CN203147748U - Solid fuel chemical-looping combustion device of circulating fluidized bed - Google Patents
Solid fuel chemical-looping combustion device of circulating fluidized bed Download PDFInfo
- Publication number
- CN203147748U CN203147748U CN2013200676123U CN201320067612U CN203147748U CN 203147748 U CN203147748 U CN 203147748U CN 2013200676123 U CN2013200676123 U CN 2013200676123U CN 201320067612 U CN201320067612 U CN 201320067612U CN 203147748 U CN203147748 U CN 203147748U
- Authority
- CN
- China
- Prior art keywords
- fuel
- oxygen
- reactor
- air
- reaction device
- 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
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 solid fuel chemical-looping combustion device of a circulating fluidized bed. The solid fuel chemical-looping combustion device is characterized by comprising an air reactor, a cyclone separator, an oxygen generator, a fuel reactor and an overflow groove, wherein the bottom of the air reactor is externally connected with air, and the top of the air reactor is connected with the cyclone separator; an exhaust port is formed in the top of the cyclone separator, and the bottom of the cyclone separator is connected with the top of the oxygen generator arranged in the fuel reactor; the bottom of the oxygen generator is connected with the top of the overflow groove, and the oxygen generator is connected with the bottom of the fuel reactor from the exterior of the fuel reactor; an air outlet is formed in the top of the fuel reactor, and a feeding port is formed in the bottom of the fuel reactor; the bottom of the overflow groove is connected with an inclined downcomer which is connected with the bottom of the air reactor, and the bottom of the overflow groove is externally connected with water steam; and a slag removal port for removing slag is formed in the bottom of the fuel reactor. The solid fuel chemical-looping combustion device can be used for realizing the complete separation between solid fuels and oxygen carriers as well as the sufficient and rapid combustion reaction of the solid fuels and meanwhile has the advantages of being capable of effectively separating CO2 and reducing the emission of greenhouse gases.
Description
Technical field
The utility model relates to a kind of device that utilizes burning chemistry chains, relates in particular to a kind of chemical chain combustion apparatus that uses solid fuel and make its generation pressurization conflagration reaction.
Background technology
The global warming issue that greenhouse gas emission brings is causing people's attention.CO
2As topmost greenhouse gases, research CO
2Emission-reduction technology is extremely urgent.CO in the flue gas
2Usually by a large amount of nitrogen dilutions, CO
2Separation and cost recovery very high.In combustion process, generate the CO of high concentration
2Or be convenient to CO
2The gas phase mixture that separates, generation, the discharging of eliminating other pollutant simultaneously are effective ways.A kind of novel combustion system that burning chemistry chains (Chemical-Looping Combustion is called for short CLC) has above-mentioned characteristic just has been subjected to more concern.Chemical chain burning technology in nineteen eighty-three first by propositions such as Ritcher, basic principle is that traditional fuel and the direct catalytic burning of air are decomposed into 2 gas-solid reactions by means of the effect of oxygen carrier, fuel need not to contact with air, by oxygen carrier airborne oxygen is delivered in the fuel.The burning chemistry chains mode is direct combustion decomposition the indirect burning of two-step reaction, has realized the graded utilization of energy, has improved energy utilization rate.The CO that generates in the fuel reaction device
2Avoided and the mixing of excess air or nitrogen, can guarantee quite high concentration.Main gas componant in the fuel reaction device is CO
2And H
2O, separation of C O
2Only need be with H
2O carries out condensation, removal, does not need the consumption of energy and the layout of separator.In combustion process, air and fuel through 2 different reactors, have been avoided fuel type NO respectively
XGeneration.Compare with conventional ignition temperature, combustion reactor and air fuel reactor running temperature are lower, have effectively controlled heating power type NO
XGeneration.Therefore, the burning chemistry chains mode is a kind of solid fuel processing mode and CO that has very much future
2Trapping technique, and become one of current research focus.
In traditional burning chemistry chains method, usually the carrier of oxygen from air reactor is directly entered fuel reaction device and solid fuel and carry out the living reaction of hybrid concurrency.But if the carrier of oxygen is directly contacted mixing with solid fuel, in combustion process, the ash content in the solid fuel is difficult to separate with the carrier of oxygen.These ash contents can directly be attached to carrier of oxygen surface, cause the activity of the carrier of oxygen to descend, and deactivation phenomenom takes place when serious.Simultaneously, being difficult to separate of the carrier of oxygen and ash content must cause when deslagging can the discharge section carrier of oxygen, causes carrier of oxygen unnecessary loss, has increased operating cost.
Summary of the invention
To be solved in the utility model is existing chemical chain combustion apparatus, being difficult to separate of the carrier of oxygen and ash content must cause when deslagging can the discharge section carrier of oxygen problem.
The utility model provides a kind of solid fuel ciculation fluidized bed chemical chain combustion apparatus, it is characterized in that, comprises air reactor, the external air in the bottom of air reactor, and the top connects cyclone separator; The top of cyclone separator is provided with exhaust outlet, and the bottom is connected at the top of the oxygen generator in the fuel reaction device; The bottom of oxygen generator connects the top of overflow launder, and oxygen generator connects the bottom of fuel reaction device from the outside of fuel reaction device; The combustion reactor top is provided with for discharging CO
2With the gas outlet of steam, the bottom is provided with for adding solid-fuelled charge door; Isopipe root connects the inclination down-comer, and the inclination down-comer is connected with the bottom of air reactor, the external steam of isopipe root; Fuel reaction device bottom is provided with the slag-drip opening for ash discharge.
The utility model belongs to chemical chain burning technology, has the general advantage of burning chemistry chains.Fuel is handled by the mode of burning chemistry chains, has realized CO in the whole circulation process naturally
2With separating of air, and do not need extra from air the energy consumption of oxygen separation.This point is compared with the oxygen-enriched combustion technology that developed recently gets up, and has saved a large amount of energy consumptions required in air separation plant and the pure oxygen preparation process, has directly increased substantially the efficient of system.Simultaneously, in chemical chain circulation, combustion process, because heat transfer temperature difference is low, the fire of system further improves the service efficiency of system capacity with loss.
The carrier of oxygen is for discharging the carrier of oxygen of oxygen molecule, and the carrier of oxygen of lower valency enters air reactor by the inclination down-comer after flowing out from overflow launder; Air feeds from the air reactor bottom, fully mixes, reacts with the carrier of oxygen of lower valency, and the carrier of oxygen of lower valency is formed the carrier of oxygen of high valence state by airborne dioxygen oxidation; The carrier of oxygen of high valence state by gas lift to the cyclone separator place, separation through cyclone separator, the air that contains trace oxygen flows out from gas outlet, cyclone separator top, and the carrier of oxygen of high valence state enters oxygen generator by the tremie pipe of cyclone separator bottom; The carrier of oxygen of the high valence state in the oxygen generator is through the burning exothermic reaction heating of oxygen generator outside, and discharging oxygen (is O
2Molecule), the carrier of oxygen of high valence state of while changes the carrier of oxygen of lower valency into; The lower valency carrier of oxygen flows out from the pipeline of oxygen generator bottom, and the process overflow launder comes back in the air reactor, and oxidation by air, regenerates the carrier of oxygen of high valence state, has realized the recycling of the carrier of oxygen.The bottom of overflow launder feeds the conveying that steam guarantees the carrier of oxygen.The oxygen that generates in oxygen generator is drawn the fuel reaction device earlier by pipeline, guides to fuel reaction device lower end again and feeds the fuel reaction device; Except oxygen, fuel reaction device lower end also feeds steam, and the feeding mode can be to mix earlier to feed again, and also can all feed from separately spout for steam and oxygen; Solid fuel joins in the fuel reaction device continuously by screw feeder; Solid fuel is in the bubbling fluidization state in the fuel reaction device; Solid fuel at first pyrolysis generates coke, and coke reacts with steam generating gasification on every side, generates with H
2With CO be main flammable synthesis gas, solid fuel and the oxygen generation combustion reaction of synthesis gas and not gasification also discharges heat, this heat keep the fuel reaction device required heat and the required heat of oxygen generator generation oxygen of reaction temperature, solid fuel gasification; The ash that solid fuel ignition and gasification produce is discharged from the slag-drip opening of fuel reaction device bottom; The CO that the fuel reaction device produces
2Discharge from the gas outlet on fuel reaction device top with steam, through condensation will be wherein moisture from after, obtain the very high CO of purity
2Thereby, realize CO
2Separation and seizure; The temperature of air reactor and fuel reaction device is all controlled at 900～1100 ℃.
In the utility model, the high price carrier of oxygen discharges oxygen under the situation of being heated, and becomes the carrier of oxygen at a low price.The carrier of oxygen does not contact with solid fuel at a low price, but the overflow launder of flowing through comes back in the air reactor.The oxygen that discharges mixes the back and feeds the fuel reaction device from the bottom with steam.This has fundamentally been avoided the carrier of oxygen to contact with solid-fuelled, thus the carrier of oxygen loss of having avoided carrier of oxygen inactivation and deslagging to cause.
The utility model has realized that not only solid fuel and the thorough of the carrier of oxygen separate, and has also realized solid-fuelled abundant, conflagration reaction, also has effectively separation of C O simultaneously
2, the advantage of minimizing greenhouse gas emission.
Description of drawings
The schematic diagram of the ciculation fluidized bed chemical chain combustion apparatus of solid fuel that Fig. 1 provides for the utility model.Among the figure:
The 1-air reactor; The 2-cyclone separator; 3-fuel reaction device;
The 4-oxygen generator; The 5-charge door; The 6-overflow launder;
7-inclination down-comer; The A-air; B-steam;
C-pressure (hydraulic) water steam; The D-slag-drip opening; E-oxygen;
The F-gas outlet; The G-exhaust outlet.
The specific embodiment
For the utility model is become apparent, now with preferred embodiment, and conjunction with figs. is described in detail below.
Embodiment
Be illustrated in figure 1 as the schematic diagram of the ciculation fluidized bed chemical chain combustion apparatus of solid fuel that the utility model provides, comprise air reactor 1, the external air A in the bottom of air reactor 1, the top connects cyclone separator 2.The top of cyclone separator 2 is provided with exhaust outlet G, and the bottom is connected at the top of the oxygen generator 4 in the fuel reaction device 3.The bottom of oxygen generator 4 connects the top of overflow launder 6, oxygen generator 4 connects the bottom of fuel reaction device 3 from the outside of fuel reaction device 3, the mode that oxygen E enters fuel reaction device 3 can be directly to enter, also can with enter again after the pressure (hydraulic) water vapor C is mixed.Combustion reactor 3 tops are provided with for discharging CO
2With the gas outlet F of steam, the bottom is provided with for adding solid-fuelled charge door 5.Overflow launder 6 bottoms connect inclination down-comer 7, and inclination down-comer 7 is connected with the bottom of air reactor 1, the external steam B in overflow launder 6 bottoms.Fuel reaction device 3 bottoms are provided with the slag-drip opening D for ash discharge.
In overflow launder 6, add carrier of oxygen Cu
2O, Cu
2O enters air reactor 1 by inclination down-comer 7 after flowing out from overflow launder 6; Air A feeds from air reactor 1 bottom, with Cu
2O fully mixes, reacts, Cu
2O is formed CuO by the dioxygen oxidation among the air A; CuO to cyclone separator 2 places, through the separation of cyclone separator 2, is contained the air of trace oxygen from the exhaust outlet G outflow on cyclone separator 2 tops by gas lift, and CuO enters oxygen generator 4 by the tremie pipe of cyclone separator 2 bottoms; CuO in the oxygen generator 4 is through the burning exothermic reaction heating of oxygen generator 4 outsides, and discharging oxygen (is O
2Molecule), the CuO body changes Cu into simultaneously
2O; Cu
2O flows out from the pipeline of oxygen generator 4 bottoms, comes back in the air reactor 1 through overflow launder 6, and by air A oxidation, regenerates CuO, has realized the recycling of the carrier of oxygen.
Overflow launder 6 bottoms feed steam B, guarantee Cu
2The conveying of O.The oxygen E that generates in oxygen generator 4 draws fuel reaction device 3 earlier by pipeline, guides to fuel reaction device 3 lower ends again and feeds fuel reaction device 3; Solid fuel joins the fuel reaction device 3 from charge door 5 continuously by screw feeder, and fuel reaction device 3 lower ends feed pressure (hydraulic) water vapor C and oxygen E, and the spout of pressure (hydraulic) water vapor C and oxygen E is arranged in fuel reaction device 3 bottom equi-spaced apart; Solid fuel is in the bubbling fluidization state in fuel reaction device 3; Solid fuel at first pyrolysis generates coke, and coke reacts with steam generating gasification on every side, generates with H
2With CO be main flammable synthesis gas, solid fuel and the oxygen generation combustion reaction of synthesis gas and not gasification also discharges heat, this heat keep fuel reaction device 3 required heat and the required heat of oxygen generator 4 generation oxygen of reaction temperature, solid fuel gasification; The ash that solid fuel ignition and gasification produce is discharged from the slag-drip opening D of fuel reaction device bottom; The CO that fuel reaction device 3 produces
2Discharge from the gas outlet F on fuel reaction device 3 tops with steam, through condensation will be wherein moisture from after, obtain the very high CO of purity
2Thereby, realize CO
2Separation and seizure; The temperature of air reactor 1, oxygen generator 4 and fuel reaction device 3 is all controlled at 900～1100 ℃.
Claims (1)
1. the ciculation fluidized bed chemical chain combustion apparatus of solid fuel is characterized in that, comprises air reactor (1), the external air in bottom (A) of air reactor (1), and the top connects cyclone separator (2); The top of cyclone separator (2) is provided with exhaust outlet (G), and the bottom is connected at the top of the oxygen generator (4) in the fuel reaction device (3); The bottom of oxygen generator (4) connects the top of overflow launder (6), and oxygen generator (4) connects the bottom of fuel reaction device (3) from the outside of fuel reaction device (3); Combustion reactor (3) top is provided with for discharging CO
2With the gas outlet (F) of steam, the bottom is provided with for adding solid-fuelled charge door (5); Overflow launder (6) bottom connects inclination down-comer (7), and inclination down-comer (7) is connected with the bottom of air reactor (1), overflow launder (6) bottom external steam (B); Fuel reaction device (3) bottom is provided with the slag-drip opening (D) for ash discharge.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013200676123U CN203147748U (en) | 2013-02-05 | 2013-02-05 | Solid fuel chemical-looping combustion device of circulating fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013200676123U CN203147748U (en) | 2013-02-05 | 2013-02-05 | Solid fuel chemical-looping combustion device of circulating fluidized bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203147748U true CN203147748U (en) | 2013-08-21 |
Family
ID=48975268
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013200676123U Expired - Lifetime CN203147748U (en) | 2013-02-05 | 2013-02-05 | Solid fuel chemical-looping combustion device of circulating fluidized bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203147748U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107143848A (en) * | 2017-06-07 | 2017-09-08 | 华中科技大学 | A kind of coal gasification burning chemistry chains system in situ of coupling chemistry chain oxygen |
-
2013
- 2013-02-05 CN CN2013200676123U patent/CN203147748U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107143848A (en) * | 2017-06-07 | 2017-09-08 | 华中科技大学 | A kind of coal gasification burning chemistry chains system in situ of coupling chemistry chain oxygen |
| CN107143848B (en) * | 2017-06-07 | 2019-03-08 | 华中科技大学 | A kind of coal gasification burning chemistry chains system in situ of coupling chemistry chain oxygen |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102200277B (en) | Chemical chain combustion method and device through solid fuel | |
| CN101699187B (en) | Coal combustion apparatus capable of separating carbon dioxide and separation method thereof | |
| CN103062910B (en) | Method and device for integrating chemical-looping combustion with CO<2> trapping | |
| CN102796561B (en) | Anaerobic gasification method and device for biomass fuels by carbon dioxide circulation | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN101570315B (en) | Method and device for producing hydrogen through biomass gasification by using single fluidized bed and two-step method | |
| CN103742899A (en) | Oxygen-enriched combustion circulating fluidized bed poly-generation system and process | |
| CN102198934A (en) | Method and device for producing hydrogen by using chemical chain | |
| CN103320175B (en) | High-efficiency clean low-carbon coal graded utilization method and device | |
| CN101638590A (en) | Method for producing synthesis gas by combustible solid waste chemical chain gasification and interconnected fluidized bed reactor | |
| CN103496672B (en) | Device and process for preparing O2-CO2 mixed gas based on chemical-looping technology | |
| CN102191089A (en) | Two-stage high-temperature preheated steam biomass gasification furnace | |
| CN202546743U (en) | Solid fuel chemical looping combustion system based on three-bed-structured fuel reactor | |
| CN110255499A (en) | Biomass cracking gases hydrogen production process, device and its control system | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN106196027A (en) | The multi-cell fluidized bed device that a kind of solid fuel chemistry chain converts | |
| CN108795505B (en) | Coal powder hydro-gasification method and system | |
| CN103484134B (en) | Solid heat carrier-based destructive distillation reactor and method of raw hydrocarbon | |
| CN100436940C (en) | Coal-burning installation based on calcium sulphate oxygen carrier and coal burning method | |
| CN106398766A (en) | Method for enhancing tar removal and CO2 trapping of chemical-chain-gasification hydrogen production process | |
| CN102589147B (en) | Method for combusting solid fuel by chemical looping and device thereof | |
| CN101747947A (en) | Gasification complex reaction device of pyrolysis fluidized bed of biomass moving bed | |
| CN104204674A (en) | Method and apparatus for oxidation of unburnts | |
| CN202546742U (en) | Two-stage double-bed reactor-based solid fuel chemical-looping combustion system | |
| CN102798222A (en) | Chemical-looping combustion device based on solid fuel and use method thereof |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130821 |
|
| CX01 | Expiry of patent term |