CN201954532U - Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion - Google Patents
Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion Download PDFInfo
- Publication number
- CN201954532U CN201954532U CN2010206350275U CN201020635027U CN201954532U CN 201954532 U CN201954532 U CN 201954532U CN 2010206350275 U CN2010206350275 U CN 2010206350275U CN 201020635027 U CN201020635027 U CN 201020635027U CN 201954532 U CN201954532 U CN 201954532U
- Authority
- CN
- China
- Prior art keywords
- high density
- fluidized bed
- coal
- recirculating fluidized
- pressurization high
- 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 - Lifetime
Links
Images
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)
Abstract
The utility model discloses a device for a coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion, wherein the upper part of a combustible reactor of the coal-pressurization high density circulating fluidized bed is communicated with a primary cyclone separator, the lower part of the primary cyclone separator is communicated with an air reactor of a cross flow moving bed through a primary dipleg, the lower part of the air reactor of the cross flow moving bed is communicated with that of the combustible reactor of the coal-pressurization high density circulating fluidized bed through a primary material return device, so a primary circulation loop is formed; and the upper part of the combustible reactor of the coal-pressurization high density circulating fluidized bed is communicated with the primary cyclone separator, the upper part of the primary cyclone separator is communicated with that of a secondary cyclone separator through a secondary exhaust pipe, the lower part of the secondary cyclone separator is communicated with a secondary material return device through a secondary dipleg, the outlet of the secondary material return device is communicated with the combustible reactor of the coal-pressurization high density circulating fluidized bed, so a secondary circulation loop is formed. The device solves the reaction matching problem, so the combustion efficiency of the coal can be greatly improved.
Description
Technical field
The utility model relates to a kind of coal chemistry chain burning separation of C O
2Device, belong to the clean burning of fuel and efficiently utilize the field.
Background technology
Carbon dioxide is the greenhouse gases that have the greatest impact in many potential greenhouse gases, and how reducing emission of carbon dioxide has become one of main contents of human kind sustainable development from now on.Burning chemistry chains (ChemicalLooping Combustion is called for short CLC) is internationally recognized CO with important prospect
2One of emission-reduction technology.Its basic principle is the not direct and air catalytic combustion of fuel, realize combustion process but react: in air reactor, utilize the oxygen in the oxygen carrier separation of air on the one hand with the cycle alternation of oxygen carrier between two reactors, in the fuel reaction device, airborne oxygen is delivered in the fuel on the other hand, carries out the burning of fuel by oxygen carrier.Because in the combustion process, fuel does not directly contact with air, combustion product has only carbon dioxide and water vapour, utilizes simple cooling device just can isolate CO
2Thereby, realize CO
2Enrichment, therefore be a kind of clean burning mode.
Since nineteen eighty-three, Germany scientist proposed the burning chemistry chains notion, many in the world research institutions had all carried out a series of research to it.Up to the present, adopt the CLC technology and the oxygen carrier research comparative maturity of gaseous fuel or liquid fuel, and the research of coal-fired CLC still is in the starting stage, and all there are many problems in the various process routes that directly are transformed into solid fuel (as coal, living beings) based on gas and liquid fuel.Because coal/oxygen carrier combustion rate and oxygen carrier oxygen carrier reaction rate differ 2～3 orders of magnitude, conventional system is difficult to realize well the optimization coupling of coal/oxygen carrier combustion reaction and the reaction of oxygen carrier oxygen carrier, does not therefore obtain internationally recognized processing technology routine so far as yet.Current, many in the world research institutions seek new thinking just one after another, research and development coal chemistry chain burning separation of C O
2New technology.
Summary of the invention
Technical problem: the utility model is difficult to realize well the optimization matching problem of coal/oxygen carrier combustion reaction and the reaction of oxygen carrier oxygen carrier at the CLC system of routine, a kind of device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide is provided, and this device has efficiency of combustion height, strong, the isolated CO of oxygen carrying capability
2Concentration height and CO
2The final high effect of capture rate.
Technical scheme: the utility model provides a kind of device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide.Thinking of the present invention is: the coal in the pressurization high density recirculating fluidized bed fuel reaction device under realization high granule density, high circulating ratio and the high particle flux and the combustion reaction process of oxygen carrier; Realize the oxygen carrier course of reaction of oxygen carrier in the cross-flow moving bed air reactor; The two stage cyclone device is realized effective completing combustion that separates and promote the carbon containing coal ash of oxygen carrier and carbon containing coal ash respectively.The gaseous product of coal and oxygen carrier burning mainly is CO
2With the admixture of gas of water vapour, finish CO through the dedusting condensation
2Separation.Below with reference to Fig. 1, specify the specific implementation of technology path of the present invention and target.
The device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide comprises pressurization high density recirculating fluidized bed fuel reaction device, primary cyclone, primary dipleg, fresh oxygen carrier granule dispenser, cross-flow moving bed air reactor, flase floor, inactivation oxygen carrier granule removal device, one-level material returning device, one-level blast pipe, secondary cyclone, secondary blast pipe, secondary dipleg and secondary material returning device;
The top of the high density of wherein pressurizeing recirculating fluidized bed fuel reaction device is connected with primary cyclone, the bottom of primary cyclone is connected with cross-flow moving bed air reactor by primary dipleg, the bottom of cross-flow moving bed air reactor is connected by the bottom of one-level material returning device with pressurization high density recirculating fluidized bed fuel reaction device, constitutes the one-level closed circuit;
The top of pressurization high density recirculating fluidized bed fuel reaction device is connected with primary cyclone, the top of primary cyclone is connected with the top of secondary cyclone by the one-level blast pipe, the bottom of secondary cyclone is communicated with the secondary material returning device by the secondary dipleg, the outlet of secondary material returning device is connected with pressurization high density recirculating fluidized bed fuel reaction device, constitutes the secondary closed circuit.
The top exit of described pressurization high density recirculating fluidized bed fuel reaction device connects primary cyclone; Bottom inlet is followed successively by gasification agent inlet, coal particle inlet, one-level returning charge inlet and secondary returning charge inlet from down to up, wherein gasification agent inlet is arranged in the bottom of pressurization high density recirculating fluidized bed fuel reaction device, and coal particle inlet, one-level returning charge inlet and secondary returning charge inlet are arranged in the side of pressurization high density recirculating fluidized bed fuel reaction device.
Be provided with many in the described cross-flow moving bed air reactor to its centroclinal flase floor, be respectively equipped with air intake and air reactor exhaust outlet in cross-flow moving bed air reactor both sides, be provided with inactivation oxygen carrier granule removal device in cross-flow moving bed air reactor bottom, be provided with fresh oxygen carrier granule dispenser on cross-flow moving bed air reactor top.
In the described pressurization high density recirculating fluidized bed fuel reaction device, coal particle and the reaction of gasifying agent generating gasification, gasification product and oxygen carrier generation redox reaction generate CO then
2And H
2O.Solid-gas the volume ratio in whole fuel reaction device space is greater than 0.1, and can reach greater than 200kg/m
2The particle flux of s and 50～100 times circulating ratio.
Finish separating of oxygen carrier granule and coal particle in the described primary cyclone.Oxygen carrier granule enters primary dipleg, and flue gas and unburned coal particle and a spot of oxygen carrier fine powder are discharged from the primary cyclone blast pipe.
Described cross-flow moving bed air reactor, the oxygen carrier that separates enters from the air reactor upper entrance, flows out from lower part outlet behind the oxygen carrier, react required air and enters from the air intake of air reactor one side, from the exhaust outlet discharge of opposite side.
Realize the secondary separation of flue gas and solid particle in the described secondary cyclone, carbon containing coal ash and a small amount of oxygen carrier fine powder enter the secondary dipleg, and flue gas (CO
2With water vapor mixture) discharge from the secondary cyclone blast pipe.
Beneficial effect: the utlity model has following characteristic and advantage:
1, the device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide of the present utility model, the high density of will pressurizeing recirculating fluidized bed and cross-flow moving bedly unite utilization is realized the combustion reaction process of coal and oxygen carrier and the oxygen carrier course of reaction of oxygen carrier respectively.By significantly improving the time of staying of particle in the combustion reaction process, there is the differential reaction matching problem that causes of quantity in the speed that solves owing to combustion reaction and oxygen carrier reaction.
2, the pressurization high density recirculating fluidized bed fuel reaction device that adopts of the utility model has high density (Gu-gas volume ratio greater than 0.1), high circulating ratio (50～100) and high particle flux (＞200kg/m
2S), the particle time of staying is much larger than the ordinary cycle fluidized-bed reactor, and gas-solid turbulence reaction (as gasification reaction, the reaction of gasification product reduction oxygen carrier of coal and steam) speed obviously increases, not only improved burning of coal efficient greatly, and imperfect combustion product such as CO effectively reduces in the gas-phase product, the separable CO that goes out high concentration
2
3, in the pressurization high density recirculating fluidized bed fuel reaction device of the present utility model, oxygen carrier concentration is far above the ordinary cycle fluidized-bed reactor, the coal gasification product is by continuously fast oxidation of oxygen carrier, thereby improved gasification reaction speed, promoted the coal gasification reaction.
4, primary cyclone of the present utility model, the difference on density and particle diameter according to oxygen carrier granule and carbon containing coal ash, oxygen carrier granule is separated to primary dipleg, flue gas and carbon containing coal ash are then discharged from the primary cyclone blast pipe, thereby assurance carbon containing coal ash does not enter in the air reactor substantially and burns, and has both improved CO
2Capture rate, the sintering problem of having avoided the carbon containing coal ash in air reactor, to burn and cause again.
5, cross-flow moving bed air reactor of the present utility model has been designed to special cross-flow moving bed, particle passes through in cross-flow moving bed fast, even sneak into a small amount of carbon containing coal ash like this in the oxygen carrier, because the reaction time is short, particle is big, contact area is little, sintering can not take place, reduced the sintering risk that the carbon containing coal ash burns in air reactor and causes; Compare with the fluidized bed air reactor, cross-flow moving bed air reactor is simple in structure, and control is convenient.
6, secondary separation device of the present utility model is an efficient cyclone separator, can effectively separate the carbon containing coal ash, effectively prolongs the time of staying of carbon containing coal ash in the fuel reaction device, improves the burn-out degree of coal.
Description of drawings
Fig. 1 is the concrete system diagram of implementing of device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide of the present utility model, comprising: pressurization high density recirculating fluidized bed fuel reaction device 1, primary cyclone 2, primary dipleg 3, fresh oxygen carrier granule dispenser 4, cross-flow moving bed air reactor 5, flase floor 6, inactivation oxygen carrier granule removal device 7, one-level material returning device 8, one-level blast pipe 9, secondary cyclone 10, secondary blast pipe 11, secondary dipleg 12, secondary material returning device 13, coal particle inlet A, gasification agent inlet B, one-level returning charge inlet C, secondary returning charge inlet D, air intake E, air reactor exhaust outlet F, one-level material returning device air inlet G, secondary cyclone gas outlet H, secondary material returning device air inlet I.
The specific embodiment
The device of the coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide that the utility model provides, this device comprises pressurization high density recirculating fluidized bed fuel reaction device 1, primary cyclone 2, primary dipleg 3, fresh oxygen carrier granule dispenser 4, cross-flow moving bed air reactor 5, flase floor 6, inactivation oxygen carrier granule removal device 7, one-level material returning device 8, one-level blast pipe 9, secondary cyclone 10, secondary blast pipe 11, secondary dipleg 12 and secondary material returning device 13.
The device of described coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide is made up of the two-stage closed circuit: the top of pressurization high density recirculating fluidized bed fuel reaction device 1 is connected with primary cyclone 2, the bottom of primary cyclone 2 is connected with cross-flow moving bed air reactor 5 by primary dipleg 3, the bottom of cross-flow moving bed air reactor 5 is connected by the bottom of one-level material returning device 8 with pressurization high density recirculating fluidized bed fuel reaction device 1, constitutes the one-level closed circuit; The top of pressurization high density recirculating fluidized bed fuel reaction device 1 is connected with primary cyclone 2, the top of primary cyclone 2 is connected by the top of one-level blast pipe 9 with secondary cyclone 10, the bottom of secondary cyclone 10 is communicated with secondary material returning device 13 by secondary dipleg 12, the outlet of secondary material returning device 13 is connected with pressurization high density recirculating fluidized bed fuel reaction device 1, constitutes the secondary closed circuit.
The top exit of described pressurization high density recirculating fluidized bed fuel reaction device 1 connects primary cyclone 2; Bottom inlet is followed successively by gasification agent inlet B, coal particle inlet A, one-level returning charge inlet C and secondary returning charge inlet D from down to up, wherein gasification agent inlet B is arranged in the bottom of pressurization high density recirculating fluidized bed fuel reaction device 1, and coal particle inlet A, one-level returning charge inlet C and secondary returning charge inlet D are arranged in the side of pressurization high density recirculating fluidized bed fuel reaction device 1.
Be provided with many in the described cross-flow moving bed air reactor 5 to its centroclinal flase floor 6, be respectively equipped with air intake E and air reactor exhaust outlet F in cross-flow moving bed air reactor 5 both sides, be provided with inactivation oxygen carrier granule removal device 7 in cross-flow moving bed air reactor 5 bottoms, be provided with fresh oxygen carrier granule dispenser 4 on cross-flow moving bed air reactor 5 tops.
Coal pressurization high density recirculating fluidized bed burning chemistry chains separation of C O
2The concrete thinking of device be: coal particle and gasifying agent (water vapour and CO
2Mixture) bottom section from pressurization high density recirculating fluidized bed fuel reaction device 1 enters, the generating gasification reaction, and gasification product and return the oxygen carrier generation redox reaction of fuel reaction device 1 then, gasification product is become CO by oxygen carrier oxidating
2And H
2O.The flue gas that reaction produces carries the oxygen loss oxygen carrier and the carbon containing coal ash leaves fuel reaction device 1, enter primary cyclone 2, the oxygen loss oxygen carrier is separated and enters air reactor 5, and carbon containing coal ash and a small amount of oxygen loss oxygen carrier fine grained then enter secondary cyclone 10 with flue gas.In secondary cyclone 10, realize the secondary separation of flue gas and solid particle (carbon containing coal ash and oxygen loss oxygen carrier fine grained), obtain clean CO
2With H
2The mixture of O (vapour) is rejected H through condensation
2O obtains highly purified CO
2, fuel reaction device 1 is given in 13 returning charges of isolated solid particle process secondary material returning device.Oxygen loss oxygen carrier from primary cyclone 2 comes out enters air reactor 5, is in contact with one another the generation redox reaction, reacted tail gas (N with the air that laterally passes through
2With a small amount of O
2Mixture) discharge from air reactor exhaust outlet D, and regenerate after the oxidation by air of oxygen loss oxygen carrier, get back to fuel reaction device 1 through one-level material returning device 8 and continue reaction.
Followingly describe coal of the present utility model pressurization high density recirculating fluidized bed burning chemistry chains separation of C O in detail with reference to Fig. 1
2The specific embodiment of device.
Present embodiment is oxygen carrier with the iron ore.Steam and CO
2Mixture is as gasifying agent and fluidizing agent; enter from the gasification agent inlet B of pressurization high density recirculating fluidized bed fuel reaction device 1 bottom, carry the coal particle that enters from coal particle inlet A, the returning charge that contains high concentration oxygen carrier iron ore that enters from one-level returning charge inlet C and coal and the oxygen carrier fine-grained mixture that enters from secondary returning charge inlet D move upward.In this process, gasifying agent and the reaction of coal generating gasification, (main component is CO and H to generate coal gas
2), coal gas again with oxygen carrier generation redox reaction, the oxygen in the oxygen carrier passes to coal gas, makes CO be oxidized to CO
2, H
2Be oxidized to H
2O (vapour) becomes ferrous oxide or tri-iron tetroxide and the iron ore oxygen carrier loses partial oxygen.Oxygen carrier generation redox reaction consumes CO and H
2, promoted the coal gasification reaction.
Reacted solid particle (oxygen loss oxygen carrier granule and carbon containing coal ash) is taken out of by flue gas, enter primary cyclone 2, most of oxygen loss oxygen carrier granule is separated and enters cross-flow moving bed air reactor 5, and carbon containing coal ash and a small amount of oxygen loss oxygen carrier fine grained then enter secondary cyclone 10 with flue gas.Primary cyclone 2 isolated oxygen loss oxygen carriers, enter from the top of cross-flow moving bed air reactor 5, air then evenly enters through behind the flase floor 6 from air intake E, both contact the generation redox reaction, reacted tail gas is discharged from air reactor exhaust outlet F, and oxygen loss oxygen carrier oxidation by air regeneration, the oxygen carrier after the regeneration enters one-level material returning device 8, at the CO that enters from one-level material returning device air inlet G
2Under the booster action of gas, get back to fuel reaction device 1 and continue reaction, the shuttling movement of above material has constituted one-level returning charge circulation.When the oxygen carrier oxygen carrying capability obviously descends, need to discharge the oxygen carrier of permanent deactivation from inactivation oxygen carrier granule removal device 7, simultaneously, replenish the corresponding fresh oxygen carrier from fresh oxygen carrier granule dispenser 4.
The carbon containing coal ash that carries that comes out from primary cyclone 2 enters in the secondary cyclone 10 with a small amount of fine grain flue gas of oxygen loss oxygen carrier, secondary separation takes place, CO
2And H
2The admixture of gas of O (vapour) is discharged from secondary cyclone gas outlet H, rejects water vapour through condensation, obtains highly purified CO
2, isolated solid particle enters secondary material returning device 13, at the CO that enters from secondary material returning device air inlet I
2Under the booster action of gas, be back to fuel reaction device 1, the shuttling movement of above material has constituted secondary returning charge circulation.
Claims (3)
1. the device of a coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide is characterized in that this device comprises pressurization high density recirculating fluidized bed fuel reaction device (1), primary cyclone (2), primary dipleg (3), fresh oxygen carrier granule dispenser (4), cross-flow moving bed air reactor (5), flase floor (6), inactivation oxygen carrier granule removal device (7), one-level material returning device (8), one-level blast pipe (9), secondary cyclone (10), secondary blast pipe (11), secondary dipleg (12) and secondary material returning device (13);
The top of the high density of wherein pressurizeing recirculating fluidized bed fuel reaction device (1) is connected with primary cyclone (2), the bottom of primary cyclone (2) is connected with cross-flow moving bed air reactor (5) by primary dipleg (3), the bottom of cross-flow moving bed air reactor (5) is connected by the bottom of one-level material returning device (8) with pressurization high density recirculating fluidized bed fuel reaction device (1), constitutes the one-level closed circuit;
The top of pressurization high density recirculating fluidized bed fuel reaction device (1) is connected with primary cyclone (2), the top of primary cyclone (2) is connected by the top of one-level blast pipe (9) with secondary cyclone (10), the bottom of secondary cyclone (10) is communicated with secondary material returning device (13) by secondary dipleg (12), the outlet of secondary material returning device (13) is connected with pressurization high density recirculating fluidized bed fuel reaction device (1), constitutes the secondary closed circuit.
2. the device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide according to claim 1 is characterized in that the top exit of described pressurization high density recirculating fluidized bed fuel reaction device (1) connects primary cyclone (2); Bottom inlet is followed successively by gasification agent inlet (B), coal particle inlet (A), one-level returning charge inlet (C) and secondary returning charge inlet (D) from down to up, wherein gasification agent inlet (B) is arranged in the bottom of pressurization high density recirculating fluidized bed fuel reaction device (1), and coal particle inlet (A), one-level returning charge inlet (C) and secondary returning charge inlet (D) are arranged in the side of pressurization high density recirculating fluidized bed fuel reaction device (1).
3. the device of coal pressurization high density recirculating fluidized bed burning chemistry chains separating carbon dioxide according to claim 1, it is characterized in that being provided with in the described cross-flow moving bed air reactor (5) many to its centroclinal flase floor (6), be respectively equipped with air intake (E) and air reactor exhaust outlet (F) in cross-flow moving bed air reactor (5) both sides, be provided with inactivation oxygen carrier granule removal device (7) in cross-flow moving bed air reactor (5) bottom, be provided with fresh oxygen carrier granule dispenser (4) on cross-flow moving bed air reactor (5) top.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206350275U CN201954532U (en) | 2010-12-01 | 2010-12-01 | Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010206350275U CN201954532U (en) | 2010-12-01 | 2010-12-01 | Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201954532U true CN201954532U (en) | 2011-08-31 |
Family
ID=44498642
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010206350275U Expired - Lifetime CN201954532U (en) | 2010-12-01 | 2010-12-01 | Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201954532U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102087023A (en) * | 2010-12-01 | 2011-06-08 | 东南大学 | Device for separating carbon dioxide through chemical-looping combustion in coal pressurizing high-density recirculating fluidized bed |
| CN102966943A (en) * | 2012-11-21 | 2013-03-13 | 华中科技大学 | Chemical looping combustion device with variable circulating fluidized beds |
-
2010
- 2010-12-01 CN CN2010206350275U patent/CN201954532U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102087023A (en) * | 2010-12-01 | 2011-06-08 | 东南大学 | Device for separating carbon dioxide through chemical-looping combustion in coal pressurizing high-density recirculating fluidized bed |
| CN102087023B (en) * | 2010-12-01 | 2012-05-23 | 东南大学 | Device for separating carbon dioxide through chemical-looping combustion in coal pressurizing high-density recirculating fluidized bed |
| CN102966943A (en) * | 2012-11-21 | 2013-03-13 | 华中科技大学 | Chemical looping combustion device with variable circulating fluidized beds |
| CN102966943B (en) * | 2012-11-21 | 2015-05-20 | 华中科技大学 | Chemical looping combustion device with variable circulating fluidized beds |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102087023B (en) | Device for separating carbon dioxide through chemical-looping combustion in coal pressurizing high-density recirculating fluidized bed | |
| CN101699187B (en) | Coal combustion apparatus capable of separating carbon dioxide and separation method thereof | |
| CN101261010B (en) | Double distribution plate coal-base serial fluidized-bed chemical chain combustion apparatus | |
| CN102183014B (en) | Method for separating CO2 through chemical looping combustion in coal pressure high-density circulating fluidized bed | |
| CN101666546B (en) | Pulverized coal combustion method and device with function of capturing CO2 | |
| CN105222129B (en) | A kind of coal-fired burning chemistry chains separation CO for coupling pure oxygen gasification2Method | |
| CN104848207B (en) | The chemical chain combustion apparatus and its method of a kind of solid fuel classification oxidation | |
| CN104403697B (en) | A kind of coal-fired boiler in power plant smoke emissioning pollution thing controls device and control method | |
| CN101672530A (en) | Method and device for burning chemistry chains based on iron or iron oxide | |
| CN105600747B (en) | A kind of hydrogen production of chemical chain device and method based on metal oxygen carrier | |
| CN102313283B (en) | Coal chemical looping combustion method by using pressurized two-circuit circulating fluidized bed | |
| CN104197323B (en) | Inner and outer circulation coupled device for separating carbon dioxide by burning coal-based chemical loopings | |
| CN102798222A (en) | Chemical-looping combustion device based on solid fuel and use method thereof | |
| CN202947125U (en) | Chemical looping combustion device of variable circulating fluidized bed | |
| CN201954532U (en) | Device for coal-pressurization high density circulating fluidized bed to separate carbon dioxide through chemical-looping combustion | |
| CN100436940C (en) | Coal-burning installation based on calcium sulphate oxygen carrier and coal burning method | |
| CN102798221B (en) | Chemical-looping combustion device and use method thereof | |
| CN102425788B (en) | Apparatus for separating CO2 by pressurized double-loop circulating fluidized bed coal chemical looping combustion | |
| CN103776023B (en) | A kind of double-fluidized-bed gas-solid burner and method | |
| CN102966943A (en) | Chemical looping combustion device with variable circulating fluidized beds | |
| CN107029554B (en) | Flue gas circulation denitration system based on sintering flue gas autocatalysis | |
| CN202598494U (en) | Circulating fluidized bed chemical-looping combustion and CO2 separation device for coal and combustible solid waste | |
| CN110194475A (en) | A kind of the high/low temperature roasting system and method for crystal aluminum chloride production aluminium oxide | |
| CN109945172A (en) | Chemical chain combustion apparatus suitable for D class A fuel A particle and A class oxygen carrier granule | |
| CN103486576A (en) | Chemical chain combustion device and method for three-reactor structure |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20110831 Effective date of abandoning: 20120523 |