CN104848207B - The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation - Google Patents
The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation Download PDFInfo
- Publication number
- CN104848207B CN104848207B CN201510161670.6A CN201510161670A CN104848207B CN 104848207 B CN104848207 B CN 104848207B CN 201510161670 A CN201510161670 A CN 201510161670A CN 104848207 B CN104848207 B CN 104848207B
- Authority
- CN
- China
- Prior art keywords
- reactor
- fuel
- air
- oxygen carrier
- oxidation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 94
- 230000003647 oxidation Effects 0.000 title claims abstract description 75
- 239000004449 solid propellant Substances 0.000 title claims abstract description 46
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000002485 combustion reaction Methods 0.000 title claims description 27
- 239000000126 substance Substances 0.000 title claims description 16
- 239000000446 fuel Substances 0.000 claims abstract description 128
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 99
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 99
- 239000001301 oxygen Substances 0.000 claims abstract description 99
- 239000007789 gas Substances 0.000 claims abstract description 73
- 238000002309 gasification Methods 0.000 claims abstract description 72
- 239000008187 granular material Substances 0.000 claims abstract description 53
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000000463 material Substances 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 22
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 21
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 19
- 230000009467 reduction Effects 0.000 claims abstract description 18
- 238000006722 reduction reaction Methods 0.000 claims description 18
- 238000005243 fluidization Methods 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 9
- 239000002245 particle Substances 0.000 claims description 8
- 239000007787 solid Substances 0.000 claims description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 7
- 239000003546 flue gas Substances 0.000 claims description 7
- 230000009719 regenerative response Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 230000008859 change Effects 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 4
- 230000004044 response Effects 0.000 claims description 4
- 239000004215 Carbon black (E152) Substances 0.000 claims description 3
- 239000003245 coal Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 238000006479 redox reaction Methods 0.000 claims description 3
- 239000010802 sludge Substances 0.000 claims description 3
- 239000002028 Biomass Substances 0.000 claims description 2
- 210000000481 breast Anatomy 0.000 claims description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 1
- 239000002184 metal Substances 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000000571 coke Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 230000009257 reactivity Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000000567 combustion gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000000280 densification Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011946 reduction process Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
Classifications
-
- 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
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
The present invention is classified the devices and methods therefor of the burning chemistry chains of oxidation, the circulation loop that the device is made up of air reactor, vortex of air separator, fuel reactor, fuel cyclone separator, material returning device, gasification reactor and isolator for a kind of solid fuel；Its method is that solid fuel carries out gasification reaction in gasification reactor, the gaseous fuel of generation carries out oxidation reaction with poor oxidation state oxygen carrier, the week reduction gas incoming fuel reactor of generation, deep oxidation reaction is carried out with oxidation state oxygen carrier, is converted into carbon dioxide and vapor discharge；Reduction-state oxygen carrier and air carry out oxidation reaction in air reactor, generate oxidation state oxygen carrier granule, after being separated through vortex of air separator, incoming fuel reactor, it is poor oxidation state oxygen carrier by week reduction gas reduction, after being separated through fuel cyclone separator, gasification reactor is entered by material returning device, reduction-state oxygen carrier is reduced to by solid fuel gasification product, reduction-state oxygen carrier granule returns to air reactor by isolator and is regenerated as oxidation state oxygen carrier.
Description
Technical field
The present invention relates to a kind of device and method of the burning chemistry chains of solid fuel classification oxidation, solid is specially realized
Fuel staging is aoxidized, and improves efficiency of combustion, reaches the chemical chain combustion apparatus and method that carbon dioxide is separated in combustion process.
Background technology
Burning chemistry chains are a kind of New combustion techniques, and fuel does not burn directly with air contact, but passes through oxygen carrier
Alternating oxidation-reduction reaction between air reactor and fuel reactor, realizes the transfer of oxygen, completes fuel chemical energy
Conversion process, its principle is：Using metal oxide as oxygen carrier, the metal oxygen carrier of reduction-state is first in air reactor
Interior and air contact carries out oxidation reaction, generates the metal oxygen carrier of oxidation state, the oxygen in air is cemented out, then aoxidized
The metal oxygen carrier incoming fuel reactor of state, and gaseous fuel contact, carry out reduction reaction, by the metal oxygen carrier of oxidation state
Middle oxygen is cemented out, and the gaseous product of fuel reactor is carbon dioxide and vapor, and vapor is rejected after condensation and obtains pure
Carbon dioxide；Metal oxygen carrier after reduction returns to air reactor, and air carries out oxidation reaction, generation oxidation state
Metal oxygen carrier, completes the regeneration of oxygen carrier.
During gaseous fuel burning chemistry chains, the transformation efficiency of gaseous fuel is by oxygen carrier in fuel reactor
The restriction of reactivity, the reactivity of oxygen carrier is lower, the fuel gas of non-complete oxidation in fuel reactor exit gas
Concentration is higher；On the other hand, during burning chemistry chains metal oxygen carrier between air reactor and fuel reactor
Alternating oxidation-reduction reaction, can cause metal oxygen carrier granule surface to sinter, and the table of densification is formed in its particle surface
Layer, oxygen carrier reactivity reduction so that in fuel reactor exiting flue gas containing more non-complete oxidation can
Combustion gas body, causes the reduction of burning chemistry chains efficiency.
In solid fuel chemistry chain combustion process, solid fuel is gasified with gasifying medium first in fuel reactor
Reaction, generates gaseous fuel, then gaseous fuel reducing metal oxide oxygen carrier, generation carbon dioxide and vapor；And gold
The reduction process of category oxide oxygen carrier is compared, and the gasification reaction of solid fuel is slow, is whole solid fuel chemistry chain burning
Speed control link, has more trickle coke granule and is not gasified totally, be directly carried from fuel reactor by air-flow, lead
Cause the reduction of solid fuel chemistry chain efficiency of combustion.
Therefore, the oxidation efficiency of gaseous fuel in fuel reactor how is improved, trickle coke granule is reduced and is taken by air-flow
Lead out, be the key for realizing solid fuel chemistry chain combustion process, its technology has extensive social benefit and commercial Application
Prospect.
The content of the invention
Goal of the invention：In order to overcome the deficiencies in the prior art, the present invention provides a kind of improve in fuel reactor
The oxidation efficiency of gaseous fuel, and reduce the dress for the solid fuel chemistry chain burning that trickle coke granule is carried away by air-flow
Put and method.
Technical scheme：To achieve the above object, the technical solution adopted by the present invention is：
A kind of chemical chain combustion apparatus of solid fuel classification oxidation, including gasification reactor, air reactor and fuel
The circular response device that reactor is interconnected to form successively.
Further, in the present invention, the top of the gasification reactor is provided with gas vent, the fuel reactor
Bottom is provided with gas feed, and the bottom of the fuel reactor is additionally provided with air distribution plate, and the air distribution plate is provided with some blast caps, institute
Gas vent is stated with the gas feed by the air distribution plate to be connected.
Further, in the present invention, the air reactor passes through vortex of air separator and the fuel reactor
Connection；
It is arranged at the air reactor blast pipe on the air reactor top and the top of the vortex of air separator
Charging aperture is connected, and the bottom discharging opening of the vortex of air separator is connected by dipleg with the top of the fuel reactor
It is logical, centre or lower area that the dipleg is stretched into inside the fuel reactor.
Further, in the present invention, the fuel reactor passes through fuel cyclone separator and the gasification reactor
Connection；
It is arranged at the fuel reactor blast pipe on the top of fuel reactor 3 and the top of the fuel cyclone separator
Charging aperture is connected, and the bottom discharging opening of the fuel cyclone separator connects the bottom of the gasification reactor.
Further, in the present invention, the bottom discharging opening of the fuel cyclone separator is through material returning device and the gasification
The bottom of reactor is connected.
Further, in the present invention, the middle part or bottom of the gasification reactor are anti-by isolator and the air
The bottom of device is answered to be connected.
A kind of method of the chemical chain combustion apparatus of solid fuel classification oxidation, solid fuel enters the gasification reactor
In, carry out to alternate cycles between the air reactor, fuel reactor and gasification reactor aoxidizing by oxygen carrier-
Reduction reaction, the oxygen carrier includes oxidation state oxygen carrier granule, poor oxidation state oxygen carrier granule and reduction-state oxygen carrier granule；
Specific method comprises the following steps：
1) gasification-oxidation reaction：The solid fuel, which enters, carries out gasification reaction, the gas of generation in the gasification reactor
Fluid fuel carries out oxidation reaction in the gasification reactor with the poor oxidation state oxygen carrier granule from the fuel reactor,
Week reduction gas and reduction-state oxygen carrier granule are generated, the week reduction gas flows upwards out the gasification reactor, led to
The blast cap for crossing the air distribution plate enters the fuel reactor, and the reduction-state oxygen carrier granule enters the air reactor；
2) secondary oxidation reacts：Through step 1) in the week reduction gas incoming fuel reactor of generation, it is and described
The oxidation state oxygen carrier granule from air reactor carries out secondary oxidation reaction in fuel reactor, generates poor oxidation state oxygen carrier
Body particle and carbon dioxide and vapor, enter the fuel cyclone separator and carry out gas solid separation, the carbon dioxide together
Discharged with vapor by flue gas exhaust pipe, the poor oxidation state oxygen carrier granule separated enters described by material returning device
In gasification reactor；
3) oxygen carrier regenerative response：Through step 1 in gasification reactor) the reduction-state oxygen carrier granule of generation enters institute
State in air reactor, oxygen carrier regenerative response is carried out with the air in air inlet reactor, generate oxidation state oxygen carrier
Grain, the oxidation state oxygen carrier granule enters the vortex of air separator by the air reactor blast pipe, enters promoting the circulation of qi
Gu separation, the oxidation state oxygen carrier granule separated enters the fuel reactor.
Further, in the present invention, step 1) in, the residual solid fuel not being gasified totally in the gasification reactor
Driven with the week reduction gas, the blast cap through the air distribution plate enters the fuel reactor, further carries out gasified reverse
Should, the gaseous fuel of generation reacts with the oxidation state oxygen carrier granule in the fuel reactor, and oxidation is converted into carbon dioxide
And vapor.
Further, in the present invention, the reaction temperature in the air reactor is 850~1100 DEG C, the fuel
Reaction temperature in reactor and the gasification reactor is 600~950 DEG C；The air reactor and the fuel reactor
It is fluidized-bed reactor, the gasification reactor is spouted fluidized bed reactor.
Further, in the present invention, the material returning device, gasification reactor and isolator are corresponding by being arranged on respectively
Described in first class gas feed, the second fluidisation gas inlet and the 3rd fluidisation gas inlet addition fluidizing gas of device bottom
Fluidizing gas is vapor and/or carbon dioxide；The solid fuel is containing hydrocarbon solid fuel, including coal, life
Material, domestic sludge.
Beneficial effect：The chemical chain combustion apparatus and method for a kind of solid fuel classification oxidation that the present invention is provided, are used
The method of the burning chemistry chains of solid fuel classification oxidation so that solid fuel carries out sufficient gasified reverse with gasifying medium first
Should, generation gaseous fuel restores metal oxide oxygen carrier, generation carbon dioxide and vapor discharge, not only increases solid
Chemistry of fuel chain efficiency of combustion, while the oxidation efficiency and transformation efficiency of gaseous fuel in fuel reactor can be improved, is reduced thin
Micro- coke granule is carried away by air-flow, is the key for realizing solid fuel chemistry chain combustion process；On the other hand, reduce anti-
Cause the factor that the reactivity of oxygen carrier is reduced during answering, contribute to being normally carried out for reaction, it is ensured that burning chemistry chains are imitated
Rate, its technology has extensive social benefit and prospects for commercial application.
Brief description of the drawings
Fig. 1 is apparatus structure schematic diagram of the invention.
Wherein there are air reactor 1, air reactor blast pipe 1.1, oxidation state oxygen carrier granule 1.2, air intlet
1.3, vortex of air separator 2, dipleg 2.1, oxygen denuded air blast pipe 2.2, fuel reactor 3, fuel reactor blast pipe
3.1, poor oxidation state oxygen carrier 3.2, air distribution plate 3.3, blast cap 3.3.1, fuel cyclone separator 4, flue gas exhaust pipe 4.1, returning charge
Device 5, material returning device feed pipe 5.1, material returning device discharge nozzle 5.2, first class gas feed 5.3, gasification reactor 6, the second fluidisation
Gas feed 6.1, spouted pipe 6.2, reduction-state oxygen carrier granule 6.3, isolator 7, isolator feed pipe 7.1, isolator discharging
Pipe 7.2, the 3rd fluidisation gas inlet 7.3.
Embodiment
The present invention is further described below in conjunction with the accompanying drawings.
The chemical chain combustion apparatus of oxidation, including gasification reactor 6, air are classified for a kind of solid fuel as shown in Figure 1
The circular response device that the circulation loop that reactor 1 and fuel reactor 3 are interconnected to form successively is constituted.
The top of gasification reactor 6 is provided with gas vent, and the bottom of fuel reactor 3 is provided with gas feed, fuel reaction
The bottom of device 3 is additionally provided with air distribution plate 3.3, and air distribution plate 3.3 is provided with some blast cap 3.3.1, and gas vent and gas feed pass through
Air distribution plate 3.3 is connected.The effect of air distribution plate is to allow gas even into fuel reactor, while supporting in fuel reactor
Particulate bed material.
Air reactor 1 is connected by vortex of air separator 2 with fuel reactor 3；
The top of the air reactor blast pipe 1.1 and vortex of air separator 2 that are arranged at the top of air reactor 1 is fed
Mouth is connected, and the bottom discharging opening of vortex of air separator 2 is connected by dipleg 2.1 with the top of fuel reactor 3, dipleg
2.1 bosoms or lower area stretched into fuel reactor 3, in order to allow reactant to contact reducibility gas from bottom, fill
Divide reaction, prevent that have neither part nor lot in reaction just runs away from upper outlet spilling.
Fuel reactor 3 is connected by fuel cyclone separator 4 with gasification reactor 6；
The top of the fuel reactor blast pipe 3.1 and fuel cyclone separator 4 that are arranged at the top of fuel reactor 3 is fed
Mouth is connected, and the top of fuel cyclone separator 4 is flue gas exhaust pipe 4.1；The bottom discharging opening of fuel cyclone separator 4 is through returning
Glassware feed pipe 5.1 connects material returning device 5, then the bottom through the connection gasification reactor 6 of material returning device discharge nozzle 5.2.The work of material returning device 5
With being to be transported to the granule materials separated from fuel cyclone separator 4 in gasification reactor 6 by fluidised mode,
The centre of material returning device 5 is provided with dividing plate, plays a part of isolation, takes precautions against gas anti-channeling in gasification reactor 6 to fuel whirlwind
In separator 4, gas-solid disngaging efficiency is reduced；The fluidizing gas that first class gas feed 5.3 enters uses steam or CO2, this
Sample just can guarantee that the gas that fuel reactor 3 is discharged is CO2And steam, and do not contain other gases.
The middle part or bottom of gasification reactor 6 connect isolator 7 by isolator feed pipe 7.1, then are discharged through isolator
Pipe 7.2 is connected with the bottom of air reactor 1；The effect of isolator 7, with material returning device 5, is also to play buffer action.
Embodiment
A kind of method of the chemical chain combustion apparatus of solid fuel classification oxidation is solid fuel not direct and air contact
Burning, solid fuel is containing hydrocarbon solid fuel, including coal, biomass, domestic sludge.Solid fuel enters gasification reaction
In device 6, oxygen is carried out to alternate cycles between air reactor 1, fuel reactor 3 and gasification reactor 6 by oxygen carrier
Change-reduction reaction, realizes the combustion process of solid fuel, and oxygen carrier includes oxidation state oxygen carrier granule 1.2, poor oxidation state and carried
Oxysome particle 3.2 and reduction-state oxygen carrier granule 6.3；Specific method comprises the following steps：
1) gasification-oxidation reaction：When combustion occurs, the configured second in the bottom of gasification reactor 6 of fluidizing gas
Change gas feed 6.1 to enter in gasification reactor 6, the configured spouted pipe 6.2 in the middle of the bottom of gasification reactor 6 of solid fuel
Deliver into gasification reactor 6, gasification-oxidation reaction heap is being set as positioned at the middle part of gasification reactor 6 or bottom；Gasified reverse
It is spouted fluidized bed structure to answer device 6, and solid fuel carries out gasification reaction with fluidizing gas first, and the gaseous fuel of generation is described
Oxidation reaction is carried out with the poor oxidation state oxygen carrier granule 3.2 from the fuel reactor 3 in gasification reactor 6, is generated weak
Reducibility gas and reduction-state oxygen carrier granule 6.3, week reduction gas flow upwards out gasification reactor 6, pass through air distribution plate 3.3
Blast cap 3.3.1 incoming fuels reactor 3 in carry out step 2) be secondary oxidation reaction；Reduction-state oxygen carrier granule 6.3 through every
Enter from device feed pipe 7.1 in isolator 7, the stream through entering from the 3rd fluidisation gas inlet 7.3 for being arranged at the bottom of isolator 7
After the fluidization for changing gas, discharge, enter through isolator discharge nozzle 7.2 again in the reduction-state oxygen carrier granule 6.3 of flow-like
Step 3 is carried out in air reactor 1) it is oxygen carrier regenerative response；
It is preferred that, step 1) in, the trickle coke of a small amount of residual solid fuel not being gasified totally in gasification reactor 6
Grain drives carrying to go out with week reduction gas, in the blast cap 3.3.1 incoming fuels reactor 3 through air distribution plate 3.3, further enters
Row gasification reaction, the gaseous fuel of generation further carries out aoxidizing instead with the oxidation state oxygen carrier granule 1.2 in fuel reactor 3
Should, oxidation is converted into carbon dioxide and vapor, improves the efficiency of combustion of gaseous fuel；
Likewise, step 1) in, the gaseous fuel of a small amount of non-complete oxidation is with week reduction gas band in gasification reactor 6
It is dynamic to carry away, the blast cap 3.3.1 incoming fuels reactor 3 through air distribution plate 3.3, with the oxidation state oxygen carrier in fuel reactor 3
Body particle 1.2 further carries out oxidation reaction, and oxidation is converted into carbon dioxide and vapor, improves the burning effect of gaseous fuel
Rate；
2) secondary oxidation reacts：Have oxidation state oxygen carrier granule 1.2 in fuel reactor 3, through step 1) generation it is weak
In reducibility gas incoming fuel reactor (3), with the oxidation state oxygen carrier from air reactor 1 in fuel reactor 3
Grain 1.2 carries out secondary oxidation reactions, generates poor oxidation state oxygen carrier granule 3.2 and carbon dioxide and vapor, carbon dioxide and
Vapor carries poor oxidation state oxygen carrier granule 3.2 and enters the fuel cyclone separator 4 together, carries out gas solid separation, dioxy
Change carbon and vapor is discharged by flue gas exhaust pipe 4.1, the material returning device feed pipe of poor oxidation state oxygen carrier granule 3.2 separated
5.1 fall through into by material returning device 5, from the fluidized gas for the entrance of first class gas feed 5.3 for being arranged at the bottom of material returning device 5
Body plays fluidization to poor oxidation state oxygen carrier granule 3.2, carries and is discharged together through material returning device discharge nozzle 5.2, into gas
Change gasification-oxidation reaction heap in reactor 6, carry out gasification-oxidation reaction of next round, carry out next round circular response；
3) oxygen carrier regenerative response：Through step 1 in gasification reactor (6)) the reduction-state oxygen carrier granule 6.3 of generation
In air inlet reactor 1, the bottom of air reactor 1 is provided with air intlet 1.3, and reduction-state oxygen carrier granule 6.3 is with entering
Air in air reactor 1 carries out oxygen carrier regenerative response, oxidation generation oxidation state oxygen carrier granule 1.2, oxidation state oxygen carrier
Body particle 1.2 is carried away by air-flow, enters empty by the air reactor blast pipe 1.1 located at the top of air reactor 1
Cyclonic wind separator 2, carries out gas solid separation, and reacted oxygen denuded air passes through the oxygen deprivation positioned at the top of vortex of air separator 2
Air exhaust duct 2.2 is discharged；The oxidation state oxygen carrier granule 1.2 separated is then free by Action of Gravity Field through dipleg 2.1
The bottom of fuel reactor 3 is fallen through into, into next round reaction.
In addition, a part of dust after solid fuel gasifies in gasification reactor 6 follows reduction-state oxygen carrier granule 6.3
Entered by isolator 7 in air reactor 1, carried away, separated by vortex of air by the gas in air reactor 1
The oxygen denuded air blast pipe 2.2 of device 2 is discharged；Another part dust is carried by the gas of gasification reactor 6 passes through fuel reactor 3
The incoming fuel reactor 3 of air distribution plate 3.3, carried away by the gas in fuel reactor 3, pass through fuel cyclone separator 4
Flue gas exhaust pipe 4.1 discharge together；
Reaction temperature in air reactor 1 is 850~1100 DEG C of conditions of high temperature, fuel reactor 3 and gasification reactor 6
In reaction temperature be 600~950 DEG C in temperature state, between air reactor, fuel reactor and gasification reactor by carry
Oxysome particle carries out heat transfer.Air reactor 1 and fuel reactor 3 are fluidized-bed reactor, and gasification reactor 6 is spray
Fluidized bed reactor.
Material returning device 5, gasification reactor 6 and isolator 7 are respectively by being arranged on the first class gas of corresponding device bottom
Body import 5.3, the second fluidisation gas inlet 6.1 and the 3rd fluidisation gas inlet 7.3 addition fluidizing gas, the effect of fluidizing gas
It is that the oxygen carrier granule allowed in material returning device 5, gasification reactor 6 and isolator 7 is fluidized so that particle has the characteristic of fluid, stream
It is vapor and/or carbon dioxide to change gas.
Described above is only the preferred embodiment of the present invention, it should be pointed out that：For the ordinary skill people of the art
For member, under the premise without departing from the principles of the invention, some improvements and modifications can also be made, these improvements and modifications also should
It is considered as protection scope of the present invention.
Claims (7)
1. a kind of chemical chain combustion apparatus of solid fuel classification oxidation, it is characterised in that：Including gasification reactor (6), air
The circular response device that reactor (1) and fuel reactor (3) are interconnected to form successively；The top of the gasification reactor (6)
Portion is provided with gas vent, and the bottom of the fuel reactor (3) is provided with gas feed, and the bottom of the fuel reactor (3) is also
Provided with air distribution plate (3.3), the air distribution plate (3.3) is provided with some blast caps (3.3.1), and the gas vent and the gas enter
Mouth is connected by the air distribution plate (3.3)；
The air reactor (1) is connected by vortex of air separator (2) with the fuel reactor (3)；It is arranged at described
The air reactor blast pipe (1.1) on air reactor (1) top and the upper feed inlet phase of the vortex of air separator (2)
Connection, the bottom discharging opening of the vortex of air separator (2) passes through dipleg (2.1) and the top of the fuel reactor (3)
It is connected, the dipleg (2.1) stretches into the fuel reactor (3) bosom or lower area；
The fuel reactor (3) is connected by fuel cyclone separator (4) with the gasification reactor (6)；It is arranged at described
The fuel reactor blast pipe (3.1) on fuel reactor (3) top and the upper feed inlet phase of the fuel cyclone separator (4)
Connection, the bottom discharging opening of the fuel cyclone separator (4) connects the bottom of the gasification reactor (6).
2. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, it is characterised in that：The fuel
The bottom discharging opening of cyclone separator (4) is connected through material returning device (5) with the bottom of the gasification reactor (6).
3. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, it is characterised in that：The gasification
The middle part or bottom of reactor (6) are connected by isolator (7) with the bottom of the air reactor (1).
4. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, it is characterised in that：Gu
Fluid fuel enters in the gasification reactor (6), gentle in the air reactor (1), fuel reactor (3) by oxygen carrier
Oxidation-reduction reaction is carried out to alternate cycles between change reactor (6), the oxygen carrier includes oxidation state oxygen carrier granule
(1.2), poor oxidation state oxygen carrier granule (3.2) and reduction-state oxygen carrier granule (6.3)；Specific method comprises the following steps：
1) gasification-oxidation reaction：The solid fuel, which enters, carries out gasification reaction, the gas of generation in the gasification reactor (6)
Fluid fuel enters in the gasification reactor (6) with the poor oxidation state oxygen carrier granule (3.2) from the fuel reactor (3)
Row oxidation reaction, generation week reduction gas and reduction-state oxygen carrier granule (6.3), the week reduction gas flow upwards out institute
Gasification reactor (6) is stated, the fuel reactor (3) is entered by the blast cap (3.3.1) of the air distribution plate (3.3), it is described to go back
Ortho states oxygen carrier granule (6.3) enters the air reactor (1)；
2) secondary oxidation reacts：Through step 1) generation the week reduction gas incoming fuel reactor (3) in, with the combustion
Expect that the oxidation state oxygen carrier granule (1.2) from air reactor (1) carries out secondary oxidation reaction in reactor (3), generates poor
Oxidation state oxygen carrier granule (3.2) and carbon dioxide and vapor, carry out gas-solid into the fuel cyclone separator (4) together
Separation, the carbon dioxide and vapor are discharged by flue gas exhaust pipe (4.1), the poor oxidation state oxygen carrier separated
Particle (3.2) is entered in the gasification reactor (6) by material returning device (5)；
3) oxygen carrier regenerative response：Through step 1 in gasification reactor (6)) the reduction-state oxygen carrier granule (6.3) of generation enters
Enter in the air reactor (1), oxygen carrier regenerative response, generation oxidation are carried out with the air in air inlet reactor (1)
State oxygen carrier granule (1.2), the oxidation state oxygen carrier granule (1.2) is entered by the air reactor blast pipe (1.1)
The vortex of air separator (2), carries out gas solid separation, and the oxidation state oxygen carrier granule (1.2) separated enters institute
State fuel reactor (3).
5. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 4, it is characterised in that：Step
It is rapid 1) in, the residual solid fuel not being gasified totally in the gasification reactor (6) drives with the week reduction gas, through institute
The blast cap (3.3.1) for stating air distribution plate (3.3) enters the fuel reactor (3), further carries out gasification reaction, the gas of generation
Fuel reacts with the oxidation state oxygen carrier granule (1.2) in the fuel reactor (3), and oxidation is converted into carbon dioxide and water steams
Gas.
6. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 4, it is characterised in that：Institute
It is 850~1100 DEG C to state the reaction temperature in air reactor (1), the fuel reactor (3) and the gasification reactor (6)
In reaction temperature be 600~950 DEG C；The air reactor (1) and the fuel reactor (3) are fluidized-bed reaction
Device, the gasification reactor (6) is spouted fluidized bed reactor.
7. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 4, it is characterised in that：Institute
Material returning device (5), gasification reactor (6) and isolator (7) are stated respectively by being arranged on the first class gas of material returning device (5) bottom
3rd fluidized gas of import (5.3), second fluidisation gas inlet (6.1) of gasification reactor (6) bottom and isolator (7) bottom
Fluidizing gas is added in body import (7.3), and the fluidizing gas is vapor and/or carbon dioxide；The solid fuel is
Containing hydrocarbon solid fuel, including coal, biomass, domestic sludge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510161670.6A CN104848207B (en) | 2015-04-07 | 2015-04-07 | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510161670.6A CN104848207B (en) | 2015-04-07 | 2015-04-07 | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104848207A CN104848207A (en) | 2015-08-19 |
| CN104848207B true CN104848207B (en) | 2017-09-01 |
Family
ID=53848053
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510161670.6A Expired - Fee Related CN104848207B (en) | 2015-04-07 | 2015-04-07 | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104848207B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110923010A (en) * | 2019-12-10 | 2020-03-27 | 中国科学院工程热物理研究所 | Coal staged gasification method and device based on chemical looping combustion |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106765065A (en) * | 2016-11-30 | 2017-05-31 | 东南大学 | A kind of burning device of circulating fluidized bed and combustion method based on tower bubbling reactor |
| 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 |
| CN109054900B (en) * | 2018-08-17 | 2020-12-29 | 新奥科技发展有限公司 | Coal gasification method and system |
| CN110864280B (en) * | 2018-08-28 | 2021-05-04 | 国家能源投资集团有限责任公司 | Reactor and apparatus for burning carbonaceous solid fuel and method for burning carbonaceous solid fuel |
| CN109282279B (en) * | 2018-09-05 | 2019-10-18 | 东南大学 | A kind of regenerated burning chemistry chains air reactor of reinforcing oxygen carrier oxidating |
| 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 |
| CN110953578A (en) * | 2019-12-20 | 2020-04-03 | 东方电气集团东方锅炉股份有限公司 | Chemical-looping reaction device with wide load regulation capacity and control method thereof |
| CN113513751B (en) * | 2021-03-30 | 2024-01-05 | 江苏大学 | Chemical-looping combustion directional desulfurization process and device coupled with microwave technology |
| CN113266819A (en) * | 2021-04-09 | 2021-08-17 | 东南大学 | Surge reactor device and surge characteristic characterization method |
| CN113834897B (en) * | 2021-08-16 | 2023-11-24 | 东南大学 | Method and device for testing bulk oxygen migration dynamics in chemical chain technology |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100284A (en) * | 2007-06-29 | 2008-01-09 | 清华大学 | Gas fuel oxygen-carried hydrogen-produced and carbon dioxide separation method and device |
| CN101261010A (en) * | 2008-04-22 | 2008-09-10 | 青岛科技大学 | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus |
| CN101666546A (en) * | 2009-09-30 | 2010-03-10 | 华中科技大学 | Pulverized coal combustion method and device with function of capturing CO2 |
| CN101672530A (en) * | 2009-08-12 | 2010-03-17 | 东南大学 | Method and device for burning chemistry chains based on iron or iron oxide |
| CN103062910A (en) * | 2013-01-11 | 2013-04-24 | 东南大学 | Method and device for integrating chemical-looping combustion with CO<2> trapping |
| CN203442802U (en) * | 2013-09-11 | 2014-02-19 | 华北电力大学 | Coupling gasification multiple-bed structure solid fuel chemical looping reaction device |
-
2015
- 2015-04-07 CN CN201510161670.6A patent/CN104848207B/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101100284A (en) * | 2007-06-29 | 2008-01-09 | 清华大学 | Gas fuel oxygen-carried hydrogen-produced and carbon dioxide separation method and device |
| CN101261010A (en) * | 2008-04-22 | 2008-09-10 | 青岛科技大学 | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus |
| CN101672530A (en) * | 2009-08-12 | 2010-03-17 | 东南大学 | Method and device for burning chemistry chains based on iron or iron oxide |
| CN101666546A (en) * | 2009-09-30 | 2010-03-10 | 华中科技大学 | Pulverized coal combustion method and device with function of capturing CO2 |
| CN103062910A (en) * | 2013-01-11 | 2013-04-24 | 东南大学 | Method and device for integrating chemical-looping combustion with CO<2> trapping |
| CN203442802U (en) * | 2013-09-11 | 2014-02-19 | 华北电力大学 | Coupling gasification multiple-bed structure solid fuel chemical looping reaction device |
Non-Patent Citations (1)
| Title |
|---|
| 污泥和准东煤的化学链燃烧实验研究;蒋守席等;《工程热物理学报》;20160531;第37卷(第5期);第1106-1111页 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110923010A (en) * | 2019-12-10 | 2020-03-27 | 中国科学院工程热物理研究所 | Coal staged gasification method and device based on chemical looping combustion |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104848207A (en) | 2015-08-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104848207B (en) | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation | |
| CN106247323B (en) | A kind of chemical chain combustion apparatus and its method based on tower bubbling fluidized bed fuel reactor | |
| CN105222129B (en) | A kind of coal-fired burning chemistry chains separation CO for coupling pure oxygen gasification2Method | |
| CN101235321B (en) | Indirect gasification device and method for solid fuel | |
| CN101699187B (en) | Coal combustion apparatus capable of separating carbon dioxide and separation method thereof | |
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN102087023B (en) | Device for separating carbon dioxide through chemical-looping combustion in coal pressurizing high-density recirculating fluidized bed | |
| CN104925752A (en) | Chemical chain hydrogen production device and method based on iron-based oxygen carrier graded reduction | |
| CN106621583B (en) | A kind of gas dry cleaning cyclone adsorbing Coupling device | |
| CN105600747B (en) | A kind of hydrogen production of chemical chain device and method based on metal oxygen carrier | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN111763535B (en) | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification | |
| CN202947125U (en) | Chemical looping combustion device of variable circulating fluidized bed | |
| CN104197323A (en) | Inner and outer circulation coupled device for separating carbon dioxide by burning coal-based chemical loopings | |
| CN209702674U (en) | A kind of gasification system | |
| CN101387397B (en) | Metal oxygen carrier oxidating and regenerating device and method in chemical chain combustion processes | |
| CN208762459U (en) | A kind of fluid bed powder coal gasification device of flying dust zero-emission | |
| CN102966943B (en) | Chemical looping combustion device with variable circulating fluidized beds | |
| CN102180757B (en) | Method for direct methanation of recirculating fluidized bed synthesis gas | |
| CN208090661U (en) | A kind of carbon-based fuel fractional combustion and destructive distillation device based on chemical chain | |
| CN109945172B (en) | Chemical-looping combustion device suitable for D-type fuel particles and A-type oxygen carrier particles | |
| CN108504389A (en) | A kind of carbon-based fuel burning chemistry chains gasification coupling device and method | |
| CN107760385A (en) | Fluid bed and melting bed combined coal gasification apparatus and its method | |
| CN102425788B (en) | Apparatus for separating CO2 by pressurized double-loop circulating fluidized bed coal chemical looping combustion | |
| CN211667810U (en) | Chemical chain reaction device with wide load regulation capacity |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| EXSB | Decision made by sipo to initiate substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20170901 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |