CN102200277A - Chemical chain combustion method and device through solid fuel - Google Patents
Chemical chain combustion method and device through solid fuel Download PDFInfo
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- CN102200277A CN102200277A CN2011101067965A CN201110106796A CN102200277A CN 102200277 A CN102200277 A CN 102200277A CN 2011101067965 A CN2011101067965 A CN 2011101067965A CN 201110106796 A CN201110106796 A CN 201110106796A CN 102200277 A CN102200277 A CN 102200277A
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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 method and a chemical chain combustion device through solid fuel. The method comprises the following steps that: an oxygen carrier Cu is oxidized by air in an air reactor to form CuO, and the CuO enters an oxygen release reactor and is decomposed to form Cu2O and release molecular oxygen O2; the Cu2O is accumulated in the oxygen release reactor and returns to the air reactor through a discharging pipe of the oxygen release reactor and an overflow tank, and the Cu2O is oxidized to form CuO again, and the CuO is recycled; and the molecular oxygen O2 released from the oxygen release reactor enters a fuel reactor and is subjected to a combustion reaction with fuel in the fuel reactor, gaseous products in the fuel reactors are CO2 and water vapor only, and after the water is condensed and separated, pure CO2 is obtained. The heat generated in the whole system is equal to the heat obtained by fuel combustion in the air, but CO2 is separated inherently.
Description
Technical field
The present invention relates to a kind of method and apparatus of burning chemistry chains, relate in particular to a kind of burning chemistry chains and separation of C O of using solid fuel
2Method and device thereof.
Background technology
Since industrial civilization, the CO in the earth atmosphere
2Concentration sharply rises owing to the Human's production activity.CO
2As a kind of typical greenhouse gases, directly cause greenhouse effects.Along with Global climate change is remarkable day by day in recent years, CO
2Capture the hot issue that becomes the current energy and environmental science research with (CCS) technology of sealing up for safekeeping.Burning chemistry chains is a kind of CO that grows up the eighties in 20th century
2The separation and collection technology.The burning chemistry chains process is finished in two reactors, and one is air reactor, and another is the fuel reaction device, and the solid matter that circulates in two reactors is called oxygen carrier.In air reactor, the oxygen carrier of lower valency is become high valence state by airborne dioxygen oxidation, and oxygen carrier obtains oxygen; The oxygen carrier of high valence state enters the fuel reaction device, is reduced by fuel gas in the fuel reaction device, and promptly oxygen carrier discharges oxygen, and oxygen carrier is come back to by high valence state and is that lower valency, the gaseous product of fuel reaction device are steam and CO
2, condensation separation obtains pure CO after going out wherein water
2, realize CO
2Separation; The oxygen carrier of lower valency is got back to air reactor and is carried out circulation next time.The total reaction of burning chemistry chains still is the aerial combustion reaction of fuel, and this circulation is still passed through in acquisition and the heat that fuel burns and equates in air, and the burning chemistry chains process has realized CO
2The inherence separate and do not need extra energy consumption.Therefore, burning chemistry chains is a kind of CO with future
2Trapping technique also becomes one of current research focus.
Summary of the invention
The invention provides a kind of method and apparatus of the burning chemistry chains that uses solid fuel.The present invention effective separation of C O when realizing solid fuel ignition
2, have the advantage that reduces greenhouse gas emission.
Technical scheme of the present invention is as follows:
A kind of method of the burning chemistry chains that uses solid fuel, the oxygen carrier Cu of lower valency is inserted in the air reactor, at air reactor bottom bubbling air, air reactor is in the fast fluidized bed state, the temperature of air reactor is controlled at 900-950 ℃, Cu is oxidation by air in air reactor, generates the CuO of high valence state; CuO by air-lift unit to cyclone separator; Gas-solid is through separating, and oxygen debt air is overflowed from the outlet of cyclone separator, and CuO enters the oxygen release reactor by the cyclone separator tremie pipe; The temperature of oxygen release reactor is controlled at 900-950 ℃; In the oxygen release reactor, CuO discharges molecular oxygen O
2Oxygen carrier is got back to the Cu of lower valency from the CuO of high valence state
2O; O
2Overflow from the outlet of oxygen release reactor, enter the fuel reaction device, Cu
2O gets back in the air reactor by oxygen release reactor tremie pipe and overflow launder, and oxidation by air, regenerates the CuO of high valence state, and oxygen carrier is realized recycling; Coal is added the fuel reaction device by screw feeder, and the lower end of fuel reaction device feeds steam, and the fuel reaction device is in bubbling fluidization; The temperature of fuel reaction device is controlled at 900-950 ℃, and pyrolysis of coal generates coke, and coke and the reaction of steam generating gasification generate with H
2With CO be the synthesis gas of main component; The coke of synthesis gas and not gasification with from the oxygen O of oxygen release reactor outlet
2Combustion reaction takes place, discharge heat, this heat is kept fuel reaction actuator temperature and the required heat absorption of gasification reaction; The ash that produces in gasification and the combustion process is discharged by the slag-drip opening of fuel reaction device bottom; The gaseous product of fuel reaction device is CO
2With steam, CO
2Overflow from fuel reaction device outlet with steam, condensation separation obtains pure CO after going out wherein water
2, realize CO
2Separation and capture.
Device technique scheme of the present invention is as follows:
A kind of device that is used for the method for the above-mentioned burning chemistry chains that uses solid fuel is made up of air reactor, cyclone separator, cyclone separator tremie pipe, fuel reaction device, oxygen release reactor, screw feeder, oxygen release reactor tremie pipe and overflow launder; The top of air reactor links to each other with the import of cyclone separator; The lower end of cyclone separator is the cyclone separator tremie pipe; The cyclone separator tremie pipe passes the top of fuel reaction device and inserts in the oxygen release reactor; The oxygen release reactor places the inside of fuel reaction device; The bottom that oxygen release reactor tremie pipe passes the fuel reaction device links to each other with overflow launder; On the oxygen release reactor, be provided with oxygen outlet and oxygen outlet and be positioned at the fuel reaction device; Overflow launder links to each other with the lower end of air reactor; The bottom of overflow launder is provided with the loosening mouth that divides; The bottom of fuel reaction device is provided with steam mouth and slag-drip opening; The lower end side of fuel reaction device links to each other with screw feeder.
Compared with prior art, the present invention has following advantage:
(1), the invention belongs to chemical chain burning technology, inherited the advantage of burning chemistry chains.Present industrial mature C O
2Isolation technics has the MDEA absorption method, and the major defect of MDEA absorption method is the complex manufacturing of amine absorber, and is with high costs; Amine absorber is poisonous simultaneously, and it can produce harm to operating personnel's health inevitably in production and use, and environment is caused secondary pollution.The oxygen-enriched combusting that new development is in recent years got up also is a kind of effective CO
2The separation and collection technology, but the air separation unit of oxygen-enriched combusting needs a large amount of energy consumptions in the preparation process of pure oxygen, directly reduce whole system efficient.Fuel is utilized by the mode of burning chemistry chains, and the heat that fuel discharges in the process of burning chemistry chains equates with the heat that the aerial burning of fuel discharges, but the burning chemistry chains process has realized CO inherently
2Separation and do not need extra energy consumption, it will be further appreciated that in utilizing the heat of burning chemistry chains, because heat transfer temperature difference is low, the of system loss reduces, the energy service efficiency of system is improved.
(2), in the burning chemistry chains of classics, directly enter the fuel reaction device from the oxygen carrier of air reactor and participate in reaction.The fuel reaction device adopts gaseous fuel usually, such as natural gas or synthesis gas.But it is the country of main fuel with the coal that China is one, and the reserves of natural gas are far below coal.If coal is obtained synthesis gas by gasification, again synthesis gas is sent into the reaction of fuel reaction device, this needs extra gasification installation, directly causes the increase of equipment investment and operating cost.Coal is directly sent into the fuel reaction device, allow the reduction of fuel gasification and oxygen carrier in same reactor, carry out, this also is to use a kind of method of solid fuel chemistry chain burning, but directly solid fuel is sent into the fuel reaction device, ash content in the solid fuel is difficult to separate with oxygen carrier, these ash contents can directly stick to the oxygen carrier surface, cause the oxygen carrier inactivation; Simultaneously, the fuel reaction device that uses solid fuel is in the process of deslagging, because ash content is difficult to separate with oxygen carrier, thus will inevitably the discharge section oxygen carrier in the process of deslagging, caused the loss of oxygen carrier, increased the cost of investment of oxygen carrier.The present invention is built-in oxygen release reactor in the fuel reaction device, according to the thermodynamical equilibrium characteristic of CuO oxygen carrier, discharges molecular oxygen O in the oxygen release reactor of CuO oxygen carrier in low oxygen partial pressure environment
2, the oxygen after the release enters in the fuel reaction device and gasification product and solid fuel generation combustion reaction again.Solid fuel can not directly contact with oxygen carrier, avoided the ash content in the fuel reaction device to pollute oxygen carrier and cause its inactivation, fuel reaction device lower end is provided with slag-drip opening simultaneously, and the material that slag-drip opening is discharged only is the reacted ash content of solid fuel, oxygen carrier has not been saved the oxygen carrier resource.According to HSC Chemistry software simulation, 2CuO 2Cu
2O+O
2The equilibrium partial pressure of oxygen is 2% in the time of 900 ℃, and in air reactor, concentration of oxygen is 21% in the inlet air, and oxygen carrier exists with the form of CuO, in fuel reaction device and oxygen release reactor-side, because fuel can be with the O that discharges in the oxygen carrier
2Complete reaction causes the partial pressure of oxygen of oxygen release reactor extremely low (＜＜2%), and the CuO that newly enters in the oxygen release reactor is decomposed into Cu immediately
2O, and discharge molecular oxygen O
2Supply with the combustion reaction in the fuel reaction device, during greater than the reduction reaction stoichiometric number of CuO (CuO can provide enough oxygen), the gas of fuel reaction device outlet only is CO in the internal circulating load of CuO
2With steam.
(3), the internal circulating load of this reactor by changing oxygen carrier can the fuel metering reactor outlet gas composition, realize multiple use.The oxygen that provides when oxygen carrier is during greater than the required stoichiometric number of fuel completing combustion, and fuel is realized completing combustion, and the gaseous product of fuel reaction device outlet only is CO
2And steam, realize CO
2Capture.The hypoxgia that provides when oxygen carrier, when promptly being lower than the stoichiometric number of fuel completing combustion, because the fuel reaction device feeds steam down, solid fuel reacts main generating gasification, the oxygen that oxygen carrier provides only is used for the combustion parts synthesis gas, the heat that discharges is kept gasification reaction, so the outlet of fuel reaction device is with H
2With CO be the synthesis gas of main component, realized producing of synthesis gas.
Description of drawings
Fig. 1 is the use solid fuel installation drawing of burning chemistry chains of the present invention.
The specific embodiment
Embodiment 1
A kind of method of the burning chemistry chains that uses solid fuel, the oxygen carrier Cu of lower valency is inserted in the air reactor 1, at air reactor bottom A bubbling air, air reactor 1 is in the fast fluidized bed state, the temperature of air reactor 1 is controlled at 900 ℃, Cu oxidation by air in air reactor 1 generates the CuO of high valence state; CuO by air-lift unit to cyclone separator 2; Gas-solid is through separating, and oxygen debt air is overflowed from the outlet G of cyclone separator, and CuO enters oxygen release reactor 5 by cyclone separator tremie pipe 3; The temperature of oxygen release reactor 5 is controlled at 900 ℃; In oxygen release reactor 5, CuO discharges molecular oxygen O
2Oxygen carrier is got back to the Cu of lower valency from the CuO of high valence state
2O; O
2Overflow from the outlet E of oxygen release reactor, enter fuel reaction device 4, Cu
2O gets back in the air reactor 1 by oxygen release reactor tremie pipe 7 and overflow launder 8, and oxidation by air, regenerates the CuO of high valence state, and oxygen carrier is realized recycling; Coal is added fuel reaction device 4 by screw feeder 6, and the lower end C of fuel reaction device feeds steam, and fuel reaction device 4 is in bubbling fluidization; The temperature of fuel reaction device 4 is controlled at 950 ℃, and pyrolysis of coal generates coke, and coke and the reaction of steam generating gasification generate with H
2With CO be the synthesis gas of main component; The coke of synthesis gas and not gasification with from the oxygen O of oxygen release reactor outlet E
2Combustion reaction takes place, discharge heat, this heat is kept fuel reaction actuator temperature and the required heat absorption of gasification reaction; The ash that produces in gasification and the combustion process is discharged by the slag-drip opening D of fuel reaction device bottom; The gaseous product of fuel reaction device 4 is CO
2With steam, CO
2Overflow from fuel reaction device outlet F with steam, condensation separation obtains pure CO after going out wherein water
2, realize CO
2Separation and capture; As accompanying drawing 1; Feed the loosening elegance steam of the bottom B of overflow launder 8.
Embodiment 2
A kind of device of the burning chemistry chains method that is used to realize to use solid fuel is made up of air reactor 1, cyclone separator 2, cyclone separator tremie pipe 3, fuel reaction device 4, oxygen release reactor 5, screw feeder 6, oxygen release reactor tremie pipe 7 and overflow launder 8; The top of air reactor 1 links to each other with the import of cyclone separator 2; The lower end of cyclone separator 2 is a cyclone separator tremie pipe 3; Cyclone separator tremie pipe 3 passes the top of fuel reaction device 4 and inserts in the oxygen release reactor 5; Oxygen release reactor 5 places the inside of fuel reaction device 4; The bottom that oxygen release reactor tremie pipe 7 passes fuel reaction device 4 links to each other with overflow launder 8; On oxygen release reactor 5, be provided with oxygen outlet E and oxygen outlet E is positioned at fuel reaction device 4; Overflow launder 8 links to each other with the lower end of air reactor 1; The bottom B of overflow launder 8 is provided with the loosening mouth that divides; The bottom of fuel reaction device 4 is provided with steam mouth C and slag-drip opening D; The lower end side of fuel reaction device 4 links to each other with screw feeder 6; As accompanying drawing 1.
Claims (3)
1. the method for the burning chemistry chains that uses solid fuel, it is characterized in that: the oxygen carrier Cu of lower valency is inserted in the air reactor (1), at air reactor bottom (A) bubbling air, air reactor (1) is in the fast fluidized bed state, the temperature of air reactor (1) is controlled at 900-950 ℃, Cu oxidation by air in air reactor (1) generates the CuO of high valence state; CuO by air-lift unit to cyclone separator (2); Gas-solid is through separating, and oxygen debt air is overflowed from the outlet (G) of cyclone separator, and CuO enters oxygen release reactor (5) by cyclone separator tremie pipe (3); The temperature of oxygen release reactor (5) is controlled at 900-950 ℃; In oxygen release reactor (5), CuO discharges molecular oxygen O
2Oxygen carrier is got back to the Cu of lower valency from the CuO of high valence state
2O; O
2Overflow from the outlet (E) of oxygen release reactor, enter fuel reaction device (4), Cu
2O gets back in the air reactor (1) by oxygen release reactor tremie pipe (7) and overflow launder (8), and oxidation by air, regenerates the CuO of high valence state, and oxygen carrier is realized recycling; Coal is added fuel reaction device (4) by screw feeder (6), and the lower end of fuel reaction device (C) feeds steam, and fuel reaction device (4) is in bubbling fluidization; The temperature of fuel reaction device (4) is controlled at 900-950 ℃, and pyrolysis of coal generates coke, and coke and the reaction of steam generating gasification generate with H
2With CO be the synthesis gas of main component; The coke of synthesis gas and not gasification with from the oxygen O of oxygen release reactor outlet (E)
2Combustion reaction takes place, discharge heat, this heat is kept fuel reaction actuator temperature and the required heat absorption of gasification reaction; The ash that produces in gasification and the combustion process is discharged by the slag-drip opening (D) of fuel reaction device bottom; The gaseous product of fuel reaction device (4) is CO
2With steam, CO
2Overflow from fuel reaction device outlet (F) with steam, condensation separation obtains pure CO after going out wherein water
2, realize CO
2Separation and capture.
2. device of realizing the method for the described burning chemistry chains that uses solid fuel of claim 1, it is characterized in that, form by air reactor (1), cyclone separator (2), cyclone separator tremie pipe (3), fuel reaction device (4), oxygen release reactor (5), screw feeder (6), oxygen release reactor tremie pipe (7) and overflow launder (8); The top of air reactor (1) links to each other with the import of cyclone separator (2); The lower end of cyclone separator (2) is cyclone separator tremie pipe (3); Cyclone separator tremie pipe (3) passes the top of fuel reaction device (4) and inserts in the oxygen release reactor (5); Oxygen release reactor (5) places the inside of fuel reaction device (4); The bottom that oxygen release reactor tremie pipe (7) passes fuel reaction device (4) links to each other with overflow launder (8); On oxygen release reactor (5), be provided with oxygen outlet (E) and oxygen outlet (E) is positioned at fuel reaction device (4); Overflow launder (8) links to each other with the lower end of air reactor (1); The bottom (B) of overflow launder (8) is provided with the loosening mouth that divides; The bottom of fuel reaction device (4) is provided with steam mouth (C) and slag-drip opening (D); The lower end side of fuel reaction device (4) links to each other with screw feeder (6).
3. device according to claim 2 is characterized in that feeding the loosening elegance steam of the bottom (B) of overflow launder (8).
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3985547A (en) * | 1974-06-17 | 1976-10-12 | Centro Sperimentale Metallurgico S.P.A. | Iron ore reduction in multiple fluidized beds |
| CN101100284A (en) * | 2007-06-29 | 2008-01-09 | 清华大学 | Gas fuel oxygen-carried hydrogen-produced and carbon dioxide separation method and device |
| CN101666546A (en) * | 2009-09-30 | 2010-03-10 | 华中科技大学 | Pulverized coal combustion method and device with function of capturing CO2 |
| CN101830432A (en) * | 2010-05-14 | 2010-09-15 | 东南大学 | Method and device based on coal gasification for preparing hydrogen and separating CO2 |
| CN202101422U (en) * | 2011-04-27 | 2012-01-04 | 东南大学 | Device performing chemical-looping combustion by utilizing solid fuels |
-
2011
- 2011-04-27 CN CN2011101067965A patent/CN102200277B/en not_active Expired - Fee Related
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3985547A (en) * | 1974-06-17 | 1976-10-12 | Centro Sperimentale Metallurgico S.P.A. | Iron ore reduction in multiple fluidized beds |
| CN101100284A (en) * | 2007-06-29 | 2008-01-09 | 清华大学 | Gas fuel oxygen-carried hydrogen-produced and carbon dioxide separation method and device |
| CN101666546A (en) * | 2009-09-30 | 2010-03-10 | 华中科技大学 | Pulverized coal combustion method and device with function of capturing CO2 |
| CN101830432A (en) * | 2010-05-14 | 2010-09-15 | 东南大学 | Method and device based on coal gasification for preparing hydrogen and separating CO2 |
| CN202101422U (en) * | 2011-04-27 | 2012-01-04 | 东南大学 | Device performing chemical-looping combustion by utilizing solid fuels |
Non-Patent Citations (1)
| Title |
|---|
| 《锅炉技术》 20080930 秦翠娟等 化学链燃烧技术的研究进展 64-73 1-3 第39卷, 第5期 * |
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| CN113834897B (en) * | 2021-08-16 | 2023-11-24 | 东南大学 | Method and device for testing bulk oxygen migration dynamics in chemical chain technology |
| CN115143437A (en) * | 2022-06-30 | 2022-10-04 | 西安交通大学 | Solid fuel integrated gasification chemical-looping combustion combined cycle power generation system |
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