
Mouth is connect with the top feed mouth of the isolator 6.The outlet of the isolator 6 is fed with the lower part of the air reactor 1
Mouth is connected.The outlet of material returning device 3 is connected with the lower part oxygen carrier import of the tower fuel reactor 4.Isolator 6
Effect is will to be transported in air reactor 1 from the granule materials that fuel separator 5 separates by fluidised mode, every
Centre from device 6 is provided with partition, plays the role of isolation, prevents the gas anti-channeling in air reactor 1 from dividing to fuel whirlwind
From in device 5, gas-solid disngaging efficiency is reduced；The fluidizing gas that isolator gas feed enters uses vapor or CO2, such ability
Guarantee that the gas that fuel reactor 4 is discharged is CO2And vapor, do not contain other gases.The effect of material returning device 3 with isolator 6,
Equally play the role of isolation to prevent collaborating.Material returning apparatus of fluidized bed can be used in material returning device and isolator.
A method of the chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor, gas or solid fuel
It is anti-in the air reactor and the tower fuel by oxygen carrier into the bottom cell of the tower fuel reactor
Alternating oxidation-reduction process between device is answered, realizes the chemical energy conversion of fuel, the oxygen carrier includes Ni-based, iron-based, copper
The various oxygen carrier granules such as base；The fuel is solid fuel or gaseous fuel；The solid fuel is to fire containing hydrocarbon solid
Material, including coal, biomass, domestic sludge；The gaseous fuel is reducibility gas, including CO, H2And CH4Deng containing hydrocarbon
Gaseous fuel；Specific method the following steps are included:
1) gasification reaction: the solid fuel enters the tower fuel reactor bottom cell, is carried by air-flow, upwards
By each cell of tower fuel reactor, gasification reaction is carried out, generates gasification product.The gaseous fuel without this step,
Tower fuel reactor bottom is directly entered to be reacted with oxidation state oxygen carrier；
2) oxidation reaction: the gasification product and come from sky that the gaseous fuel or the solid fuel are generated by step 1)
The oxidation state oxygen carrier granule of solid/liquid/gas reactions device by each cell of tower fuel reactor, carries out oxidation reaction, oxygen upwards in turn
Change state oxygen carrier granule and be reduced into reduction-state oxygen carrier granule, gaseous fuel or gasification product, which are oxidized, generates vapor and two
Carbonoxide, reduction-state oxygen carrier granule and vapor and carbon dioxide enter fuel cyclone separator together and carry out gas solid separation,
The vapor and carbon dioxide are discharged by flue gas exhaust pipe, and the reduction-state oxygen carrier granule separated passes through isolation
Device enters in the air reactor；
3) oxygen carrier regenerative response: the reduction-state oxygen carrier granule generated through step 2) in tower fuel reactor into
Enter in the air reactor, carry out oxidation reaction with the air entered in air reactor, generate oxidation state oxygen carrier granule,
Realize the regeneration of oxygen carrier, the oxidation state oxygen carrier granule is divided by the air reactor transverse tube into the vortex of air
From device, gas solid separation is carried out, the oxygen denuded air after reaction is discharged from air exhaust duct, the oxidation state oxygen carrier separated
Particle enters the tower fuel reactor by material returning device.
Further, in the present invention, in step 1), the residual that is not gasified totally in the tower fuel reactor bottom
Solid fuel drives with fluidizing gas, is entered in tower fuel reactor in one layer of cell, further by the cloth wind partition
Gasification reaction is carried out, the gasification product of generation is reacted with the oxidation state oxygen carrier granule in the fuel reactor, is converted into two
Carbonoxide and vapor.
Further, in the present invention, in step 1) and step 2), non-complete oxidation in the tower fuel reactor
Gaseous fuel is entered in tower fuel reactor in one layer of cell by the cloth wind partition, and further progress oxidation reaction turns
Turn to carbon dioxide and vapor.
Further, in the present invention, the reaction temperature in the air reactor is 850~1100 DEG C, described tower
Reaction temperature in fuel reactor is 600~1000 DEG C；The air reactor is fast fluidized bed reactor, described tower
Fuel reactor is bubbling fluidized bed reactor.
Further, in the present invention, the material returning device, tower fuel reactor and isolator pass through respectively is arranged in phase
Material returning device fluidisation gas inlet, fuel reactor fluidisation gas inlet and the isolator fluidisation gas inlet for the device bottom answered add
Add fluidizing gas, the fluidizing gas is vapor and/or carbon dioxide gas.
Embodiment 1
A kind of method of the chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor be fuel it is not direct and
Air catalytic combustion, fuel are gaseous fuel.Gaseous fuel is reducibility gas, including CO, H2And CH4Deng containing hydrocarbon gas
Fluid fuel.Gaseous fuel enters in tower fuel reactor 4, by oxygen carrier in air reactor 1 and tower fuel reactor 4
Between alternate cycles carry out oxidation-reduction reaction, realize the burning of gaseous fuel, the oxygen carrier includes Ni-based, iron-based, copper
The various oxygen carrier granules such as base；Specific method the following steps are included:
1) oxidation reaction: fluidizing gas enters through the fuel reactor fluidisation gas inlet of tower 4 bottom of fuel reactor
In tower fuel reactor 4, gaseous fuel enters tower fuel reaction through the fuel inlet of tower 4 bottom sides of fuel reactor
In device 4, tower fuel reactor 4 be bubbling fluidization bed structure, gaseous fuel in tower fuel reactor 4 with come from air it is anti-
It answers the oxidation state oxygen carrier granule of device 1 to carry out oxidation reaction, generates reduction-state oxygen carrier granule 4.1 and vapor and titanium dioxide
Carbon, the oxidation state oxygen carrier granule not being reduced or the oxygen deprivation state oxygen carrier granule not being completely reduced pass through cloth wind partition 4.2
One layer of cell continues oxidation reaction on into tower fuel reactor 4；The final product of oxidation reaction in tower fuel reactor 4
Including reduction-state oxygen carrier granule 4.1 and vapor and carbon dioxide, enter fuel whirlwind point together through fuel reactor transverse tube
Gas solid separation is carried out from device 5, vapor and carbon dioxide are discharged by flue gas exhaust pipe, and reduction-state oxygen carrier granule 4.1 is through firing
The dipleg of material cyclone separator enters in isolator 6, the fluidisation through entering from the isolator fluidisation gas inlet of 6 bottom of isolator
After the fluidization of gas, it is discharged again through isolator discharge nozzle in the reduction-state oxygen carrier granule 4.1 of flow-like, it is anti-into air
Answer progress step 2) i.e. oxygen carrier regenerative response in device 1；
Preferably, in step 1), the small indoor oxidation state not being reduced on a small quantity in tower 4 lower part of fuel reactor or middle part is carried
Oxysome particle and the oxygen deprivation state oxygen carrier granule not being completely reduced are entered in tower fuel reactor 4 by cloth wind partition 4.2
In one layer of cell, with gaseous fuel further progress oxidation reaction, it is converted into carbon dioxide and vapor, improves the burning of fuel
Efficiency；
Likewise, the gaseous fuel of a small amount of non-complete oxidation passes through cloth wind partition in tower fuel reactor 4 in step 1)
4.2 enter in tower fuel reactor 4 in one layer of cell, further with the oxidation state oxygen carrier granule 1.2 in fuel reactor 4
Oxidation reaction is carried out, carbon dioxide and vapor is converted into, improves the efficiency of combustion of fuel；
2) oxygen carrier regenerative response: the reduction-state oxygen carrier granule 4.1 generated in tower fuel reactor 4 through step 1) into
Enter in air reactor 1, the bottom of air reactor 1 is equipped with air intlet, and reduction-state oxygen carrier granule 4.1 and entrance air are anti-
It answers the air of device 1 to carry out oxygen carrier regenerative response, generates oxidation state oxygen carrier granule, oxidation state oxygen carrier granule is through air reaction
Device transverse tube enters vortex of air separator 2, carries out gas solid separation, and the oxygen denuded air after reaction, which passes through, is located at vortex of air separator 2
Top air exhaust duct discharge；Dipleg of the oxidation state oxygen carrier granule separated then through vortex of air separator is by weight
Power effect freely falls through into 3 top of material returning device, the fluidized gas through entering from the reactor fluidisation gas inlet of 3 bottom of material returning device
After the fluidization of body, it is discharged again through material returning device discharge nozzle in the oxidation state oxygen carrier granule of flow-like, it is anti-into tower fuel
4 bottom of device is answered, next round oxidation reaction is carried out, carries out next round circular response；
Reaction temperature in air reactor 1 is 850~1100 DEG C of conditions of high temperature, the reaction in tower fuel reactor 4
Temperature is temperature state in 600~1000 DEG C, carries out heat biography by oxygen carrier granule between air reactor and fuel reactor
It passs.Air reactor 1 is fast fluidized bed reactor, and tower fuel reactor 4 is bubbling fluidized bed reactor.
Material returning device 3, tower fuel reactor 4 and isolator 6 pass through the material returning device that corresponding device bottom is arranged in respectively
Fluidisation gas inlet, fuel reactor fluidisation gas inlet and isolator fluidisation gas inlet add fluidizing gas, fluidizing gas
Effect be the oxygen carrier granule fluidisation allowed in material returning device 3, tower fuel reactor 4 and isolator 6 so that particle has fluid
Characteristic, fluidizing gas be vapor and/or carbon dioxide gas.
Embodiment 2
A kind of method of the chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor be fuel it is not direct and
Air catalytic combustion, fuel are solid fuel.Solid fuel is containing hydrocarbon solid fuel, including coal, biomass, life dirt
Mud.Solid fuel enters in tower fuel reactor 4, through oxygen carrier between air reactor 1 and tower fuel reactor 4
Oxidation-reduction reaction is carried out to alternate cycles, realizes the burning of solid fuel, the oxygen carrier includes Ni-based, iron-based, copper-based etc.
Various oxygen carrier granules；Specific method the following steps are included:
1) gasification reaction: fluidizing gas enters through the fuel reactor fluidisation gas inlet of tower 4 bottom of fuel reactor
In tower fuel reactor 4, solid fuel enters tower fuel reaction through the fuel inlet of tower 4 bottom sides of fuel reactor
In device 4, tower fuel reactor 4 is bubbling fluidization bed structure, and solid fuel carries out gasification reaction with fluidizing gas first, is generated
Gasification product, gasification product and the solid fuel particle for failing gasification are anti-into tower fuel by the cloth wind partition 4.2 of setting
Answer one layer of cell on device 4；
2) oxidation reaction: solid fuel by step 1) generate gasification product in tower fuel reactor 4 with come from
The oxidation state oxygen carrier granule of air reactor 1 carries out oxidation reaction, generates reduction-state oxygen carrier granule 4.1 and vapor and two
Carbonoxide, the oxidation state oxygen carrier granule not being reduced or the oxygen deprivation state oxygen carrier granule not being completely reduced pass through cloth wind partition
4.2, which enter tower 4 upper layer of fuel reactor, continues oxidation reaction, and tower 4 middle part of fuel reactor or bottom are set as gasification-
Oxidation reaction layer；The final product of oxidation reaction includes reduction-state oxygen carrier granule 4.1 and vapor in tower fuel reactor 4
And carbon dioxide, enter fuel cyclone separator 5 together through fuel reactor transverse tube and carries out gas solid separation, vapor and titanium dioxide
Carbon is discharged by flue gas exhaust pipe, and reduction-state oxygen carrier granule 4.1 enters in isolator 6 through the dipleg of fuel cyclone separator,
After the fluidization of fluidizing gas through entering from the isolator fluidisation gas inlet of 6 bottom of isolator, in the reduction of flow-like
State oxygen carrier granule is discharged through isolator discharge nozzle again, into progress step 3) i.e. oxygen carrier regenerative response in air reactor 1；
Preferably, in step 1), the remnants not being gasified totally on a small quantity in tower 4 bottom of fuel reactor or lower chamber are solid
The subtle coke granule of fluid fuel carries away with fluidizing gas drive, enters tower fuel reactor 4 by cloth wind partition 4.2
In upper one layer of cell, further progress gasification reaction, the gasification product and the oxidation state oxygen carrier in fuel reactor 4 of generation
Grain further progress oxidation reaction, is converted into carbon dioxide and vapor, improves the efficiency of combustion of fuel；
Likewise, the small indoor oxidation state not being reduced on a small quantity in tower 4 lower part of fuel reactor or middle part carries in step 2)
Oxysome particle and the oxygen deprivation state oxygen carrier granule not being completely reduced are entered in tower fuel reactor 4 by cloth wind partition 4.2
In one layer of cell, with gasification product further progress oxidation reaction, it is converted into carbon dioxide and vapor, improves the burning of fuel
Efficiency；
Likewise, the gasification product of a small amount of non-complete oxidation is through cloth in tower fuel reactor 4 in step 1) and step 2)
Wind partition 4.2 enters in tower fuel reactor 4 in one layer of cell, with the oxidation state oxygen carrier granule in fuel reactor 4
Further progress oxidation reaction, is converted into carbon dioxide and vapor, improves the efficiency of combustion of fuel；
3) oxygen carrier regenerative response: the reduction-state oxygen carrier granule 4.1 generated in tower fuel reactor 4 through step 2) into
Enter in air reactor 1, the bottom of air reactor 1 is equipped with air intlet, and reduction-state oxygen carrier granule 4.1 and entrance air are anti-
It answers the air of device 1 to carry out oxygen carrier regenerative response, generates oxidation state oxygen carrier granule, oxidation state oxygen carrier granule is through air reaction
Device transverse tube enters vortex of air separator 2, carries out gas solid separation, and the oxygen denuded air after reaction, which passes through, is located at vortex of air separator 2
Top air exhaust duct discharge；Dipleg of the oxidation state oxygen carrier granule separated then through vortex of air separator is by weight
Power effect freely falls through into 3 top of material returning device, the fluidized gas through entering from the reactor fluidisation gas inlet of 3 bottom of material returning device
After the fluidization of body, it is discharged again through material returning device discharge nozzle in the oxidation state oxygen carrier granule of flow-like, it is anti-into tower fuel
4 bottom of device is answered, next round gasification, oxidation reaction are carried out, carries out next round circular response；
In addition, the part dust after solid fuel gasifies in tower 4 lower chamber of fuel reactor passes through fuel reaction
The cloth wind partition 4.2 of device 4 enters tower 4 middle and upper part cell of fuel reactor, is carried away by the gas in fuel reactor 4,
It is discharged together by the flue gas exhaust pipe of fuel cyclone separator 5；
Reaction temperature in air reactor 1 is 850~1100 DEG C of conditions of high temperature, the reaction in tower fuel reactor 4
Temperature is temperature state in 600~1000 DEG C, carries out heat biography by oxygen carrier granule between air reactor and fuel reactor
It passs.Air reactor 1 is fast fluidized bed reactor, and tower fuel reactor 4 is bubbling fluidized bed reactor.
Material returning device 3, tower fuel reactor 4 and isolator 6 pass through the material returning device that corresponding device bottom is arranged in respectively
Fluidisation gas inlet, fuel reactor fluidisation gas inlet and isolator fluidisation gas inlet add fluidizing gas, fluidizing gas
Effect be the oxygen carrier granule fluidisation allowed in material returning device 3, tower fuel reactor 4 and isolator 6 so that particle has fluid
Characteristic, fluidizing gas be vapor and/or carbon dioxide gas.
Embodiment 3
Oxygen carrier granule is replaced to carry out cold conditions circulation experiment at room temperature with quartz sand, quartz sand particle size 0.1-0.3mm,
Four independent cloth wind partitions are set along short transverse in the tower fuel reactor of middle use, tower fuel reactor is separated
For five cells, find that pressure fluctuates in a certain range over time, mean value by the bed pressure drop curve of Fig. 2, Fig. 3
Stablize near some definite value.This shows that Matter Transfer is in good condition in fluidized bed, in air reactor and fuel reactor
Material reaches dynamic equilibrium.And in cyclic process, do not observe that apparent plug flow and section are gushed in tower fuel reactor
Phenomenon, uniformly, gas-solid mixing is good for flowing.
To sum up, the chemical chain combustion apparatus and method of the present invention based on tower bubbling fluidized bed fuel reactor,
It can control bubble size, guarantee that flowing uniformly, improves gas-solid mixing, promote gas-solid reaction, it is anti-in fuel to increase solid particle
It answers the device residence time, improves the efficiency of combustion of chemistry of fuel chain, technology has extensive social benefit and prospects for commercial application.
It illustrates, the above is only a preferred embodiment of the present invention, it should be pointed out that: for the general of the art
For logical technical staff, various improvements and modifications may be made without departing from the principle of the present invention, these improve and
Retouching also should be regarded as protection scope of the present invention.
Claims (8)
1. a kind of chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor, it is characterised in that: according to oxygen carrier
Flow direction is successively anti-by air reactor (1), vortex of air separator (2), material returning device (3), tower bubbling fluidization bed material
The circular response device for answering device (4), fuel cyclone separator (5) and isolator (6) to be composed in series；The tower bubbling fluidization
Bed material reactor (4) is separated into several cells by multiple independent cloth wind partitions (4.2) along gas flow direction, each cell it
Between be interconnected.
2. the chemical chain combustion apparatus according to claim 1 based on tower bubbling fluidized bed fuel reactor, feature
Be: the air reactor (1) is fast fluidized bed reactor.
3. the chemical chain combustion apparatus according to claim 1 based on tower bubbling fluidized bed fuel reactor, feature
Be: the cloth wind partition includes porous cloth wind partition or blast cap cloth wind partition.
4. a kind of any chemical chain combustion apparatus based on tower bubbling fluidized bed fuel reactor of claim 1 ~ 3
Method, it is characterised in that: fuel enters tower bubbling fluidized bed fuel reactor (4) bottom, by oxygen carrier respectively in air
Alternately oxidation-reduction process between reactor (1) and tower bubbling fluidized bed fuel reactor (4), realizes fuel
Chemical energy conversion；Specific method the following steps are included:
1) oxidation reaction: gasification product or gaseous fuel and the oxidation state oxygen carrier granule in air reactor (1) are under
Each cell of the tower bubbling fluidized bed fuel reactor (4) is passed sequentially through upwards, carries out oxidation reaction, oxidation state oxygen carrier
Body particle is reduced into reduction-state oxygen carrier granule, and gaseous fuel or gasification product, which are oxidized, generates vapor and carbon dioxide,
Reduction-state oxygen carrier granule and vapor and carbon dioxide enter fuel cyclone separator (5) together and carry out gas solid separation, and water steams
Gas and carbon dioxide discharge, the reduction-state oxygen carrier granule separated are entered in air reactor (1) by isolator (6)；
The gasification product is that solid fuel enters the small indoor fluidisation with entrance in tower bubbling fluidized bed fuel reactor (4) bottom
Gas vaporization reacts to obtain；The solid fuel is containing hydrocarbon solid fuel；The gaseous fuel is reducibility gas；
2) oxygen carrier regenerative response: enter the reduction-state oxygen carrier granule in air reactor (1), with air reactor (1) bottom
The air that portion enters carries out oxidation reaction, generates oxidation state oxygen carrier granule, completes the regeneration of oxygen carrier, the oxidation state oxygen carrier
Body particle is brought into vortex of air separator (2) by air-flow, carries out gas solid separation, and the oxygen denuded air discharge after reaction separates
Oxidation state oxygen carrier granule by material returning device (3) reenter tower bubbling fluidized bed fuel reactor (4) restore it is anti-
It answers.
5. the method for the chemical chain combustion apparatus according to claim 4 based on tower bubbling fluidized bed fuel reactor,
It is characterized by: the residual solid fuel that the small interior in tower bubbling fluidized bed fuel reactor (4) bottom is not gasified totally
Or the gaseous fuel of non-complete oxidation enters tower upper one layer of bubbling fluidized bed fuel reactor (4) by cloth wind partition (4.2)
In cell, further progress gasification or oxidation reaction are eventually converted into carbon dioxide and vapor.
6. the method for the chemical chain combustion apparatus according to claim 4 based on tower bubbling fluidized bed fuel reactor,
It is characterized by: the reaction temperature in the air reactor (1) is 850~1100 DEG C；The tower bubbling fluidization bed material
Reaction temperature in reactor (4) is 600~1000 DEG C.
7. the method for the chemical chain combustion apparatus according to claim 4 based on tower bubbling fluidized bed fuel reactor,
It is characterized by: the solid fuel includes coal, biomass, domestic sludge, the gaseous fuel includes CO, H2、CH4。
8. the method for the chemical chain combustion apparatus according to claim 4 based on tower bubbling fluidized bed fuel reactor,
It is characterized by: the material returning device (3), tower bubbling fluidized bed fuel reactor (4) and isolator (6) are added by bottom respectively
Add fluidizing gas, the fluidizing gas is vapor and/or carbon dioxide gas.
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| CN107325846B (en) * | 2017-06-28 | 2019-10-11 | 大连理工大学 | Coal pyrolysis chemical looping gasification coupling process based on low-rank coal cascade utilization |
| CN108504389B (en) * | 2018-01-24 | 2024-04-09 | 江苏大学 | Chemical-looping combustion gasification coupling device and method for carbon-based fuel |
| CN108204593B (en) * | 2018-01-30 | 2024-05-07 | 广州环保投资集团有限公司 | Method for incinerating garbage by chemical chains |
| CN108548175B (en) * | 2018-05-30 | 2023-09-29 | 华中科技大学 | Coupling decarbonization and atmosphere isolation interconnected fluidized bed flexible feed back device |
| CN109181779B (en) * | 2018-09-14 | 2021-07-27 | 东南大学 | A chemical chain oil and gas co-production synergistic carbon dioxide reduction method |
| CN109945172B (en) * | 2019-02-25 | 2020-09-04 | 清华大学 | Chemical chain combustion device suitable for Class D fuel particles and Class A oxygen carrier particles |
| CN110115878A (en) * | 2019-04-17 | 2019-08-13 | 江苏大学 | A kind of the double circulation desulphurization system and sulfur method of the burning of solid fuel chemistry chain |
| CN110410781B (en) * | 2019-08-07 | 2020-11-10 | 哈尔滨理工大学 | Magnetic nanoscale oxygen carrier chemical chain reactor and use method thereof |
| CN110953578B (en) * | 2019-12-20 | 2024-06-11 | 东方电气集团东方锅炉股份有限公司 | Chemical chain reaction device with wide load regulation capability and control method thereof |
| CN113266819A (en) * | 2021-04-09 | 2021-08-17 | 东南大学 | Surge reactor device and surge characteristic characterization method |
| CN114031039A (en) * | 2021-12-17 | 2022-02-11 | 南京师范大学 | System and method for low temperature chemical chain desulfurization and co-production of sulfuric acid in H2S-containing synthesis gas |
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| CN101804314A (en) * | 2010-05-12 | 2010-08-18 | 新奥新能(北京)科技有限公司 | Fluidized bed reactor |
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