CN103486576A - Chemical chain combustion device and method for three-reactor structure - Google Patents
Chemical chain combustion device and method for three-reactor structure Download PDFInfo
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- CN103486576A CN103486576A CN201310442407.5A CN201310442407A CN103486576A CN 103486576 A CN103486576 A CN 103486576A CN 201310442407 A CN201310442407 A CN 201310442407A CN 103486576 A CN103486576 A CN 103486576A
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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
Abstract
The invention discloses a chemical chain combustion device and method for a three-reactor structure. The chemical chain combustion device comprises an air reactor fluidized bed, wherein the air reactor fluidized bed is connected with a cyclone separator through a lifting pipe; the bottom of the cyclone separator is connected with a fuel reactor; a spiral feeder is arranged on the fuel reactor. The chemical chain combustion device is characterized in that the fuel reactor is connected with a material inlet of a purification reactor through a down pipe; a material outlet of the purification reactor is connected with a reaction chamber of the air reactor fluidized bed through a return pipe. The structure of the device is especially suitable for chemical chain combustion reaction of solid fuel; materials are fluidized and purified by water vapor in the added purification reactor; the purposes of cleaning oxygen carriers and carrying fine particles out of the purification reactor can be achieved while carbon particles remained in the oxygen carriers are removed through a gasification reaction by adjusting the flow quantity of the fluidizing vapor.
Description
Technical field
The present invention relates to a kind of chemical chain combustion apparatus and method of three structure of reactor, belong to chemical combustion systems technology field.
Background technology
Burning chemistry chains (Chemical looping combustion) technology is the revolutionary novel combustion system of a kind of tool, it is decomposed into two steps by a traditional step combustion reaction carries out respectively in fuel reactor and air reactor, by the middle circulation carrier of oxygen (being generally metal oxide), airborne oxygen is offered to fuel.In the traditional combustion reaction, because N
2dilution, CO in flue gas
2concentration is 13% left and right only, and needing to consume a large amount of energy could trap it; And, in the burning chemistry chains process, fuel and air are isolated, the flue gas therefore produced in fuel reactor can be by airborne N
2dilution, its main component is CO
2and H
2o, just can obtain highly purified CO through simple condensation
2in order to utilize or seal up for safekeeping.Simultaneously, it can also effectively suppress the generation of other pollutants, and, because the cascade utilization of energy, the burning chemistry chains mode can improve the thermal efficiency of system.Therefore, chemical chain burning technology is a kind of efficient, clean combustion system, is also at present the focus direction of studying both at home and abroad.
In the burning chemistry chains process, fuel tolerance is strong, and gas, liquid, solid fuel all can be suitable for.And be an important process in chemical chain technical research field for the reactor design of different fuel form, carrier of oxygen type always.Before 2000, the correlative study of chemical chain technology mainly concentrates on uses the gaseous fuel aspect, and after 2000, the various countries researcher just develops the chemical chain system that uses solid fuel (being mainly coal, petroleum coke etc.) gradually.Use solid fuel more complicated than the burning chemistry chains process of fuel gas fuel, more be difficult to control, main cause is because therefore the little 2-3 of the gas-solid reaction speed magnitude occurred in the solid-solid reaction speed ratio air reactor in fuel reactor is controlled and existed very large difficulty with operation in the structural design of two reactors.Design is mainly serial type fluidized-bed reactor (Interconnected fluidized-bed) and double-circulating fluid bed reactor (Dual CFB) for using solid-fuelled burning chemistry chains reactor at present.Interconnected fluidized bed reactor form class is similar to traditional recirculating fluidized bed, the air reactor of a fast bed and the fuel reactor of a low speed bubbling bed/turbulent bed, consists of, isolated with loop seal between two reaction beds; Double-circulating fluid bed reactor is formed by two circulating fluidized bed system serial connections.Although these two kinds of structure of reactor are different, all are based on two structure of reactor, i.e. a fuel reactor, an air reactor.At present, the correlative study result shows, in using solid-fuelled burning chemistry chains system, from fuel reactor, the carrier of oxygen out, carries the part carbon granule and directly is transferred in air reactor, and the consequence of this situation is the CO that has reduced system
2capturing efficiency.In addition, the microcellular structure of carrier of oxygen particle stops up and is all the unfavorable factors that affect systematic function along with the increase carrier of oxygen particle size of cycle-index diminishes.Therefore need to be improved for the structure of traditional chemical chain combustion system now, to solve the problems of the technologies described above.
Summary of the invention
Technical problem to be solved by this invention is to contain the problems such as residual carbon particle and carrier of oxygen particle (the particularly natural carrier of oxygen) constantly attenuate for using in solid-fuelled burning chemistry chains system the carrier of oxygen particle of discharging from fuel reactor, improved on traditional chemical chain combustion reactor structure, realized better system thermal performance and economic performance.
In order to solve the problems of the technologies described above, the invention provides a kind of chemical chain combustion apparatus of three structure of reactor, comprise the air reactor fluid bed, the air reactor fluid bed comprises reative cell, be provided with air distribution plate in reative cell, reative cell is provided with air inlet one, and the reative cell top is provided with changeover portion, changeover portion is connected with cyclone separator by riser, and the cyclone separator top is provided with exhaust outlet one; The cyclone separator bottom is connected with fuel reactor, and the fuel reactor top is provided with exhaust outlet two, and bottom is provided with slag-drip opening and air inlet three; Fuel reactor is provided with feeding screw, it is characterized in that, fuel reactor is connected with the material inlet of purification reactor by down-comer, and the material outlet of purification reactor is connected with the reative cell of air reactor fluid bed by the feed back pipe; The purification reactor top is provided with exhaust outlet three, and bottom is provided with air inlet five.
Preferably, described cyclone separator bottom is connected with fuel reactor by the first loop seal, and the first loop seal bottom is provided with air inlet two.
Preferably, be provided with the second loop seal between the material inlet of described down-comer and purification reactor, the second loop seal bottom is provided with air inlet four.
Preferably, the horizontal level of described material inlet sets high than the horizontal position of material outlet.
The present invention also provides a kind of burning chemistry chains method of three structure of reactor, it is characterized in that, adopt the chemical chain combustion apparatus of above-mentioned any one three structure of reactor, to after the second loop seal, be transferred in purification reactor from the carrier of oxygen particle of discharging fuel reactor, utilize water vapour to carry out fluidisation and purification, flow by regulating fluidization steam vapor, when realizing carbon granule residual in the carrier of oxygen is removed by gasification reaction, can also and carry out purification reactor by fine particle by carrier of oxygen cleaning.
Preferably, the mode of fluidization of described purification reactor is turbulent bed.
Enter fluidizing gas water vapour and/or CO from the air inlet threeway in fuel reactor in the chemical chain combustion apparatus of described three structure of reactor
2by solid fuel gasification, concrete reaction is:
C+H
2O→H
2+CO
C+CO
2→2CO
The CO, the H that generate
2with the carrier of oxygen generation reduction reaction in fuel reactor, concrete reaction is:
MeO+H
2→Me+H
2O
MeO+CO→Me+CO
2
Be rich in CO in the mixed flue gas that reaction generates
2and H
2o, discharge from exhaust outlet two, can obtain the CO of high concentration through simple condensation process
2.Simultaneously, extract a part and be back to the fluidizing gas of air inlet three as fuel reactor from the mixed flue gas obtained, the advantage of design cycle is like this: 1. rationally utilize source of the gas, reduce additional energy source consumption; 2. flue gas recirculation can improve CO in flue gas
2concentration.Contain some CO and/or H in flue gas
2the time, increased so on the one hand CO
2the energy consumption of purifying, also reduced on the other hand the utilization ratio of fuel, and the recirculation of flue gas can effectively overcome these problems.
When using solid fuel; because the fuel time of staying not, fuel carrier of oxygen particle time of contact not or the reason of the aspect such as carrier of oxygen performance reduction; often there is residual carbon granule in the carrier of oxygen particle of discharging from fuel reactor; and also likely stop up carbon granule or ash content are arranged in the micropore of carrier of oxygen particle surface, can affect like this CO of system
2the heating power of capturing efficiency and system, economic performance.On the other hand, along with the increase of cycle-index, carrier of oxygen particle can diminish in continuous fragmentation, and the variation of carrier of oxygen particle size will affect the fluidizing performance of material in fluidized system and the separating property in cyclone separator.Therefore, in purification reactor, use water vapour as fluidizing gas, on the one hand, can be by reaction
C+H
2O→H
2+CO
By residual carbon granule gasification, the synthesis gas of generation can further reduce carrier of oxygen particle; On the other hand, by regulating the flow of water vapour, can purge purification to carrier of oxygen particle, by the material such as the ash content of enrichment in carrier of oxygen surface and micropore, residual carbon and be crushed to very the carrier of oxygen of fine particle and carry and pass through exhaust outlet three discharges.So realize the purpose such as purification, screening of carrier of oxygen particle.
After purification, carrier of oxygen particle is transported in the air reactor fluid bed, pass into air from air reactor fluid bed bottom air inlet one as fluidizing gas, that the carrier of oxygen of reduction-state is grain fluidized, the oxidation reaction of carrier of oxygen particle occurs in main chamber, air reactor lower end, when fluidized particles process changeover portion, the cross-sectional area of air reactor reduces rapidly, the fluidized forms of particle converts fast fluidization to from the turbulence fluidisation, and fluidizing gas promotes carrier of oxygen particle rapidly, when carrying, carrier of oxygen particle further is oxidizing to stable state.In cyclone separator, the flue gas of carrier of oxygen particle and generation is separated, is rich in N in flue gas
2from the cyclone separator upper end, be discharged from, and carrier of oxygen particle enters in the first loop seal by down-comer, the first loop seal still passes into water vapour as fluidized wind from air inlet two, play the sealing left and right, carrier of oxygen particle further is transported in fuel reactor, completes the outer circulation of a carrier of oxygen particle.Solid fuel adds from the wall of fuel reactor by feeding screw.
Water vapour, as gasifying medium, can, by carbon granule gasification residual in the carrier of oxygen, improve system CO
2capturing efficiency; Water vapour, as fluidized wind, can purge the carbon of enrichment in carrier of oxygen particle surface and space, ash content or other materials, clean, and realizes purifying purpose; By regulating the flow of fluidized wind, the tiny carrier of oxygen particle that fragmentation can also be formed afterwards carries out purification reactor together in company with the ash material that grades.
The accompanying drawing explanation
The structural representation of the chemical chain combustion apparatus that Fig. 1 is three structure of reactor provided by the invention.
The specific embodiment
For the present invention is become apparent, hereby with preferred embodiment, and coordinate accompanying drawing to be described in detail below.
Embodiment
As shown in Figure 1, structural representation for the chemical chain combustion apparatus of three structure of reactor provided by the invention, comprise air reactor fluid bed 1, and air reactor fluid bed 1 comprises reative cell 1-2, be provided with air distribution plate 1-1 in reative cell 1-2, reative cell 1-2 is provided with air inlet one A.Reative cell 1-2 top is provided with changeover portion 1-3, and changeover portion 1-3 is connected with cyclone separator 2 by riser 1-4.The cross section of reative cell 1-2 is more much larger than the cross section of riser 1-4, so one section changeover portion 1-3 coupled reaction chamber 1-2 and riser 1-4 will be set.Cyclone separator 2 tops are provided with exhaust outlet one F.Cyclone separator 2 bottoms are connected with fuel reactor 5 by the first loop seal 3, and the first loop seal 3 bottoms are provided with air inlet two B.Fuel reactor 5 tops are provided with exhaust outlet two E, and bottom is provided with slag-drip opening D and air inlet three C.Fuel reactor 5 is provided with feeding screw 4.Fuel reactor 5 is connected with the material inlet 8-1 of purification reactor 8 by down-comer 6, is provided with the second loop seal 7, the second loop seal 7 bottoms between the material inlet 8-1 of down-comer 6 and purification reactor 8 and is provided with air inlet four G.The material outlet 8-2 of purification reactor 8 is connected with the reative cell 1-2 of air reactor fluid bed 1 by feed back pipe 9, and the horizontal level of material inlet 8-1 sets high than the horizontal position of material outlet 8-2.Purification reactor 8 tops are provided with exhaust outlet three I, and bottom is provided with air inlet five H.
With coal dust act as a fuel, CaSO
4-CaS carrier of oxygen circulation is example, in air reactor, the CaS particle in the 1-2 of main chamber, bottom by airborne O
2be oxidized to CaSO
4, fluidized forms is turbulent bed, the CaSO of generation
4particle and part also unreacted CaS particle are streamed to changeover portion 1-3, because the reducing rapidly of cross-sectional area, fluidized forms converts fast bed to from turbulent bed, thereby by hybrid particles upwards conveying in riser 1-4, O in course of conveying
2continue to incite somebody to action partly also unreacted CaS particulate oxidation and become CaSO
4, in the flue gas of generation, be rich in N
2, also comprise a small amount of O simultaneously
2with some minimum gas, flue gas is separated and discharge from exhaust outlet one F in cyclone separator, and the reaction temperature in air reactor fluid bed 1 is controlled between 1000～1050 ℃.In fuel reactor 5, coal dust is coiled into the fluidized wind H that glassware 4 is delivered in fuel reactor 5 and is passed into
2o and CO
2gasification generates CO and H
2, the synthesis gas of generation is by CaSO
4particle is reduced to CaS, generates H simultaneously
2o and CO
2from exhaust outlet, two E discharge, and partial fume is drawn is back to air inlet three C as fluidizing gas, and the reaction temperature in fuel reactor 5 is controlled between 900～1000 ℃.From the carrier of oxygen particle of discharging fuel reactor 5, after the second loop seal 7, enter in purification reactor 8.Purification reactor 8 is used water vapour as fluidized wind, and by carbon granule gasification residual in carrier of oxygen particle, synthesis gas is further by carrier of oxygen reduction, and synthesis gas is oxidized to H simultaneously
2o and CO
2, water vapour is purged carrier of oxygen particle, cleaned simultaneously, and residual ash content and tiny carrier of oxygen particle etc. is carried out to purification reactor 8, realizes purification, the screening purpose of carrier of oxygen particle, thereby improves the CO of burning chemistry chains system
2capturing efficiency and heating power, economic performance.
Claims (6)
1. the chemical chain combustion apparatus of a structure of reactor, comprise air reactor fluid bed (1), air reactor fluid bed (1) comprises reative cell (1-2), be provided with air distribution plate (1-1) in reative cell (1-2), reative cell (1-2) is provided with air inlet one (A), reative cell (1-2) top is provided with changeover portion (1-3), changeover portion (1-3) is connected with cyclone separator (2) by riser (1-4), and cyclone separator (2) top is provided with exhaust outlet one (F); Cyclone separator (2) bottom is connected with fuel reactor (5), and fuel reactor (5) top is provided with exhaust outlet two (E), and bottom is provided with slag-drip opening (D) and air inlet three (C); Fuel reactor (5) is provided with feeding screw (4), it is characterized in that, fuel reactor (5) is connected with the material inlet (8-1) of purification reactor (8) by down-comer (6), and the material outlet (8-2) of purification reactor (8) is connected with the reative cell (1-2) of air reactor fluid bed (1) by feed back pipe (9); Purification reactor (8) top is provided with exhaust outlet three (I), and bottom is provided with air inlet five (H).
2. the chemical chain combustion apparatus of a kind of three structure of reactor as claimed in claim 1, it is characterized in that, described cyclone separator (2) bottom is connected with fuel reactor (5) by the first loop seal (3), and the first loop seal (3) bottom is provided with air inlet two (B).
3. the chemical chain combustion apparatus of a kind of three structure of reactor as claimed in claim 1, it is characterized in that, be provided with the second loop seal (7) between the material inlet (8-1) of described down-comer (6) and purification reactor (8), the second loop seal (7) bottom is provided with air inlet four (G).
4. the chemical chain combustion apparatus of a kind of three structure of reactor as claimed in claim 1, is characterized in that, the horizontal level of described material inlet (8-1) sets high than the horizontal position of material outlet (8-2).
5. the burning chemistry chains method of a structure of reactor, it is characterized in that, adopt the chemical chain combustion apparatus of described three structure of reactor of any one in claim 1-3, to after the second loop seal (7), be transferred in purification reactor (8) from the carrier of oxygen particle of discharging fuel reactor (5), utilize water vapour to carry out fluidisation and purification, flow by regulating fluidization steam vapor, when realizing carbon granule residual in the carrier of oxygen is removed by gasification reaction, can also and carry out purification reactor (8) by fine particle by carrier of oxygen cleaning.
6. the burning chemistry chains method of three structure of reactor as claimed in claim 5, is characterized in that, the mode of fluidization of described purification reactor (8) is turbulent bed.
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| CN201310442407.5A CN103486576A (en) | 2013-09-25 | 2013-09-25 | Chemical chain combustion device and method for three-reactor structure |
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Cited By (3)
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| CN108554324A (en) * | 2017-12-29 | 2018-09-21 | 南京理工大学 | A kind of device and method preparing ammonia based on chemical chain reaction |
| CN112703348A (en) * | 2018-08-29 | 2021-04-23 | 斗山能捷斯有限责任公司 | Incineration apparatus and method |
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