CN102705822B - Device and method for separating CO2 by circulating fluidized bed chemical looping-combustion of coal and combustible solid waste - Google Patents
Device and method for separating CO2 by circulating fluidized bed chemical looping-combustion of coal and combustible solid waste Download PDFInfo
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- CN102705822B CN102705822B CN201210154841.9A CN201210154841A CN102705822B CN 102705822 B CN102705822 B CN 102705822B CN 201210154841 A CN201210154841 A CN 201210154841A CN 102705822 B CN102705822 B CN 102705822B
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- fluidized bed
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- oxygen carrier
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery
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Abstract
The invention discloses a device and a method for separating CO2 by circulating fluidized bed chemical looping-combustion of coal and combustible solid waste; the device mainly comprises three portions including a burning reaction system, a separation system and an oxygen carrying reaction system, wherein the burning reaction system is a circulating fluidized bed fuel reactor (1); the separation system comprises a one-stage inertial separator (2), a one-stage inertial separator outlet (3), a one-stage dipleg (4), a two-stage cyclone separator (11), a two-stage cyclone separator outlet (10) and a two-stage dipleg (12); the oxygen carrying reaction system comprises a cross-flow moving bed air reactor (6), a fresh oxygen carrier particle feeder (5), a J-shaped material returning valve (8) and an inactive oxygen carrier particle discharger (C); the method can enable the speed of combustion reaction of coal/combustible solid waste and oxygen carrier to be matched with the speed of oxygen carrying reaction of the oxygen carrier so as to achieve the effects that burning efficiency is high, oxygen carrying capability of the oxygen carriers is strong, concentration of separated CO2 is high, and final CO2 capturing rate is high.
Description
Technical field
The present invention relates to the apparatus and method of the recirculating fluidized bed burning chemistry chains of a kind of coal and solid waste, belong to recycling and the fluidized bed combustion field of coal combustion, solid waste.
Background technology
China is the current CO2 emission state of maximum in the world, forces China must find efficient and rational CO from the pressure of environmental protection and world opinion
2reduction of discharging means.Meanwhile, China is also maximum in the world generation of waste materials state, and the increase year after year of solid waste generation causes and has a strong impact on China environmental protection and the ecological balance, and wherein, the combustible constituent in solid waste accounts for the over half of China's solid waste total amount.Present stage, China was still very low to the comprehensive utilization ratio of flammable solid waste due to the restriction of technology and condition.Utilize chemical chain burning technology (CLC) to process flammable solid discarded object, both realized the recycling of solid waste, reduce its pollution to environment, can help to alleviate again the pressure of coal supply and demand, reduce CO2 emissions, be conducive to promote the formation of China's diversification energy resource structure, there is important economy, society and environmental benefit.
Existing flammable solid discarded object is converted into fuel, the composition of combustion Product complexity of these conventional methods, CO mainly with hot chemical treatment (burning, gasification and pyrolysis) method greatly
2not easily separated.Burning chemistry chains (CLC) is a kind of burning theory of novelty, its energy releasing mechanism is to react without flame chemistry, not directly and air catalytic combustion, but the cycle alternation between two reactors (air reactor and fuel reactor) reacts to realize the combustion process of fuel to fuel with oxygen carrier.By oxygen carrier first with airborne oxygen generation oxidation reaction, then in fuel reactor, carry out reduction reaction with fuel and generate carbon dioxide and water, the carbon dioxide therefore generating is easily separated.
In China, not only the solid waste treating technology of existing use and equipment are long-term by abroad being monopolized at present, and core technology and the pilot scale rank device of forward-looking burning chemistry chains (CLC) all rest in the hand of foreign study mechanism especially; Present Domestic has possessed independent research and development capacity, and close the gap is in the short period of time developed the solid waste chemical chain burning technology that is suitable for China's national situation, has independent intellectual property right, avoids repeating away the road for development that introduction absorbs.
Summary of the invention
technical problem:the object of the present invention is to provide a kind of coal and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O
2apparatus and method, overcome the combustion rate and the problems such as mating of oxygen carrier oxygen carrier reaction rate of coal/flammable solid discarded object and oxygen carrier, and design a kind of coal and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O
2method, the method can make the two reaction rate match, and reaches that efficiency of combustion is high, strong, the isolated CO of the oxygen carrying capability of oxygen carrier
2high and the CO of concentration
2the final high texts of capture rate.
technical scheme:the present invention proposes a kind of coal and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O
2apparatus and method.Coal and solid waste recirculating fluidized bed burning chemistry chains separation of C O
2device, mainly comprises combustion reaction system, piece-rate system and oxygen carrier reaction system three parts; Combustion reaction system is recirculating fluidized bed fuel reactor; Piece-rate system comprises one-level inertia separator, the outlet of one-level inertia separator, primary dipleg, secondary cyclone, secondary cyclone outlet and secondary dipleg; Oxygen carrier reaction system comprises cross-flow moving bed air reactor, fresh oxygen carrier granule dispenser, J-shaped returning charge valve and inactivation oxygen carrier granule removal device;
Recirculating fluidized bed fuel reactor top is connected with one-level inertia separator by elbow, the bottom of one-level inertia separator connects primary dipleg, the top of one-level inertia separator connects the top of secondary cyclone by the outlet of one-level inertia separator, the bottom of secondary cyclone connects the middle part of primary dipleg by secondary dipleg, the lower part outlet of primary dipleg is arranged in cross-flow moving bed air reactor, the bottom of cross-flow moving bed air reactor connects the bottom of recirculating fluidized bed fuel reactor by J-shaped returning charge valve, inactivation oxygen carrier granule removal device, reactor gasifying agent (steam) entrance and reactor gasifying agent (CO
2) entrance is positioned at the bottommost of recirculating fluidized bed fuel reactor, flammable solid discarded object entrance, coal particle entrance is positioned on the wall of bottom of recirculating fluidized bed fuel reactor.
Recirculating fluidized bed top is connected with one-level inertia separator top by the elbow of hexagonal angle; The diameter of the primary dipleg being connected with one-level inertia separator is the twice of recirculating fluidized bed fuel reactor diameter, and the diameter of the secondary dipleg that secondary cyclone connects is recirculating fluidized bed fuel reactor diameter 1/2nd; In cross-flow moving bed air reactor, adopt porous plate as gas distributor, outlet is furnished with the deflector that cross section is equilateral triangle.
Coal of the present invention and solid waste recirculating fluidized bed burning chemistry chains separation of C O
2the method of operating of device is: solid waste and coal particle enter from the bottom of recirculating fluidized bed fuel reactor, the oxygen loss oxygen carrier that the flue gas that gasification reaction produces carries enters cross-flow moving bed air reactor after one-level inertia separator separates with carbon containing dust, oxygen carrier after regeneration is got back to fuel reactor and is continued reaction, repeats above process; The carbon containing dust that one-level inertia separator is separated and a small amount of oxygen loss oxygen carrier fine grained enter secondary cyclone with flue gas and carry out secondary separation, and the solid particle separating is back to air reactor and continues reaction; Secondary cyclone is isolated end product CO
2and H
2o discharges, and rejects steam through condensation, obtains highly purified CO
2.
In described recirculating fluidized bed fuel reactor, adopt pressure 0.1MPa, particle flux 5 0～100 kg/m
2the normal pressure high flux of s, or pressure >0.1MPa, particle flux >200kg/m
2two kinds of modes of operation of pressurization high flux of s.
Implementation method thinking of the present invention is as follows: the flameless combustion course of reaction that realizes gasification and gasification product and the oxygen carrier generation of coal and flammable solid discarded object in recirculating fluidized bed fuel reactor; In inertia separator, realize effective separation process of oxygen carrier granule and flue gas; In cross-flow moving bed air reactor, realize the process of oxygen carrier again of oxygen carrier.And by repeating above process, realize burning chemistry chains and the CO of coal and flammable solid discarded object
2separate.
Different from traditional solid waste handling process, handling process of the present invention is: coal particle and flammable solid discarded object particle are followed gasifying agent (steam and CO
2mixture) generating gasification reaction in recirculating fluidized bed fuel reactor, coal more easily gasifies compared to solid waste, and the gas of generation can be accelerated course of reaction; Gasification product and the band oxygen oxygen carrier generation combustion reaction of returning to recirculating fluidized bed fuel reactor, generate CO
2and H
2o; The flue gas that reaction produces carries oxygen loss oxygen carrier and carbon containing coal ash, enters one-level inertia separator and separates; The oxygen loss oxygen carrier separating enters in air reactor, be in contact with one another to react with the air laterally passing through and obtain regeneration, returning to recirculating fluidized bed fuel reactor through one-level returning charge inlet valve afterwards separates, the solid particle (carbon containing dust and oxygen loss oxygen carrier fine grained) that secondary separation is got off returns to recirculating fluidized bed fuel reactor through secondary returning charge inlet valve to be continued to participate in combustion reaction, and isolated gas is rejected H through condensation
2o, obtains highly purified CO
2
beneficial effect:compare with solid waste treatment system with existing conventional CLC system, the present invention has following characteristic and advantage:
1, recirculating fluidized bed is combined to utilization with cross-flow moving bed, realize respectively the combustion reaction process of solid waste/oxygen carrier and the oxygen carrier course of reaction of oxygen carrier.By significantly improving the oxygen carrier reaction rate of oxygen carrier, solve and have the differential reaction matching problem causing of quantity because of the two reaction rate.
2, fuel reactor can adopt normal pressure or pressurized operation, and under pressurized conditions, recirculating fluidized bed has density high (Gu-gas volume ratio be greater than 0.1), circulating ratio high (50～100), the high (>200kg/m of material flux
2s) feature, the material particles time of staying is much larger than common the normal pressure fluidized bed reactor, gas-solid turbulence reaction (as coal and solid waste particle gasification reaction, the reaction of gasification product reduction oxygen carrier) speed obviously increases, not only significantly improved the burn rate of solid waste, and in gas-phase product, the imperfect combustion product such as CO effectively reduces.Oxygen carrier concentration in fuel reactor is far above ordinary cycle fluidized-bed reactor, and the gasification product of solid waste is by the continuous Quick Oxidation of oxygen carrier, thereby improved gasification reaction speed, promoted the gasification reaction of solid waste.
3, the CLC system that breaks traditions adopts fluid bed as the thinking of air reactor, adopt cross-flow moving bed as air reactor, oxygen loss oxygen carrier and air cross-flow hybrid reaction therein.
4,, because air reactor adopts special cross-flow moving bed design, oxygen carrier granule interiorly passes through fast cross-flow moving bed.Even if sneak into a small amount of carbon containing dust in oxygen carrier, because the reaction time is short, particle compared with large, contact area is little, is difficult for sintering occurs, and has reduced the carbon containing dust sintering risk causing of burning in air reactor; Compare with fluidized bed air reactor, cross-flow moving bed air reactor is simple in structure, and it is convenient to control.
5, the present invention adopts the elbow of 120 ° to be connected with one-level inertia separator top on recirculating fluidized bed top, follow the hydrodynamic characters of movement of particles, compared with conventional right angle connected mode, reduce the wearing and tearing of particle to junction, improve the stability of system operation.
Accompanying drawing explanation
Fig. 1 is coal of the present invention and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O
2equipments overall structure schematic diagram.
Fig. 2 is coal of the present invention and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O
2air reactor structure enlarged diagram in device.
In above figure, have: recirculating fluidized bed fuel reactor 1, one-level inertia separator 2, one-level inertia separator outlet 3, primary dipleg 4, fresh oxygen carrier granule dispenser 5, cross-flow moving bed air reactor 6, deflector 7, J-shaped returning charge valve 8, one-level returning charge inlet valve 9, secondary cyclone outlet 10, secondary cyclone 11, secondary dipleg 12, secondary returning charge inlet valve 13, air ports orifice plate 14.
Flammable solid discarded object entrance A, coal particle entrance B, inactivation oxygen carrier granule removal device C, reactor gasifying agent (steam) entrance D, reactor gasifying agent (CO
2) entrance E, air intake F, air reactor exhaust outlet G.
The specific embodiment
Describe coal of the present invention and flammable solid discarded object recirculating fluidized bed burning chemistry chains separation of C O in detail referring to Fig. 1
2method, (main component is as Fe take iron ore for oxygen carrier
2o
3) be example.
1) air distribution plate that recirculating fluidized bed solid waste reactor (following or abbreviation fuel reactor) 1 bottom is arranged is gasification agent inlet, and lower-left side has two entrances, is flammable solid discarded object entrance A above, is coal particle entrance B below.Right side is one-level returning charge entrance.Steam and CO
2mixture is as gasifying agent and fluidizing agent, respectively from reactor gasifying agent (steam) entrance D and the reactor gasifying agent (CO of fuel reactor 1 bottom
2) entrance E enters, the returning charge that carry the flammable solid discarded object particle entering from flammable solid discarded object entrance A and the coal particle entering from coal particle entrance B, enters from one-level returning charge entrance moves upward.In this process, gasifying agent reacts with flammable solid discarded object particle and coal particle generating gasification, generates fuel gas, and main component is CO and H
2.Fuel gas and oxygen carrier generation redox reaction, the oxygen in oxygen carrier passes to fuel gas, makes CO be oxidized to CO
2, H
2be oxidized to H
2o(gas), and oxygen carrier loses partial oxygen generation ferrous oxide or tri-iron tetroxide.Oxygen carrier generation redox reaction, consumes CO and H
2, also promoted the gasification reaction of coal and flammable solid discarded object.
2) reacted solid particle (oxygen loss oxygen carrier granule and carbon containing dust) is taken out of by flue gas, enter with fuel reactor and export the one-level inertia separator 2 being connected, most of oxygen loss oxygen carrier granule is separated to be got off to enter the cross-flow moving bed air reactor (following or abbreviation air reactor) 6 being connected with primary dipleg 4, and carbon containing dust and a small amount of oxygen loss oxygen carrier fine grained enter secondary cyclone 11 with flue gas from one-level inertia separator outlet 3.
3), in air reactor 6, the isolated oxygen loss oxygen carrier of one-level inertia separator 2 carries out oxygen carrier reaction.Oxygen loss oxygen carrier enters from the top of air reactor 6, air evenly enters after air ports orifice plate 14 from air intake F, cross-flow contact there is redox reaction in both, oxygen loss oxygen carrier oxidation by air regeneration, and reacted tail gas is discharged from air reactor exhaust outlet G.Oxygen carrier after regeneration, through J-shaped returning charge valve 8 and one-level returning charge inlet valve 9, is got back to fuel reactor and is continued reaction.The shuttling movement of material between fuel reactor 1-one-level inertia separator 2-air reactor 6-fuel reactor 1 formed one-level returning charge circulation.In the time that oxygen carrier oxygen carrying capability obviously declines, supplement corresponding fresh oxygen carrier from fresh oxygen carrier granule dispenser 5, meanwhile, the oxygen carrier of permanent deactivation is discharged from inactivation oxygen carrier granule removal device C.
4) carry carbon containing dust and a small amount of fine grain flue gas of oxygen loss oxygen carrier in the interior generation secondary separation of secondary cyclone 11.The solid particle separating enters secondary dipleg 12, is back to primary dipleg 4 continues reaction through secondary returning charge inlet valve 13.The shuttling movement of material between fuel reactor 1-one-level inertia separator 2-secondary cyclone 11-air reactor 6-fuel reactor 1-formed secondary returning charge circulation.CO
2and H
2o(gas) admixture of gas discharge from secondary cyclone outlet 10, reject steam through condensation, obtain highly purified CO
2.
Claims (2)
1. a coal and flammable solid waste recirculating fluidized bed burning chemistry chains separation of C O
2device, mainly comprise combustion reaction system, piece-rate system and oxygen carrier reaction system three parts; It is characterized in that, combustion reaction system is recirculating fluidized bed fuel reactor (1); Piece-rate system comprises one-level inertia separator (2), the outlet of one-level inertia separator (3), primary dipleg (4), secondary cyclone (11), secondary cyclone outlet (10) and secondary dipleg (12); Oxygen carrier reaction system comprises cross-flow moving bed air reactor (6), fresh oxygen carrier granule dispenser (5), J-shaped returning charge valve (8) and inactivation oxygen carrier granule removal device (C);
The top of recirculating fluidized bed fuel reactor (1) connects the top of one-level inertia separator (2), the bottom of one-level inertia separator (2) connects primary dipleg (4), the top of one-level inertia separator (2) connects the top of secondary cyclone (11) by one-level inertia separator outlet (3), the bottom of secondary cyclone (11) connects the middle part of primary dipleg (4) by secondary dipleg (12), the lower part outlet of primary dipleg (4) is arranged in cross-flow moving bed air reactor (6), the bottom of cross-flow moving bed air reactor (6) connects the bottom of recirculating fluidized bed fuel reactor (1) by J-shaped returning charge valve (8), inactivation oxygen carrier granule removal device (C), reactor gasification agent inlet (D) and reactor gasification agent inlet (E) are positioned at the bottommost of recirculating fluidized bed fuel reactor (1), flammable solid discarded object entrance (A), coal particle entrance (B) is positioned on the wall of bottom of recirculating fluidized bed fuel reactor (1),
Described recirculating fluidized bed top is connected with one-level inertia separator top by the elbow of hexagonal angle; The diameter of the primary dipleg (4) being connected with one-level inertia separator (2) is the twice of recirculating fluidized bed fuel reactor (1) diameter, and the diameter of the secondary dipleg (12) that secondary cyclone (11) connects is recirculating fluidized bed fuel reactor (1) diameter 1/2nd; In cross-flow moving bed air reactor (6), adopt porous plate as gas distributor, outlet is furnished with the deflector that cross section is equilateral triangle.
2. a coal as claimed in claim 1 and flammable solid waste recirculating fluidized bed burning chemistry chains separation of C O
2device separation of C O
2method, it is characterized in that: solid waste and coal particle enter from the bottom of recirculating fluidized bed fuel reactor (1), the oxygen loss oxygen carrier that the flue gas that gasification reaction produces carries enters cross-flow moving bed air reactor (6) after one-level inertia separator (2) separates with carbon containing dust, oxygen carrier after regeneration is got back to fuel reactor (1) and is continued reaction, repeats above process; The carbon containing dust that one-level inertia separator (2) is separated and a small amount of oxygen loss oxygen carrier fine grained enter secondary cyclone (11) with flue gas and carry out secondary separation, and the solid particle separating is back to air reactor (6) and continues reaction; Secondary cyclone (11) is isolated end product CO
2and H
2o discharges, and rejects steam through condensation, obtains highly purified CO
2;
In described recirculating fluidized bed fuel reactor (1), adopt pressure 0.1MPa, particle flux 50～100kg/m
2the normal pressure high flux of s, or pressure >0.1MPa, particle flux >200kg/m
2two kinds of modes of operation of pressurization high flux of s.
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|---|---|---|---|
| CN201210154841.9A CN102705822B (en) | 2012-05-18 | 2012-05-18 | Device and method for separating CO2 by circulating fluidized bed chemical looping-combustion of coal and combustible solid waste |
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|---|---|---|---|
| CN201210154841.9A CN102705822B (en) | 2012-05-18 | 2012-05-18 | Device and method for separating CO2 by circulating fluidized bed chemical looping-combustion of coal and combustible solid waste |
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| CN102705822A CN102705822A (en) | 2012-10-03 |
| CN102705822B true CN102705822B (en) | 2014-07-09 |
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| CN104197323B (en) * | 2014-09-19 | 2017-02-15 | 东南大学 | Inner and outer circulation coupled device for separating carbon dioxide by burning coal-based chemical loopings |
| CN111115570B (en) * | 2019-12-31 | 2022-02-22 | 西安交通大学 | Chemical chain conversion recovery non-magnetic metal oxide parallel hydrogen production system and process |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| CN202073606U (en) * | 2011-03-17 | 2011-12-14 | 绍兴文理学院 | Dynamic system of chemical-looping combustion with petroleum and natural gas without flame |
| CN202598494U (en) * | 2012-05-18 | 2012-12-12 | 东南大学 | Circulating fluidized bed chemical-looping combustion and CO2 separation device for coal and combustible solid waste |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AT505526B1 (en) * | 2007-08-14 | 2010-09-15 | Univ Wien Tech | FLUID BED REACTOR SYSTEM |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| 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 |
| CN202073606U (en) * | 2011-03-17 | 2011-12-14 | 绍兴文理学院 | Dynamic system of chemical-looping combustion with petroleum and natural gas without flame |
| CN202598494U (en) * | 2012-05-18 | 2012-12-12 | 东南大学 | Circulating fluidized bed chemical-looping combustion and CO2 separation device for coal and combustible solid waste |
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