CN104848207A - Chemical looping combustion device for solid fuel grading oxidation and method thereof - Google Patents
Chemical looping combustion device for solid fuel grading oxidation and method thereof Download PDFInfo
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- CN104848207A CN104848207A CN201510161670.6A CN201510161670A CN104848207A CN 104848207 A CN104848207 A CN 104848207A CN 201510161670 A CN201510161670 A CN 201510161670A CN 104848207 A CN104848207 A CN 104848207A
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 102
- 230000003647 oxidation Effects 0.000 title claims abstract description 79
- 239000004449 solid propellant Substances 0.000 title claims abstract description 50
- 238000002485 combustion reaction Methods 0.000 title claims abstract description 31
- 239000000126 substance Substances 0.000 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 19
- 239000000446 fuel Substances 0.000 claims abstract description 126
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 102
- 239000001301 oxygen Substances 0.000 claims abstract description 102
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 102
- 238000002309 gasification Methods 0.000 claims abstract description 76
- 239000007789 gas Substances 0.000 claims abstract description 73
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 40
- 238000006243 chemical reaction Methods 0.000 claims abstract description 26
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 20
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 20
- 230000009467 reduction Effects 0.000 claims abstract description 20
- 239000008187 granular material Substances 0.000 claims description 60
- 239000000463 material Substances 0.000 claims description 23
- 238000006722 reduction reaction Methods 0.000 claims description 16
- 238000005243 fluidization Methods 0.000 claims description 13
- 238000007599 discharging Methods 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
- 239000007787 solid Substances 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 238000006479 redox reaction Methods 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
- 239000010802 sludge Substances 0.000 claims description 3
- 210000000481 breast Anatomy 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 5
- 239000002184 metal Substances 0.000 description 8
- 239000000571 coke Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 229910044991 metal oxide Inorganic materials 0.000 description 4
- 150000004706 metal oxides Chemical class 0.000 description 4
- 230000009257 reactivity Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000007084 catalytic combustion reaction Methods 0.000 description 2
- 239000000428 dust Substances 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
- 230000009471 action Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 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
- 238000010586 diagram Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000002955 isolation Methods 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
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 invention discloses a chemical looping combustion device for solid fuel grading oxidation and a method thereof. The device is a circulating loop formed by an air reactor, an air cyclone separator, a fuel reactor, a fuel cyclone separator, a return feeder, a gasification reactor and an isolator. The method includes the steps that solid fuel is subjected to gasification reaction in the gasification reactor, generated gas fuel and oxygen carrier at a poor oxidation state are subjected to oxidation reaction, generated weak reduction gas enters the fuel reactor, and the generated weak reduction gas and oxygen carrier at an oxidation state are subjected to deep oxidation reaction, are converted into carbon dioxide and steam and are discharged; oxygen carrier at a reduction state in the air reactor and air are subjected to oxidation reaction to generate oxygen carrier particles at an oxidation state, and after being separated by the air cyclone separator, the oxygen carrier particles at an oxidation state enter the fuel reactor and are reduced to oxygen carrier at a poor oxidation state through weak reduction gas; after being separated by the fuel cyclone separator, the oxygen carrier at the poor oxidation state enters the gasification reactor through the return feeder and is reduced to the oxygen carrier at a reduction state through the solid fuel gasification products, and finally the oxygen carrier particles at a reduction state are returned to the air reactor through the isolator and are regenerated to form the oxygen carrier at the oxidation state.
Description
Technical field
The present invention relates to the device and method of the burning chemistry chains of a kind of solid fuel classification oxidation, be specially and realize solid fuel classification oxidation, improve efficiency of combustion, reach chemical chain combustion apparatus and the method for separating carbon dioxide in combustion process.
Background technology
Burning chemistry chains is a kind of New combustion technique, fuel is not directly and air catalytic combustion, but by the alternating oxidation-reduction reaction of oxygen carrier between air reactor and fuel reactor, realize the transfer of oxygen, complete the conversion process of fuel chemical energy, its principle is: use metal oxide as oxygen carrier, first the metal oxygen carrier of reduction-state contacts with air and carries out oxidation reaction in air reactor, generate the metal oxygen carrier of oxidation state, oxygen in air is cemented out, then the metal oxygen carrier of oxidation state enters fuel reactor, contact with gaseous fuel, carry out reduction reaction, oxygen in the metal oxygen carrier of oxidation state is cemented out, the gaseous product of fuel reactor is carbon dioxide and steam, reject steam after condensation and obtain pure carbon dioxide, metal oxygen carrier after reduction turns back to air reactor, and air carries out oxidation reaction, generates the metal oxygen carrier of oxidation state, completes the regeneration of oxygen carrier.
In gaseous fuel burning chemistry chains process, in fuel reactor, the transformation efficiency of gaseous fuel is subject to the restriction of the reactivity of oxygen carrier, and the reactivity of oxygen carrier is lower, and in fuel reactor exit gas, the combustable gas concentration of non-complete oxidation is higher; On the other hand, alternating oxidation-the reduction reaction of metal oxygen carrier between air reactor and fuel reactor in burning chemistry chains process, metal oxygen carrier granule surface can be caused to sinter, fine and close top layer is formed at its particle surface, the reactivity of oxygen carrier reduces, thus make the fuel gas containing more non-complete oxidation in fuel reactor exiting flue gas, cause burning chemistry chains efficiency to reduce.
In solid fuel chemistry chain combustion process, in fuel reactor, first solid fuel carries out gasification reaction with gasifying medium, generates gaseous fuel, then gaseous fuel reducing metal oxide oxygen carrier, generates carbon dioxide and steam; Compare with the reduction process of metal oxide oxygen carrier, solid-fuelled gasification reaction is slow, it is the rate control loop joint of whole solid fuel chemistry chain burning, have more trickle coke granule not to be gasified totally, directly carried by air-flow and leave fuel reactor, cause solid fuel chemistry chain efficiency of combustion to reduce.
Therefore, how improving the oxidation efficiency of gaseous fuel in fuel reactor, reduce trickle coke granule and carried away by air-flow, is the key realizing solid fuel chemistry chain combustion process, and its technology has social benefit and prospects for commercial application widely.
Summary of the invention
Goal of the invention: in order to overcome the deficiencies in the prior art, the invention provides a kind of oxidation efficiency improving gaseous fuel in fuel reactor, and reduces the device and method of the solid fuel chemistry chain burning that trickle coke granule is carried away by air-flow.
Technical scheme: for achieving the above object, the technical solution used in the present invention is:
A chemical chain combustion apparatus for solid fuel classification oxidation, comprises the circular response device that gasification reactor, air reactor and fuel reactor are interconnected to form successively.
Further, in the present invention, the top of described gasification reactor is provided with gas vent, the bottom of described fuel reactor is provided with gas feed, the bottom of described fuel reactor is also provided with air distribution plate, described air distribution plate is provided with some blast caps, and described gas vent is connected by described air distribution plate with described gas feed.
Further, in the present invention, described air reactor is connected with described fuel reactor by vortex of air separator;
The air reactor blast pipe being arranged at described air reactor top is connected with the upper feed inlet of described vortex of air separator, the bottom discharging opening of described vortex of air separator is connected by the top of dipleg with described fuel reactor, and described dipleg stretches into centre or the lower area of described fuel reactor inside.
Further, in the present invention, described fuel reactor is connected with described gasification reactor by fuel cyclone separator;
The fuel reactor blast pipe being arranged at described fuel reactor 3 top is connected with the upper feed inlet of described fuel cyclone separator, and the bottom discharging opening of described fuel cyclone separator connects the bottom of described gasification reactor.
Further, in the present invention, the bottom discharging opening of described fuel cyclone separator is connected through the bottom of material returning device with described gasification reactor.
Further, in the present invention, the middle part of described gasification reactor or bottom are connected by the bottom of isolator with described air reactor.
A kind of method of chemical chain combustion apparatus of solid fuel classification oxidation, solid fuel enters in described gasification reactor, by oxygen carrier at described air reactor, carry out oxidation-reduction reaction to alternate cycles between fuel reactor and gasification reactor, described oxygen carrier comprises oxidation state oxygen carrier granule, poor oxidation state oxygen carrier granule and reduction-state oxygen carrier granule; Concrete grammar comprises the following steps:
1) gasification-oxidation reaction: described solid fuel enters in described gasification reactor and carries out gasification reaction, the gaseous fuel generated carries out oxidation reaction with the poor oxidation state oxygen carrier granule from described fuel reactor in described gasification reactor, generate week reduction gas and reduction-state oxygen carrier granule, described week reduction gas upwards flows out described gasification reactor, enter described fuel reactor by the blast cap of described air distribution plate, described reduction-state oxygen carrier granule enters described air reactor;
2) secondary oxidation reaction: through step 1) the described week reduction gas that generates enters in fuel reactor, secondary oxidation reaction is carried out with the oxidation state oxygen carrier granule from air reactor in described fuel reactor, generate poor oxidation state oxygen carrier granule and carbon dioxide and steam, enter described fuel cyclone separator together and carry out gas solid separation, described carbon dioxide and steam are discharged by flue gas exhaust pipe, and the described poor oxidation state oxygen carrier granule separated enters in described gasification reactor by material returning device;
3) oxygen carrier regenerative response: through step 1 in gasification reactor) the described reduction-state oxygen carrier granule that generates enters in described air reactor, oxygen carrier regenerative response is carried out with the air entered in air reactor, generate oxidation state oxygen carrier granule, described oxidation state oxygen carrier granule enters described vortex of air separator by described air reactor blast pipe, carry out gas solid separation, the described oxidation state oxygen carrier granule separated enters described fuel reactor.
Further, in the present invention, step 1) in, the residual solid fuel be not gasified totally in described gasification reactor drives with described week reduction gas, blast cap through described air distribution plate enters described fuel reactor, carry out gasification reaction further, the oxidation state oxygen carrier granule in the gaseous fuel of generation and described fuel reactor reacts, and oxidation conversion is carbon dioxide and steam.
Further, in the present invention, the reaction temperature in described air reactor is 850 ~ 1100 DEG C, and the reaction temperature in described fuel reactor and described gasification reactor is 600 ~ 950 DEG C; Described air reactor and described fuel reactor are fluidized-bed reactor, and described gasification reactor is spouted fluidized bed bioreactor.
Further, in the present invention, to add fluidizing gas described in fluidizing gas be steam and/or carbon dioxide respectively by being arranged on the first class gas feed of corresponding device bottom, the second fluidisation gas inlet and the 3rd fluidisation gas inlet for described material returning device, gasification reactor and isolator; Described solid fuel is containing hydrocarbon solid fuel, comprises coal, living beings, domestic sludge.
Beneficial effect: the chemical chain combustion apparatus of a kind of solid fuel classification oxidation provided by the invention and method, adopt the method for the burning chemistry chains of solid fuel classification oxidation, solid fuel is made first to carry out sufficient gasification reaction with gasifying medium, generate gaseous fuel and restore metal oxide oxygen carrier, generate carbon dioxide and steam discharge, not only increase solid fuel chemistry chain efficiency of combustion, oxidation efficiency and the transformation efficiency of gaseous fuel in fuel reactor can be improved simultaneously, reduce trickle coke granule to be carried away by air-flow, it is the key realizing solid fuel chemistry chain combustion process, on the other hand, decrease in course of reaction the factor causing the reactivity of oxygen carrier to reduce, contribute to normally carrying out of reaction, ensure burning chemistry chains efficiency, its technology has social benefit and prospects for commercial application widely.
Accompanying drawing explanation
Fig. 1 is apparatus structure schematic diagram of the present invention.
Wherein there is 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, material returning 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, second fluidisation gas inlet 6.1, spouted pipe 6.2, reduction-state oxygen carrier granule 6.3, isolator 7, isolator feed pipe 7.1, isolator discharge nozzle 7.2, 3rd fluidisation gas inlet 7.3.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention is further described.
Be illustrated in figure 1 the chemical chain combustion apparatus of a kind of solid fuel classification oxidation, comprise the circular response device that closed circuit that gasification reactor 6, air reactor 1 and fuel reactor 3 be interconnected to form successively forms.
The top of gasification reactor 6 is provided with gas vent, the bottom of fuel reactor 3 is provided with gas feed, the bottom of fuel reactor 3 is also 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 is connected by air distribution plate 3.3 with gas feed.The effect of air distribution plate allows gas uniform enter fuel reactor, supports the particulate bed material in fuel reactor simultaneously.
Air reactor 1 is connected with fuel reactor 3 by vortex of air separator 2;
The air reactor blast pipe 1.1 being arranged at air reactor 1 top is connected with the upper feed inlet of vortex of air separator 2, the bottom discharging opening of vortex of air separator 2 is connected by the top of dipleg 2.1 with fuel reactor 3, dipleg 2.1 stretches into bosom in fuel reactor 3 or lower area, reducibility gas is contacted from bottom in order to allow reactant, abundant reaction, prevents having neither part nor lot in reaction and just runs away from upper outlet spilling.
Fuel reactor 3 is connected with gasification reactor 6 by fuel cyclone separator 4;
The fuel reactor blast pipe 3.1 being arranged at fuel reactor 3 top is connected with the upper feed inlet of fuel cyclone separator 4, and the top of fuel cyclone separator 4 is flue gas exhaust pipe 4.1; The bottom discharging opening of fuel cyclone separator 4 connects material returning device 5 through material returning device feed pipe 5.1, then connects the bottom of gasification reactor 6 through material returning device discharge nozzle 5.2.The effect of material returning device 5 is transported in gasification reactor 6 by the granule materials separated from fuel cyclone separator 4 by fluidised mode, the centre of material returning device 5 is provided with dividing plate, play the effect of isolation, gas anti-channeling in strick precaution gasification reactor 6, in fuel cyclone separator 4, reduces gas-solid disngaging efficiency; The fluidizing gas that first class gas feed 5.3 enters adopts steam or CO
2, the gas that such guarantee fuel reactor 3 is discharged is CO
2and steam, and not containing other gas.
The middle part of gasification reactor 6 or bottom connect isolator 7 by isolator feed pipe 7.1, then are connected through the bottom of isolator discharge nozzle 7.2 with air reactor 1; The effect of isolator 7, with material returning device 5, is also play buffer action.
Embodiment
The method of chemical chain combustion apparatus of solid fuel classification oxidation be solid fuel not directly and an air catalytic combustion, solid fuel is contain hydrocarbon solid fuel, comprises coal, living beings, domestic sludge.Solid fuel enters in gasification reactor 6, by oxygen carrier at air reactor 1, carry out oxidation-reduction reaction to alternate cycles between fuel reactor 3 and gasification reactor 6, realize solid-fuelled combustion process, oxygen carrier comprises oxidation state oxygen carrier granule 1.2, poor oxidation state oxygen carrier granule 3.2 and reduction-state oxygen carrier granule 6.3; Concrete grammar comprises the following steps:
1) gasification-oxidation reaction: when combustion occurs, fluidizing gas enters in gasification reactor 6 through the second fluidisation gas inlet 6.1 be arranged on bottom gasification reactor 6, solid fuel delivers in gasification reactor 6 through the spouted pipe 6.2 in the middle of being arranged on bottom gasification reactor 6, is being positioned in the middle part of gasification reactor 6 or bottom is set as that gasification-oxidation reaction is piled; Gasification reactor 6 is spouted fluidized bed structure, first solid fuel carries out gasification reaction with fluidizing gas, the gaseous fuel generated carries out oxidation reaction with the poor oxidation state oxygen carrier granule 3.2 from described fuel reactor 3 in described gasification reactor 6, generate week reduction gas and reduction-state oxygen carrier granule 6.3, week reduction gas upwards flows out gasification reactor 6, is entered in fuel reactor 3 carry out step 2 by the blast cap 3.3.1 of air distribution plate 3.3) i.e. secondary oxidation reaction; Reduction-state oxygen carrier granule 6.3 enters in isolator 7 through isolator feed pipe 7.1, after the fluidization of the fluidizing gas through entering from the 3rd fluidisation gas inlet 7.3 be arranged at bottom isolator 7, reduction-state oxygen carrier granule 6.3 in flow-like is discharged through isolator discharge nozzle 7.2 again, enters in air reactor 1 and carry out step 3) i.e. oxygen carrier regenerative response;
Preferably, step 1) in, the trickle coke granule of the residual solid fuel be not gasified totally on a small quantity in gasification reactor 6 drives with week reduction gas and carries away, enter in fuel reactor 3 through the blast cap 3.3.1 of air distribution plate 3.3, carry out gasification reaction further, oxidation state oxygen carrier granule 1.2 in the gaseous fuel and the fuel reactor 3 that generate carries out oxidation reaction further, and oxidation conversion is carbon dioxide and steam, the efficiency of combustion of raising gaseous fuel;
Same, step 1) in, in gasification reactor 6, the gaseous fuel of a small amount of non-complete oxidation drives with week reduction gas and carries away, fuel reactor 3 is entered through the blast cap 3.3.1 of air distribution plate 3.3, oxidation reaction is carried out further with the oxidation state oxygen carrier granule 1.2 in fuel reactor 3, oxidation conversion is carbon dioxide and steam, improves the efficiency of combustion of gaseous fuel;
2) secondary oxidation reaction: have oxidation state oxygen carrier granule 1.2 in fuel reactor 3, through step 1) the week reduction gas that generates enters in fuel reactor (3), secondary oxidation reaction is carried out with the oxidation state oxygen carrier granule 1.2 from air reactor 1 in fuel reactor 3, generate poor oxidation state oxygen carrier granule 3.2 and carbon dioxide and steam, carbon dioxide and steam carry together with poor oxidation state oxygen carrier granule 3.2 and enter described fuel cyclone separator 4, carry out gas solid separation, carbon dioxide and steam are discharged by flue gas exhaust pipe 4.1, the poor oxidation state oxygen carrier granule 3.2 material returning device feed pipe 5.1 separated falls and enters through in material returning device 5, the fluidizing gas entered from the first class gas feed 5.3 be arranged at bottom material returning device 5 is to poor oxidation state oxygen carrier granule 3.2, play fluidization, carry and discharge through material returning device discharge nozzle 5.2 together, enter the gasification-oxidation reaction heap in gasification reactor 6, carry out the 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 described reduction-state oxygen carrier granule 6.3 that generates enters in air reactor 1, the bottom of air reactor 1 is provided with air intlet 1.3, reduction-state oxygen carrier granule 6.3 and the air entered in air reactor 1 carry out oxygen carrier regenerative response, oxidation generates oxidation state oxygen carrier granule 1.2, oxidation state oxygen carrier granule 1.2 is carried away by air-flow, vortex of air separator 2 is entered by the air reactor blast pipe 1.1 being located at the top of air reactor 1, carry out gas solid separation, the oxygen denuded air blast pipe 2.2 of reacted oxygen denuded air through being positioned at the top of vortex of air separator 2 is discharged, the described oxidation state oxygen carrier granule 1.2 separated freely falls through dipleg 2.1 gravitate and enters bottom fuel reactor 3, enters next round reaction.
In addition, a part of dust after solid fuel gasifies in gasification reactor 6 is followed reduction-state oxygen carrier granule 6.3 and is entered into air reactor 1 by isolator 7, carried away by the gas in air reactor 1, discharged by the oxygen denuded air blast pipe 2.2 of vortex of air separator 2; The gas that another part dust is vaporized reactor 6 carries and enters fuel reactor 3 by the air distribution plate 3.3 of fuel reactor 3, is carried away, discharged together by the flue gas exhaust pipe 4.1 of fuel cyclone separator 4 by the gas in fuel reactor 3;
Reaction temperature in air reactor 1 is 850 ~ 1100 DEG C of conditions of high temperature, reaction temperature in fuel reactor 3 and gasification reactor 6 is temperature state in 600 ~ 950 DEG C, air reactor, relies on oxygen carrier granule to carry out heat transmission between fuel reactor and gasification reactor.Air reactor 1 and fuel reactor 3 are fluidized-bed reactor, and gasification reactor 6 is spouted fluidized bed bioreactor.
Material returning device 5, gasification reactor 6 and isolator 7 add fluidizing gas respectively by first class gas feed 5.3, second fluidisation gas inlet 6.1 and the 3rd fluidisation gas inlet 7.3 being arranged on corresponding device bottom, the effect of fluidizing gas is the oxygen carrier granule fluidisation allowed in material returning device 5, gasification reactor 6 and isolator 7, make particle have the characteristic of fluid, fluidizing gas is steam and/or carbon dioxide.
The above is only the preferred embodiment of the present invention; be noted that for those skilled in the art; under the premise without departing from the principles of the invention, can also make some improvements and modifications, these improvements and modifications also should be considered as protection scope of the present invention.
Claims (10)
1. a chemical chain combustion apparatus for solid fuel classification oxidation, is characterized in that: comprise the circular response device that gasification reactor (6), air reactor (1) and fuel reactor (3) are interconnected to form successively.
2. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, it is characterized in that: the top of described gasification reactor (6) is provided with gas vent, the bottom of described fuel reactor (3) is provided with gas feed, the bottom of described fuel reactor (3) is also provided with air distribution plate (3.3), described air distribution plate (3.3) is provided with some blast caps (3.3.1), and described gas vent is connected by described air distribution plate (3.3) with described gas feed.
3. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, is characterized in that: described air reactor (1) is connected with described fuel reactor (3) by vortex of air separator (2);
The air reactor blast pipe (1.1) being arranged at described air reactor (1) top is connected with the upper feed inlet of described vortex of air separator (2), the bottom discharging opening of described vortex of air separator (2) is connected by the top of dipleg (2.1) with described fuel reactor (3), and described dipleg (2.1) stretches into described fuel reactor (3) bosom or lower area.
4. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, is characterized in that: described fuel reactor (3) is connected with described gasification reactor (6) by fuel cyclone separator (4);
The fuel reactor blast pipe (3.1) being arranged at described fuel reactor (3) top is connected with the upper feed inlet of described fuel cyclone separator (4), and the bottom discharging opening of described fuel cyclone separator (4) connects the bottom of described gasification reactor (6).
5. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 4, is characterized in that: the bottom discharging opening of described fuel cyclone separator (4) is connected through the bottom of material returning device (5) with described gasification reactor (6).
6. the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 1, is characterized in that: the middle part of described gasification reactor (6) or bottom are connected by the bottom of isolator (7) with described air reactor (1).
7. the method for the chemical chain combustion apparatus of a solid fuel classification oxidation, it is characterized in that: solid fuel enters in described gasification reactor (6), by oxygen carrier described air reactor (1), between fuel reactor (3) and gasification reactor (6) alternate cycles ground carry out oxidation-reduction reaction, described oxygen carrier comprises oxidation state oxygen carrier granule (1.2), poor oxidation state oxygen carrier granule (3.2) and reduction-state oxygen carrier granule (6.3); Concrete grammar comprises the following steps:
1) gasification-oxidation reaction: described solid fuel enters in described gasification reactor (6) and carries out gasification reaction, the gaseous fuel generated carries out oxidation reaction with the poor oxidation state oxygen carrier granule (3.2) from described fuel reactor (3) in described gasification reactor (6), generate week reduction gas and reduction-state oxygen carrier granule (6.3), described week reduction gas upwards flows out described gasification reactor (6), described fuel reactor (3) is entered by the blast cap (3.3.1) of described air distribution plate (3.3), described reduction-state oxygen carrier granule (6.3) enters described air reactor (1),
2) secondary oxidation reaction: through step 1) the described week reduction gas that generates enters in fuel reactor (3), secondary oxidation reaction is carried out with the oxidation state oxygen carrier granule (1.2) from air reactor (1) in described fuel reactor (3), generate poor oxidation state oxygen carrier granule (3.2) and carbon dioxide and steam, enter described fuel cyclone separator (4) together and carry out gas solid separation, described carbon dioxide and steam are discharged by flue gas exhaust pipe (4.1), the described poor oxidation state oxygen carrier granule (3.2) separated enters in described gasification reactor (6) by material returning device (5),
3) oxygen carrier regenerative response: through step 1 in gasification reactor (6)) the described reduction-state oxygen carrier granule (6.3) that generates enters in described air reactor (1), oxygen carrier regenerative response is carried out with the air entered in air reactor (1), generate oxidation state oxygen carrier granule (1.2), described oxidation state oxygen carrier granule (1.2) enters described vortex of air separator (2) by described air reactor blast pipe (1.1), carry out gas solid separation, the described oxidation state oxygen carrier granule (1.2) separated enters described fuel reactor (3).
8. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 7, it is characterized in that: step 1) in, the residual solid fuel be not gasified totally in described gasification reactor (6) drives with described week reduction gas, blast cap (3.3.1) through described air distribution plate (3.3) enters described fuel reactor (3), carry out gasification reaction further, generate gaseous fuel and described fuel reactor (3) in oxidation state oxygen carrier granule (1.2) react, oxidation conversion is carbon dioxide and steam.
9. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 7, it is characterized in that: the reaction temperature in described air reactor (1) is 850 ~ 1100 DEG C, the reaction temperature in described fuel reactor (3) and described gasification reactor (6) is 600 ~ 950 DEG C; Described air reactor (1) and described fuel reactor (3) are fluidized-bed reactor, and described gasification reactor (6) is spouted fluidized bed bioreactor.
10. the method for the chemical chain combustion apparatus of solid fuel classification oxidation according to claim 7, it is characterized in that: described material returning device (5), gasification reactor (6) and isolator (7) add fluidizing gas respectively by being arranged on the first class gas feed (5.3) of corresponding device bottom, the second fluidisation gas inlet (6.1) and the 3rd fluidisation gas inlet (7.3), and described fluidizing gas is steam and/or carbon dioxide; Described solid fuel is containing hydrocarbon solid fuel, comprises coal, living beings, domestic sludge.
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| CN108204593A (en) * | 2018-01-30 | 2018-06-26 | 广州环保投资集团有限公司 | The method and device that a kind of chemical chain is burnt away the refuse |
| CN109054900A (en) * | 2018-08-17 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
| CN109282279A (en) * | 2018-09-05 | 2019-01-29 | 东南大学 | A kind of regenerated burning chemistry chains air reactor of reinforcing oxygen carrier oxidating |
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| 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 |
Families Citing this family (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 |
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 |
|---|
| 蒋守席等: "污泥和准东煤的化学链燃烧实验研究", 《工程热物理学报》 * |
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|---|---|---|---|---|
| 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 |
| CN108204593A (en) * | 2018-01-30 | 2018-06-26 | 广州环保投资集团有限公司 | The method and device that a kind of chemical chain is burnt away the refuse |
| CN109054900A (en) * | 2018-08-17 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
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| 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 |
| 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 |
| CN113513751A (en) * | 2021-03-30 | 2021-10-19 | 江苏大学 | Microwave technology-coupled chemical-looping combustion directional desulfurization process and device |
| 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 |
| CN113834897A (en) * | 2021-08-16 | 2021-12-24 | 东南大学 | Method and device for testing bulk phase oxygen migration kinetics in chemical chain technology |
| 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 |
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