CN103776023B - A kind of double-fluidized-bed gas-solid burner and method - Google Patents
A kind of double-fluidized-bed gas-solid burner and method Download PDFInfo
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- CN103776023B CN103776023B CN201410015069.1A CN201410015069A CN103776023B CN 103776023 B CN103776023 B CN 103776023B CN 201410015069 A CN201410015069 A CN 201410015069A CN 103776023 B CN103776023 B CN 103776023B
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Abstract
The invention discloses a kind of double-fluidized-bed gas-solid burner and method, solid fuel and gaseous fuel are added in reduction reactor respectively, react at this and oxidation state oxygen carrier, generate the gaseous product primarily of CO2 and steam composition and reduction-state oxygen carrier, enrichment to CO2 and seizure can be realized through gas solid separation to flue gas condensing; Reduction-state oxygen carrier is admitted to oxidation reactor and is again oxidized into oxidation state oxygen carrier, then once more turns back in reduction reactor and participates in reaction.The reduction reactor of this device can realize the adaptability to polytype fuel and oxygen carrier; This device introduces classification fluidizing method simultaneously, strengthens the mixing of material in device, improves the reaction efficiency of device; By the particular design of bottom of device returning charge structure, reduce the resistance that recycle stock is flowed to reduction reactor by oxidation reactor, relatively large Matter Transfer can be realized under controlled prerequisite.
Description
Technical field
The present invention relates to clean burning and the efficiency utilization field of fuel, be specifically related to a kind of double-fluidized-bed gas-solid burner and method, the burn application of the solid fuel being applicable to comprise coal, living beings etc. and the gaseous fuel comprising natural gas, synthesis gas from coal gasification etc.
Background technology
Along with the high speed development of society, the energy-output ratio of China has in the last few years and increases fast.According to State Statistics Bureau's data, within 2012, China's total energy consumption has reached 36.2 hundred million tons of standard coals, and the thing followed is all kinds of problems that the aspect such as energy resource supply and environmental pollution highlights day by day.As one of important reply means, new forms of energy and clean energy technology are more and more proposed and are used widely gradually.
Double fluidized bed combustion technology is a kind of clean and effective combustion technology with outstanding application prospect, on the advantage bases such as the disposal of pollutants that it has at fluid bed itself is low, simple to operate, treating capacity is large, in conjunction with self special design feature double-fluidized-bed, by the design of double-reactor, decoupling zero is carried out to the thermal chemical reaction entirety that macro manifestations is burning, realize controlling the refinement of thermal chemical reaction neutron reaction thus reach in course of reaction generate energy and material the object that utilizes of clean and effective.
Although current double fluidized bed combustion technology has had some achievements in research in gaseous fuel and solid-fuelled high-efficiency cleaning utilize, simultaneously practical with commercialization in also make some progress, but prior art is limited to the fluidization operational factor restriction of specific stream fluidized bed reactor, lacks the adaptive capacity to complexity source fuel.Especially, under the background utilized by getting more and more at current biomass and flammable solid discarded object, existing double fluidized bed combustion technology can't meet current application request.In addition, when considering execute-in-place, double-fluidized-bed requirement can realize material comparatively big cycle volume, notice that the impact effect of complicated change material to double-fluidized-bed returning charge differs greatly simultaneously, in existing double fluidized bed combustion technology, between double-reactor, the design of returning charge EGR still also exists in some shortcomings in adaptability, causes prior art to be difficult to realize to the control of solid circulating rate in the case thus.
Summary of the invention
Technical problem: adapt to fuel type change for being difficult to existing for existing double fluidized bed combustion technology and when recycle stock change between reactor solid circulating rate be difficult to the shortcomings such as controls, the object of the invention is to provide that a kind of structure is simple, control conveniently and be applicable to multiple gases and solid-fuelled double-fluidized-bed gas-solid burner and method.
Technical scheme: for solving the problems of the technologies described above, the technical solution used in the present invention is: a kind of double-fluidized-bed gas-solid burner, this device comprises reduction reactor and oxidation reactor;
Reduction reactor top is connected with reduction reactor cyclone separator, and reduction reactor cyclone separator lower end is connected with side, reduction reactor material returning device top, and reduction reactor cyclone separator upper end is connected with condenser; Reduction reactor middle and upper part is provided with overflow mechanism and is connected with returning charge down-comer; Reduction reactor material returning device is connected with oxidation reactor by reduction reactor material returning device returning charge inclined tube; Oxidation reactor top is connected with oxidation reactor cyclone separator, and oxidation reactor cyclone separator lower end is connected with side, oxidation reactor material returning device top; Oxidation reactor material returning device is connected with bottom oxidation reactor; Oxidation reactor and reduction reactor connect and compose loop structure by bottom by lower material returning device, and screw feeder is used for reduction reactor feed, and condenser is connected with reduction reactor cyclone separator, for separating of output high concentration CO 2.
Preferably, reduction reactor and oxidation reactor are provided with two-stage gas nozzle at differing heights respectively.
Preferably, reduction reactor is by making it to run on respectively bubbling fluidization state or turbulent fluidised state or fast fluidization state to valve switch set on flash device.
Present invention also offers a kind of double-fluidized-bed gas-solid combustion method, the method comprises the steps,
Solid fuel adds in reduction reactor by material inlet by feeding screw, and gaseous fuel adds in reduction reactor by reduction reactor first order jet nozzle; In reduction reactor mixed material by by bottom reduction reactor and first jet and second nozzle feed gas fluidized, the response characteristic of based on fuel is by fluidized state in the adjustment of fluidization gas and the switch adjustment reduction reactor of overflow mechanism valve; Fuel mixes with the oxidation state oxygen carrier be fluidized and reacts, and is obtained by reacting the gaseous product be made up of CO2 and steam, and gaseous product is separated through cyclone separator and exports, and after moisture is removed in condenser cooling, the enrichment realizing CO2 catches; Reduction-state oxygen carrier to be sent back in the middle part of oxidation reactor and by by bottom oxidation reactor and the 3rd nozzle and the 4th nozzle feed gas fluidized, by utilizing the O contained in fluidizing gas
2occur oxidation reaction again obtain oxidation state oxygen carrier, with after after oxidation reactor cyclone separator gas solid separation, oxidation state oxygen carrier is sent back to bottom oxidation reactor; Oxidized oxygen carrier comes back to reduction reactor through lower material returning device, forms the circulation between double-fluidized-bed reactor.
Beneficial effect: compared with prior art, the present invention has following characteristic and advantage:
(1) double-fluidized-bed gas-solid burner of the present invention makes described device can adapt to the service requirement of bubbling fluidization state, turbulent fluidised state and fast fluidization state respectively by particular design, make described device can tackle the fuel in complicated source, and reaction efficiency can be improved to greatest extent by the adjustment of operational factor, thus realize the efficiency utilization of material and energy;
(2) reduction reactor involved in the present invention and oxidation reactor adopt bottom communication type material returning device to realize the Matter Transfer of described device, relatively little owing to transmitting resistance, the transmission capacity of material can be ensured, thus ensure the reaction efficiency of single unit system, make it the application demand adapting to different fuel and oxygen carrier;
(3) the present invention all can be suitable for multiclass solid fuel and gaseous fuel, has good fuel tolerance, and described device also meets the application requirement simultaneously used solid fuel with gaseous fuel mixed combustion.
(4) the present invention is by adopting the particular design of two-stage gas nozzle, enhances the mixing intensity of inside reactor material, is conducive to total system and realizes higher operational efficiency, make use of the material participating in reaction more efficiently.
Accompanying drawing explanation
Fig. 1 is the present invention's double-fluidized-bed gas-solid burner structural representation.
Fig. 2 is the structural representation of the reduction reactor that the present invention relates to.
Fig. 3 is the structural representation of the bottom material-returning device that the present invention relates to.
Wherein have: first jet 1, second nozzle 2, reduction reactor 3, reduction reactor cyclone separator 4, reduction reactor feeding screw 5, reduction reactor flash device 6, reduction reactor material returning device 7, reduction reactor material returning device left air compartment fluidized wind entrance 8, reduction reactor material returning device right air compartment fluidized wind entrance 9, reduction reactor material returning device returning charge inclined tube 10, oxidation reactor 11, oxidation reactor cyclone separator 12, reduction reactor material returning device 13, 3rd nozzle 14, 4th nozzle 15, oxidation reactor bottom fluidization wind entrance 16, lower material returning device 17, reduction reactor bottom fluidization wind entrance 18, condenser 19, high concentration CO 2 20, oxygen debt air 21, overflow inclined tube control valve 22.
Detailed description of the invention
Below in conjunction with accompanying drawing, technical scheme of the present invention is described in detail.
See Fig. 1-3, the double-fluidized-bed gas-solid burner of one provided by the invention, this device comprises reduction reactor 3 and oxidation reactor 11;
Reduction reactor 3 top is connected with reduction reactor cyclone separator 4, and reduction reactor cyclone separator 4 lower end is connected with side, reduction reactor material returning device 7 top, and reduction reactor cyclone separator 4 upper end is connected with condenser 19; Reduction reactor 3 middle and upper part is provided with overflow mechanism 6 and is connected with returning charge down-comer; Reduction reactor material returning device 7 is connected with oxidation reactor 11 by reduction reactor material returning device returning charge inclined tube 10; Oxidation reactor 11 top is connected with oxidation reactor cyclone separator 12, and oxidation reactor cyclone separator 12 lower end is connected with side, oxidation reactor material returning device 13 top; Oxidation reactor material returning device 13 is connected with bottom oxidation reactor 11; Oxidation reactor 11 and reduction reactor 3 connect and compose loop structure by bottom by lower material returning device 17, and screw feeder 5 is for giving reduction reactor 3 feed, and condenser 19 is connected with reduction reactor cyclone separator 4, for separating of output high concentration CO 2 20.
Reduction reactor 3 and oxidation reactor 11 are provided with two-stage gas nozzle at differing heights respectively.
Reduction reactor 3 is by making it to run on respectively bubbling fluidization state or turbulent fluidised state or fast fluidization state to valve switch set on flash device 6.
In described device, reduction reactor is provided with flash structure and gas-solid separating device, achieve the adaptability of reduction reactor to multiple duties such as bubbling fluidization state, turbulent fluidised state and fast fluidization states, by the adjustment of operational factor one in a big way in change the time of staying of mixed material in bed and mixed characteristic, make described reaction unit can adapt to the fuel of complicated kind.The valve on overflow pipe should be closed when reduction reactor is in fast fluidization state running status in described double-fluidized-bed device.
Reduction reactor in described device and oxidation reactor are provided with two-stage gas nozzle at differing heights respectively, pass into by classification the mixability that gas strengthens the material in reactor, make described device have good reaction efficiency.
Matter Transfer between two reactors of described device is controlled by the material returning device of pneumatic control, and feed flow can regulate according to both sides reactor actual operating state to improve reaction efficiency.Lower material returning device between double-reactor is arranged on the bottom of device, arrange inclined tube by reactor bottom to be connected with the upper end of lower material returning device, the requirement of returning charge amount when the resistance reducing Matter Transfer under controlled prerequisite makes described device can adapt to use different fuel and oxygen carrier.
The reduction reactor height of described device is H, and oxidation reactor height is L(0.8H ~ 1.2H); First jet height is 0.1H, and second nozzle height is 0.4H, and the 3rd nozzle height is 0.3L, and the 4th nozzle height is 0.1L; Reduction reactor flash open height is 0.6H ~ 0.7H; Reduction reactor spiral feed entrance should be arranged between first jet and second nozzle, is highly 0.2H ~ 0.3H; The material inlet height of being sent back to oxidation reactor by reduction reactor is 0.2L, and the material inlet height that oxidation reactor spiral material returning device returns is 0.05L; Reduction reactor internal diameter is D, and oxidation reactor internal diameter is 0.8D ~ D, and bottom is connected inclined tube internal diameter with lower material returning device is 0.4D, and reduction reactor overflow pipe internal diameter is 0.3D; Flash inclined tube and horizontal plane angle are 45 °, and bottom fluidization wind air distribution plate and horizontal plane angle are 30 °, and under bottom, material returning device connection inclined tube and horizontal plane angle are 45 °.
Present invention also offers a kind of double-fluidized-bed gas-solid combustion method, the method comprises the steps,
Solid fuel adds in reduction reactor 3 by material inlet by feeding screw 5, and gaseous fuel adds in reduction reactor 3 by reduction reactor first order jet nozzle 1; In reduction reactor 3 mixed material by by bottom reduction reactor 18 and first jet 1 and second nozzle 2 feed gas fluidized, the response characteristic of based on fuel is by fluidized state in the adjustment of fluidization gas and the switch adjustment reduction reactor 3 of overflow mechanism valve; Fuel mixes with the oxidation state oxygen carrier be fluidized and reacts, and is obtained by reacting the gaseous product be made up of CO2 and steam, and gaseous product is separated through cyclone separator 4 and exports, and after condenser 19 cools and removes moisture, the enrichment realizing CO2 catches; Reduction-state oxygen carrier to be sent back in the middle part of oxidation reactor 11 and by by bottom oxidation reactor 16 and the 3rd nozzle 14 and the 4th nozzle 15 feed gas fluidized, by utilizing the O contained in fluidizing gas
2occur oxidation reaction again obtain oxidation state oxygen carrier, with after after oxidation reactor cyclone separator 12 gas solid separation, oxidation state oxygen carrier is sent back to bottom oxidation reactor 11; Oxidized oxygen carrier comes back to reduction reactor 3 through lower material returning device 17, forms the circulation between double-fluidized-bed reactor.
Described method requires to make oxidation reactor run on fast fluidization state by controlling fluidization gas.The running status of reduction reactor then needs to adjust according to fuel used response characteristic, fluidization gas can be reduced for the fuel that reaction rate is relatively slow to make it to run on bubbling fluidization state, and along with the raising of fuel reaction speed, reduction reactor also can run on turbulent fluidization state and fast fluidization state by increasing fluidization gas.
Layered fluidized method in described method application fluid bed, strengthens gas-solid, the solid-solid blend intensity in each region in reactor by the fluidization gas of each layering of conservative control, play the effect improving reaction efficiency and accelerate reaction rate.
Described method requires that the operating temperature in reduction reactor is 800 ~ 1000 DEG C, and the operating temperature in oxidation reactor is 900 ~ 1100 DEG C.Should note preventing temperature from crossing and make high fuel ash melting cause fluidization operation difficulty.
Embodiment 1
Fuel selects coal and natural gas (main component is CH4), and iron ore selected by circulation fluidized bed material, and the oxidation state of oxygen carrier contained by it mainly exists with Fe2O3 form, and reduction-state then mainly exists with Fe3O4, FeO and Fe form.Because oxidation state oxygen carrier is relative very fast with coal dust, natural gas reaction rate under the design work condition of reduction reactor, make it as fast fluidization bed operating by closing the valve that reduction reactor overflow mechanism 6 is arranged, in reduction reactor, superficial gas velocity is set as 3.5 ~ 4m/s, and in oxidation reactor, superficial gas velocity is set as 4 ~ 4.5m/s.Reduction reactor fluidized wind tolerance is assigned as second nozzle 5% ~ 15%, first jet 45% ~ 55%, bottom fluidization wind entrance 35% ~ 45%, and oxidation reactor fluidized wind tolerance is assigned as the 4th nozzle 15% ~ 25%, the 3rd nozzle 35% ~ 45%, bottom fluidization wind entrance 35% ~ 45%.
Coal is admitted to reduction reactor 3 via reduction reactor feeding screw 5, and reduction reactor spiral charging rate is set as 0.5m/s, and natural gas mixes with fluidizing gas (steam) to be sent in reduction reactor 3 through first jet 1.Controlling temperature in reduction reactor 3 is 1000 ± 20 DEG C, and in controlled oxidization reactor 11, temperature is 900 ± 20 DEG C.
Coal and natural gas add after reduction reactor 3 with second nozzle 2, first jet 1 and reduction reactor bottom 18 steam passed into and oxidation state oxygen carrier fluidisation altogether, in the bed acutely mixed, material reacts.First there is pyrolysis and generate coke in coal, coke and steam react the synthesis gas that to generate with H2 and CO be main component, and synthesis gas and natural gas together react with oxidation state oxygen carrier and directly generate CO2 and steam in reduction reactor; Gaseous product (mainly CO2 and steam) exports from reduction reactor cyclone separator 4, exports high concentration CO 2 after isolating moisture in condenser 19, achieves separation and the seizure of CO2.
Reduction-state oxygen carrier, after reduction reactor cyclone separator 4 gas solid separation, to be admitted in reduction reactor material returning device 7 through down-comer, with after to be sent back to the middle part of oxidation reactor 11 through reduction reactor material returning device returning charge inclined tube 10.In oxidation reactor 11, reduction-state oxygen carrier (Fe3O4, FeO and Fe) by by 16 Air Fluidizeds sent into bottom oxidation reactor the 3rd nozzle 14, the 4th nozzle 15 and oxidation reactor, and in the process be oxidized by O2 in air and regenerate oxidation state oxygen carrier (Fe2O3).After oxidation reactor cyclone separator gas solid separation, oxygen debt air is overflowed by upper end, oxidation state oxygen carrier is then sent to bottom oxidation reactor through oxidation reactor material returning device 13, to flow in lower material returning device 17 subsequently, and be transferred to get back in reduction reactor 3 and carry out secondary response again, form the circulation of oxygen carrier.
The double-chamber structure of reduction reactor material returning device 7 for being interconnected, comprise pan feeding room and discharge chamber, can realize material between double-fluidized-bed reactor controlled circulation and in effective anti-locking apparatus gas alter mixed, can the flux of controlled circulation material by passing into fluidization gas flow in material returning device.
Embodiment 2
Adopt the device identical with embodiment 1, fuel selects coal and living beings fuel combination, selects Ni-based oxygen carrier (NiO).Because oxidation state oxygen carrier (NiO) and the reaction rate of described fuel combination under condition of work designed by reduction reactor are relatively slow, make it as bubbling fluidization bed operating by opening the valve that reduction reactor overflow mechanism 6 is arranged, in reduction reactor, superficial gas velocity is set as 0.4 ~ 0.6m/s, and in oxidation reactor, superficial gas velocity is set as 4 ~ 4.5m/s.Reduction reactor fluidized wind tolerance is assigned as second nozzle 5% ~ 15%, first jet 45% ~ 55%, bottom fluidization wind entrance 35% ~ 45%, and oxidation reactor fluidized wind tolerance is assigned as the 3rd nozzle 15% ~ 25%, the 4th nozzle 35% ~ 45%, bottom fluidization wind entrance 35% ~ 45%.
Fuel combination is admitted to reduction reactor 3 via reduction reactor feeding screw 5, and reduction reactor spiral charging rate is set as 0.5m/s.Controlling temperature in reduction reactor 3 is 1000 ± 20 DEG C, and controlled oxidization reactor 11 is 900 ± 20 DEG C.
The gaseous product (mainly CO2 and steam) that reduction reactor generates exports from reduction reactor cyclone separator 4, exports high concentration CO 2, realize separation and the seizure of CO2 in condenser 19 after isolating moisture.
Reduction-state oxygen carrier (Ni) is mixed with ash content after reduction reactor cyclone separator 4 gas solid separation, to be admitted in reduction reactor material returning device 7 through down-comer, with after to be sent back to the middle part of oxidation reactor 11 through the returning charge inclined tube 10 of reduction reactor material returning device.In oxidation reactor 11, reduction-state oxygen carrier (Ni) is oxidation state oxygen carrier (NiO) by O2 institute oxidation regeneration in air.After oxidation reactor cyclone separator gas solid separation, oxygen debt air is overflowed by upper end, oxidation state oxygen carrier is then sent to bottom oxidation reactor through oxidation reactor material returning device 13, to flow in lower material returning device 17 subsequently, and be transferred to get back in reduction reactor 3 and carry out secondary response again, form the circulation of oxygen carrier.
Claims (2)
1. a double-fluidized-bed gas-solid burner, is characterized in that, this device comprises reduction reactor (3) and oxidation reactor (11);
Reduction reactor (3) top is connected with reduction reactor cyclone separator (4), reduction reactor cyclone separator (4) lower end is connected with reduction reactor material returning device (7) side, top, and reduction reactor cyclone separator (4) upper end is connected with condenser (19); Reduction reactor (3) middle and upper part is provided with overflow mechanism (6) and is connected with returning charge down-comer; Reduction reactor material returning device (7) is connected with oxidation reactor (11) by reduction reactor material returning device returning charge inclined tube (10); Oxidation reactor (11) top is connected with oxidation reactor cyclone separator (12), and oxidation reactor cyclone separator (12) lower end is connected with oxidation reactor material returning device (13) side, top; Oxidation reactor material returning device (13) is connected with oxidation reactor (11) bottom; Oxidation reactor (11) connects and composes loop structure by bottom by lower material returning device (17) with reduction reactor (3), screw feeder (5) is for giving reduction reactor (3) feed, condenser (19) is connected with reduction reactor cyclone separator (4), for separating of output high concentration CO 2 (20);
Reduction reactor (3) and oxidation reactor (11) are provided with two-stage gas nozzle at differing heights respectively;
Reduction reactor (3) makes it to run on respectively bubbling fluidization state or turbulent fluidised state or fast fluidization state by the valve switch upper set to flash device (6).
2. a gas-solid combustion method for double-fluidized-bed gas-solid burner as claimed in claim 1, it is characterized in that, the method comprises the steps,
Solid fuel adds in reduction reactor (3) by material inlet by feeding screw (5), and gaseous fuel adds in reduction reactor (3) by reduction reactor first order jet nozzle (1); Reduction reactor (3) interior mixed material is gas fluidized by what fed by (18) bottom reduction reactor and first jet (1) and second nozzle (2), the adjustment of response characteristic by fluidization gas of based on fuel and switch adjustment reduction reactor (3) the interior fluidized state of overflow mechanism valve; Fuel mixes with the oxidation state oxygen carrier be fluidized and reacts, be obtained by reacting the gaseous product be made up of CO2 and steam, gaseous product is separated through cyclone separator (4) and exports, and after moisture is removed in condenser (19) cooling, the enrichment realizing CO2 catches; Reduction-state oxygen carrier is sent back to oxidation reactor (11) middle part and gas fluidized by what fed by (16) bottom oxidation reactor and the 3rd nozzle (14) and the 4th nozzle (15), by utilizing the O contained in fluidizing gas
2occur oxidation reaction again obtain oxidation state oxygen carrier, with after after oxidation reactor cyclone separator (12) gas solid separation, oxidation state oxygen carrier be sent back to oxidation reactor (11) bottom; Oxidized oxygen carrier comes back to reduction reactor (3) through lower material returning device (17), forms the circulation between double-fluidized-bed reactor.
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| CN104401938B (en) * | 2014-10-31 | 2016-04-20 | 东南大学 | Be rich in methane gas and prepare H 2the apparatus and method of the synthetic gas that/CO ratio is adjustable |
| CN105333439B (en) * | 2015-11-08 | 2020-03-31 | 广东博业热能供应有限公司 | Secondary high-temperature gasification incineration system for garbage |
| CN106247323B (en) * | 2016-09-14 | 2019-01-18 | 东南大学 | A kind of chemical chain combustion apparatus and its method based on tower bubbling fluidized bed fuel reactor |
| CN113719843B (en) * | 2021-08-12 | 2022-09-09 | 中国矿业大学 | Method for recycling low-concentration gas resources |
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