CN106975341A - A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor - Google Patents
A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor Download PDFInfo
- Publication number
- CN106975341A CN106975341A CN201710293779.4A CN201710293779A CN106975341A CN 106975341 A CN106975341 A CN 106975341A CN 201710293779 A CN201710293779 A CN 201710293779A CN 106975341 A CN106975341 A CN 106975341A
- Authority
- CN
- China
- Prior art keywords
- reactor
- steam
- calcium
- absorbing agent
- fluid bed
- 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.)
- Pending
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/81—Solid phase processes
- B01D53/83—Solid phase processes with moving reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a kind of device of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor, including fluid bed carbonation reactor, fluidized bed calcination decomposition reactor, fluidized bed steam activated reactor, fluid bed dehydration regeneration reactor, the first cyclone separator, the second cyclone separator, the first material returning device, the second material returning device, recycle stock heat exchanger, CO2Connecting pipe between heat exchanger, air gas separation unit and each several part；Using steam activation reactor active regeneration is carried out to inactivating CaO after calcining, by being hydrated dehydration reaction significantly absorbent regeneration pore structure and reaction surface, calcium-base absorbing agent activity can be significantly maintained, suppresses absorbent activity decline, the discharge of inactivation absorbent and fresh absorbent magnitude of recruitment is reduced；The heat of high-temperature flue gas and recycle stock is made full use of using heat exchanger, high-temperature oxygen, nitrogen and steam is produced, the heat-economy and energy utilization efficiency of carbon acquisition procedure is improved.
Description
Technical field
The present invention relates to removing CO2Device field, be exactly a kind of carrying vapour activated reactor calcium base absorb
The devices and methods therefor of agent circularly removing carbon dioxide.
Background technology
Aggravate for reply global warming with greenhouse effects, a large amount of CO that process discharges need to be utilized to fossil energy2Subtracted
Row and control, the recycle chemistry chain capture CO based on calcium-base absorbing agent2Technology is due to can be with fossil energy using PROCESS COUPLING
Receive much concern.Calcium base chemical chain technology circulation capture CO2It is divided into carbonating and two steps of calcining：Composition is mainly CaO's first
Calcium-base absorbing agent utilizes the CO in the flue gas of process generation in carbonation reactor with fossil fuel2Carry out carbonation reaction and
Form CaCO3, carbonation reactor outlet can obtain low CO2The flue gas of concentration；Then formed in carbonation reactor
CaCO3Decomposed after being heated into calcination reactor and discharge CO2, the reactor heat can by the pure oxygen burning of carbon-containing fuel or its
He supplies thermal source, and reactor outlet can obtain the CO of high concentration2, while absorbent calcining and decomposing is CaO and is recycled to carbonating
Reactor cycles are utilized.Calcium-base absorbing agent passes through carbonating-calcination reaction circulation capture CO2, CO in flue gas can be completed2Separation
And enrichment.The technical advantage is as follows：（1）Acquisition procedure can be coupled with fluidization；（2）CO2Capture temperature range higher, because
And recyclable high-grade waste heat and drive steam circulation, reduce by coupling calcium tape loop Lai loss in efficiency；（3）Calcium-base absorbing agent
Presoma lime stone and dolomite wide material sources and cheap；（4）Capture CO2Simultaneously can SO in cooperation-removal flue gas2；（5）Make
Absorbent after can be used for other industrial process, for example as the raw material of cement industry.
Current calcium base chemical chain carbon capture technique subject matter is：Calcium-base absorbing agent generation can not during high temperature circulation
Inverse crystal structure sintering, causes absorbent loose structure to be densified, so as to hinder CO2Participate in being carbonated into absorbent core
Reaction so that absorbent is inactivated, i.e. CO2Acquisition performance fails rapidly as cycle-index increases.
The content of the invention
It is an object of the invention to provide a kind of calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor
Devices and methods therefor.
Above-mentioned purpose is realized by following scheme：
A kind of device of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor, it is characterised in that：
Lost including fluid bed carbonation reactor, fluidized bed calcination decomposition reactor, fluidized bed steam activated reactor, fluid bed
Water reuse (treatment reactor, the first cyclone separator, the second cyclone separator, the first material returning device, the second material returning device, recycle stock heat exchange
Device, CO2Connecting pipe between heat exchanger, air gas separation unit and each several part；
The fluid bed carbonation reactor bottom sets smoke inlet, and middle and lower part sets solid circle material inlet, and top sets flue gas
Outlet；The fluidized bed calcination decomposition reactor bottom sets oxygen intake and scum pipe, and middle and lower part sets fresh absorbent, carbon respectively
Base fuel and solid circle material inlet, top sets exhanst gas outlet；The fluidized bed steam activated reactor middle and upper part sets solid
Material overfall；The fluid bed dehydration regeneration reactor middle and upper part sets solid material overfall；
On the flue gas pipeline connected with fluidized bed calcination decomposition reactor top exhanst gas outlet, if the first cyclone separator；The
One cyclone separator bottom is connected with material heat exchanger；Recycle stock heat exchanger exit is divided into two branch pipes, a branch pipe and stream
Change bed steam activation reactor, fluid bed dehydration regeneration reactor, the first material returning device to be sequentially connected, another branch pipe is returned with first
Glassware is joined directly together；First material returning device is connected with located at fluid bed carbonation reactor middle and lower part solid circle material inlet；The
CO is set at the top of one cyclone separator2Discharge pipe；CO2Discharge pipe and CO2Heat exchanger is connected；CO2Heat exchanger sets two-way cooling tube
It is respectively cryogenic oxygen and low temperature nitrogen from air gas separation unit in road, pipeline；Air gas separation unit sets air and entered respectively
Mouth, nitrogen outlet and oxygen outlet；Recycle stock heat exchanger sets cooling water inlet and steam (vapor) outlet；
On the flue gas pipeline connected with fluid bed carbonation reactor top exhanst gas outlet, if the second cyclone separator；Second
Cyclone separator bottom is connected to fluidized bed calcination decomposition reactor solid circle material inlet by the second material returning device；Second rotation point
Fume emission pipeline is set from device top.
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of carrying vapour activated reactor of described device, its feature
It is, including：
（1）Air feeding air gas separation unit is separated into oxygen and nitrogen, and oxygen is through CO2Heat exchanger is preheated to 500-900 DEG C
Feeding fluidized bed calcination decomposition reactor bottom is as fluidizing agent afterwards, while providing oxidant for carbon-based fuel burning；Nitrogen
Through CO2Feeding fluid bed dehydration regeneration reactor is as fluidizing agent after heat exchanger heating, while reacting heat supply for dehydration；
（2）Fluidized bed calcination decomposition reactor sets temperature to be 800-1000 DEG C, and calcium-base absorbing agent and the carbon-based fuel of supplement are sent
Enter reactor middle and lower part material inlet, carbon-based fuel and step（1）In preheated oxygen occur combustion reaction be calcium-base absorbing agent
Decompose heat supply；The high temperature CaO solid materials formed in calcination reactor are changed after being separated through the first cyclone separator in recycle stock
400-500 DEG C is cooled in hot device, subsequent CaO materials are divided into two parts, a part is delivered to fluid bed carbon through the first material returning device
Acidification reactor middle and lower part solid circle material inlet, another part is activated into fluidized bed steam activated reactor；It is useless
Solid is abandoned periodically to discharge by calcination reactor bottom scum pipe；
（3）Fluidized bed steam activated reactor sets temperature to be 300-400 DEG C, and fluidizing agent is steam；The one of step (2) generation
Part CaO in steam activation reactor with steam generation hydration reaction, the solid-state Ca (OH) of generation2Through solid material overfall
Send into fluid bed dehydration regeneration reactor；
（4）Fluid bed dehydration regeneration reactor sets temperature to be 500-650 DEG C, and fluidizing agent is the 500-650 that step (1) is produced
DEG C high temperature nitrogen, step (3) produce solid-state Ca (OH)2The heated dehydration in fluid bed dehydration regeneration reactor, formation
CaO absorbents are recycled to fluid bed carbonation reactor middle and lower part solid circle thing through solid material overfall and the first material returning device
Expect entrance；
（5）Fluid bed carbonation reactor sets temperature to be 650-750 DEG C, CaO and flue gas that step (2) and step (4) are produced
Middle CO2Generation carbonation reaction generates CaCO3, subsequent gas-solid mixture enter the second cyclone separator；Through the second cyclone separator
Solid particle delivers to fluidized bed calcination reactor through the second material returning device after separation, starts subsequent cycle and reuses, removes CO2Afterwards
Flue gas is discharged by the second separator top flue gas pipeline；First Cyclone outlet is carbon-based fuel pure oxygen burning and CaCO3
Decompose the high concentration CO of generation2, so as to realize CO in flue gas2Removing and enrichment.
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of described carrying vapour activated reactor, its feature exists
In：Step（1）The CO2It is respectively nitrogen and oxygen from air gas separation unit that heat exchanger, which is set in two-way cooling pipe, pipeline,
Gas.
A kind of method of the calcium-base absorbing agent circularly removing carbon dioxide of described carrying vapour activated reactor, its feature exists
In：Step（2）The recycle stock cooler uses water as cooling medium.
A kind of method of the calcium-base absorbing agent circularly removing carbon dioxide of described carrying vapour activated reactor, its feature exists
In：Step（2）The first material returning device fluidizing agent is steam, and steam is water cooling medium and high temperature in recycle stock cooler
Gasification is formed after material-heat-exchanging.
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of described carrying vapour activated reactor, its feature exists
In：Step（3）The fluidizing agent steam of the fluidized bed steam activated reactor is water cooling medium in recycle stock cooler
Formed with gasifying after high-temperature material heat exchange.
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of described carrying vapour activated reactor, its feature exists
In：Step（4）The second material returning device fluidizing agent is steam, and steam is water cooling medium and high temperature in recycle stock cooler
Gasification is formed after material-heat-exchanging
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of described carrying vapour activated reactor, it is characterised in that：Institute
State the artificial synthesized calcium-base absorbing agent that fresh absorbent is higher than 20% for lime stone, dolomite or other CaO mass percents.
A kind of calcium-base absorbing agent carbon dioxide recycle removal methods of described carrying vapour activated reactor, its feature exists
In：The carbon-based fuel is one kind in coal, biomass, natural gas, coal gas, synthesis gas.
The principle of the invention is as follows：
CaO in carbonation reactor with CO in flue gas2Generation carbonation reaction：CaO+CO2→CaCO3, so that CO in flue gas2
It is removed, forms CaCO3；Remove CO2Flue gas is discharged at the top of carbonation reactor afterwards；CaCO from carbonation reactor3Enter
Enter calcination reactor and occur following reaction：CaCO3→CaO+CO2, the reaction is the endothermic reaction, and institute's calorific requirement comes from coal, biology
The carbon-based fuel pure oxygen burning such as matter or natural gas；CaCO3It is CO to decompose with carbon-based fuel pure oxygen burning product2, therefore calcining and decomposing
Reactor outlet is high concentration CO2, can be directly used for sealing up for safekeeping or other purposes；The CaO reactions that calcining and decomposing reactor is formed
In high-temperature calcination and after being recycled for multiple times, slump of disastrous proportions occurs in activity to activity, i.e. its CO that can be captured2Quality Down, for dimension
Its activity is held, part CaO is sent into steam activation reactor, another part CaO is directly recycled to carbonation reactor；CaO exists
With steam generation hydration reaction CaO+H in steam activation reactor2O→Ca(OH)2, there is document to show that CaO is forming Ca (OH)2
During particle volume expand, the CaO pore structures of renewable sintering；The Ca (OH) formed in steam activation reaction2Send
Enter dehydration regeneration reactor, occur dehydration reaction Ca (OH)2→CaO+H2O is decomposed again, is formed with flourishing pore structure
CaO absorbents；Regeneration CaO absorbents are recycled to carbonation reactor and start next circulation.
Compared with prior art, beneficial effects of the present invention are as follows：
（1）Based on calcium-base absorbing agent Cyclic Carbonation-calcining and decomposing process, using CaO absorbent carbonation reactions in flue gas
CO2Separation removal is carried out, followed by CaCO3Calcining and decomposing reaction completes CO2Enrichment, gained high concentration CO2Can directly seal up for safekeeping or
It is used for other purposes;
（2）Active regeneration is carried out to inactivating CaO after calcining using steam activation reactor, is reacted significantly again by hydration-dehydration
Raw absorbent pore structure and reaction surface, can significantly maintain calcium-base absorbing agent activity, suppress absorbent activity decline, reduce and lose
Absorbent discharge living and fresh absorbent magnitude of recruitment；
（3）Steam activation only is carried out to partial inactivation calcium-base absorbing agent, steam activation reactor load is reduced, while reducing steam
Usage amount and energy consumption；
（4）The heat of high-temperature flue gas and recycle stock is made full use of using heat exchanger, high-temperature oxygen, nitrogen and steam is produced, carries
The heat-economy and energy utilization efficiency of high-carbon acquisition procedure.
Brief description of the drawings
Fig. 1 be a kind of carrying vapour activated reactor of the present invention calcium-base absorbing agent carbon dioxide recycle removing means and
Method schematic diagram.
In figure：1. fresh absorbent entrance；2. carbon-based fuel entrance；3. oxygen intake；4. scum pipe；5. fluid bed is forged
Burn decomposition reactor；6. the first cyclone separator；7. recycle stock heat exchanger；8. fluidized bed steam activated reactor；9. fluidisation
Bed dehydration regeneration reactor；10. the first material returning device；11. smoke inlet；12. fluid bed carbonation reactor；13. the second whirlwind
Separator；14. remove CO2Fume emission pipeline afterwards；15. the second material returning device；16. air gas separation unit；17.CO2Heat exchanger；
18.CO2Enriched flue gas；19. air；20. nitrogen；21. high temperature nitrogen；22. oxygen；23. high-temperature oxygen；24. cooling water；25.
Steam；26. steam；27. nitrogen；28. steam；29. steam；30. solid material overfall；31. solid material overfall；32.
Solid circle material inlet；33. solid circle material inlet；34. exhanst gas outlet；35. exhanst gas outlet.
Embodiment
Below in conjunction with the accompanying drawings, the implementation to the present invention is illustrated.
Calcium-base absorbing agent CO of the present invention2Circularly removing device includes fluid bed carbonation reactor 12, fluid bed and forged
Burn decomposition reactor 5, fluidized bed steam activated reactor 8, fluid bed dehydration regeneration reactor 9, the first cyclone separator 6, the
Two cyclone separators 13, the first material returning device 10, the second material returning device 15, recycle stock heat exchanger 7, CO2Heat exchanger 17, air separation
Connecting pipe between unit 16 and each several part；
The bottom of fluid bed carbonation reactor 12 sets smoke inlet 11, and middle and lower part sets solid circle material inlet 33, top
If exhanst gas outlet 34；The bottom of fluidized bed calcination decomposition reactor 5 sets oxygen intake 3 and scum pipe 4, and middle and lower part is set newly respectively
Fresh absorbent entrance 1, carbon-based fuel entrance 2 and solid circle material inlet 32, top sets exhanst gas outlet 35；The fluid bed steams
The middle and upper part of vapour activated reactor 8 sets solid material overfall 30；The middle and upper part of fluid bed dehydration regeneration reactor 9 sets solids
Expect overfall 31；
On the flue gas pipeline connected with the top exhanst gas outlet of fluidized bed calcination decomposition reactor 5, if the first cyclone separator 6；
The bottom of first cyclone separator 6 is connected with recycle stock heat exchanger 7；The outlet of recycle stock heat exchanger 7 is divided into two branch pipes, one
Branch pipe is sequentially connected with fluidized bed steam activated reactor 8, fluid bed dehydration regeneration reactor 9, the first material returning device 10, another
Branch pipe is joined directly together with the first material returning device 10；First material returning device 10 and the circulation located at the middle and lower part of fluid bed carbonation reactor 12
Solid material inlet 33 is connected；The top of first cyclone separator 6 sets CO2Discharge pipe；CO2Discharge pipe and CO2The phase of heat exchanger 17
Even；Air gas separation unit 16 sets the entrance of air 19, the outlet of nitrogen 20 and exported with oxygen 22 respectively；CO2It is cold that heat exchanger 17 sets two-way
But it is respectively nitrogen 20 and oxygen 22 from air gas separation unit 16 in pipeline, pipeline；Recycle stock heat exchanger 7 sets cooling water
Entrance 24 and steam (vapor) outlet 25；
On the flue gas pipeline connected with the top exhanst gas outlet of fluid bed carbonation reactor 12, if the second cyclone separator 13；
The bottom of second cyclone separator 13 is connected to the solid circle material of fluidized bed calcination decomposition reactor 5 by connecting the second material returning device 15
Entrance 32；The top of second rotary separator 13 sets fume emission pipeline 14, exports as removing CO2Flue gas afterwards.
Embodiment 1
The feeding air gas separation unit 16 of air 19 is separated into nitrogen 20 and oxygen 22；Nitrogen 20 is through CO2Heat exchanger is heated to be height
Warm nitrogen 21 sends into fluid bed dehydration regeneration reactor 9 as fluidizing agent, while being dehydration reaction Ca (OH)2→CaO+H2O is supplied
Heat；Oxygen 22 is through CO2Heat exchanger preheating is made for the bottom oxygen intake 3 of the feeding fluidized bed calcination of high-temperature oxygen 23 decomposition reactor 5
For fluidizing agent, while providing oxidant for carbon-based fuel pure oxygen burning；
The temperature of fluidized bed calcination decomposition reactor 5 is 800-1000 DEG C, and fresh calcium-base absorbing agent is respectively fed to instead with carbon-based fuel
Device middle and lower part fresh absorbent entrance 1 and carbon-based fuel entrance 2 are answered, it is calcium that with high-temperature oxygen 23 combustion reaction, which occurs, for carbon-based fuel
Base absorbant decomposition reaction CaCO3→CaO+CO2Heat supply；The high temperature CaO solid materials formed in calcination reactor are through the first whirlwind
Separator 6 is cooled to 400-500 DEG C after separating in recycle stock heat exchanger 7, and subsequent CaO materials are divided into two parts, a part
The middle and lower part solid circle material inlet 33 of fluid bed carbonation reactor 12 is delivered to through the first material returning device 10, another part enters
Fluidized bed steam activated reactor 8 is activated；Waste solid is fixed by the bottom scum pipe 4 of fluidized bed calcination decomposition reactor 5
Phase discharges；
The heat exchange pipeline import of recycle stock heat exchanger 7 is liquid cooled water 24, and superheated steam 25,25 points of steam are formed after heat exchange
For steam 26, steam 28 and steam 29, it is sent to is returned as fluidized bed steam activated reactor 8, the first material returning device 10, second respectively
Glassware 15 is used as fluidizing agent；
Fluidized bed steam activated reactor temperature is 300-400 DEG C, and fluidizing agent is steam 26；From recycle stock heat exchanger 7
Partial CaO in steam activation reactor with steam generation hydration reaction, the solid-state Ca (OH) of generation2Overflow through solid material
In the feeding fluid bed dehydration of head piece 30 regeneration reactor 9；
The temperature of fluid bed dehydration regeneration reactor 9 is 500-650 DEG C, and fluidizing agent is high temperature nitrogen 21, from overfall 30
Solid-state Ca (OH)2Be heated dehydration Ca (OH) in fluid bed dehydration regeneration reactor 92→CaO+H2O, the CaO absorbents warp of formation
The material returning device 10 of solid material overfall 31 and first is recycled to fluid bed carbonation reactor middle and lower part solid circle material inlet
33；
The temperature of fluid bed carbonation reactor 12 is 650-750 DEG C, and the CaO from the first material returning device 10 enters with smoke inlet 11
CO in the flue gas entered2Generation carbonation reaction generates CaCO3, subsequent gas-solid mixture enter the second cyclone separator 13；Through
Solid particle delivers to fluidized bed calcination decomposition reactor 5 through the second material returning device 15 after the separation of two cyclone separators 13, starts next
Circulating repetition is used, and removes CO2Flue gas is discharged by the second separator top flue gas pipeline 14 afterwards；First cyclone separator 6 is exported
For carbon-based fuel pure oxygen burning and CaCO3Decompose the high concentration CO of generation2Enriched flue gas, through CO2Heat exchanger 17 is obtained after cooling
To CO2Enriched flue gas 18 is simultaneously discharged, so as to realize CO in flue gas2Removing and enrichment.
Claims (9)
1. a kind of device of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor, it is characterised in that：
Lost including fluid bed carbonation reactor, fluidized bed calcination decomposition reactor, fluidized bed steam activated reactor, fluid bed
Water reuse (treatment reactor, the first cyclone separator, the second cyclone separator, the first material returning device, the second material returning device, recycle stock heat exchange
Device, CO2Connecting pipe between heat exchanger, air gas separation unit and each several part；
The fluid bed carbonation reactor bottom sets smoke inlet, and middle and lower part sets solid circle material inlet, and top sets flue gas
Outlet；The fluidized bed calcination decomposition reactor bottom sets oxygen intake and scum pipe, and middle and lower part sets fresh absorbent, carbon respectively
Base fuel and solid circle material inlet, top sets exhanst gas outlet；The fluidized bed steam activated reactor middle and upper part sets solid
Material overfall；The fluid bed dehydration regeneration reactor middle and upper part sets solid material overfall；
On the flue gas pipeline connected with fluidized bed calcination decomposition reactor top exhanst gas outlet, if the first cyclone separator；The
One cyclone separator bottom is connected with material heat exchanger；Recycle stock heat exchanger exit is divided into two branch pipes, a branch pipe and stream
Change bed steam activation reactor, fluid bed dehydration regeneration reactor, the first material returning device to be sequentially connected, another branch pipe is returned with first
Glassware is joined directly together；First material returning device is connected with located at fluid bed carbonation reactor middle and lower part solid circle material inlet；The
CO is set at the top of one cyclone separator2Discharge pipe；CO2Discharge pipe and CO2Heat exchanger is connected；CO2Heat exchanger sets two-way cooling tube
It is respectively cryogenic oxygen and low temperature nitrogen from air gas separation unit in road, pipeline；Air gas separation unit sets air and entered respectively
Mouth, nitrogen outlet and oxygen outlet；Recycle stock heat exchanger sets cooling water inlet and steam (vapor) outlet；
On the flue gas pipeline connected with fluid bed carbonation reactor top exhanst gas outlet, if the second cyclone separator；Second
Cyclone separator bottom is connected to fluidized bed calcination decomposition reactor solid circle material inlet by the second material returning device；Second rotation point
Fume emission pipeline is set from device top.
2. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor of 1 described device is required according to profit
Method, it is characterised in that including：
（1）Air feeding air gas separation unit is separated into oxygen and nitrogen, and oxygen is through CO2Heat exchanger is preheated to after 500-900 DEG C
Fluidized bed calcination decomposition reactor bottom is sent into as fluidizing agent, while providing oxidant for carbon-based fuel burning；Nitrogen is passed through
CO2Feeding fluid bed dehydration regeneration reactor is as fluidizing agent after heat exchanger heating, while reacting heat supply for dehydration；
（2）Fluidized bed calcination decomposition reactor sets temperature to be 800-1000 DEG C, and calcium-base absorbing agent and the carbon-based fuel of supplement are sent
Enter reactor middle and lower part material inlet, carbon-based fuel and step（1）In preheated oxygen occur combustion reaction be calcium-base absorbing agent
Decompose heat supply；The high temperature CaO solid materials formed in calcination reactor are changed after being separated through the first cyclone separator in recycle stock
400-500 DEG C is cooled in hot device, subsequent CaO materials are divided into two parts, a part is delivered to fluid bed carbon through the first material returning device
Acidification reactor middle and lower part solid circle material inlet, another part is activated into fluidized bed steam activated reactor；It is useless
Solid is abandoned periodically to discharge by calcination reactor bottom scum pipe；
（3）Fluidized bed steam activated reactor sets temperature to be 300-400 DEG C, and fluidizing agent is steam；The one of step (2) generation
Part CaO in steam activation reactor with steam generation hydration reaction, the solid-state Ca (OH) of generation2Through solid material overfall
Send into fluid bed dehydration regeneration reactor；
（4）Fluid bed dehydration regeneration reactor sets temperature to be 500-650 DEG C, and fluidizing agent is the 500-650 that step (1) is produced
DEG C nitrogen, the solid-state Ca (OH) that step (3) is produced2The heated dehydration in fluid bed dehydration regeneration reactor, the CaO of formation absorbs
Agent is recycled to fluid bed carbonation reactor middle and lower part solid circle material inlet through solid material overfall and the first material returning device；
（5）Fluid bed carbonation reactor sets temperature to be 650-750 DEG C, CaO and flue gas that step (2) and step (4) are produced
Middle CO2Generation carbonation reaction generates CaCO3, subsequent gas-solid mixture enter the second cyclone separator；Through the second cyclone separator
Solid particle delivers to fluidized bed calcination reactor through the second material returning device after separation, starts subsequent cycle and reuses, removes CO2Afterwards
Flue gas is discharged by the second separator top flue gas pipeline；First Cyclone outlet is carbon-based fuel pure oxygen burning and CaCO3
Decompose the high concentration CO of generation2, so as to realize CO in flue gas2Removing and enrichment.
3. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：Step（1）The CO2It is respectively to come from air gas separation unit that heat exchanger, which is set in two-way cooling pipe, pipeline,
Nitrogen and oxygen.
4. a kind of side of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：Step（2）The recycle stock cooler uses water as cooling medium.
5. a kind of side of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：Step（2）The first material returning device fluidizing agent is steam, and steam is cooling in recycle stock cooler
WATER AS FLOW MEDIUM gasifies after being exchanged heat with high-temperature material and formed.
6. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：Step（3）The fluidizing agent steam of the fluidized bed steam activated reactor is in recycle stock cooler
Water cooling medium gasifies after being exchanged heat with high-temperature material and formed.
7. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：Step（4）The second material returning device fluidizing agent is steam, and steam is cooling in recycle stock cooler
WATER AS FLOW MEDIUM gasifies after being exchanged heat with high-temperature material and formed.
8. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：The fresh absorbent is the artificial conjunction that lime stone, dolomite or other CaO mass percents are higher than 20%
Into calcium-base absorbing agent.
9. a kind of calcium-base absorbing agent carbon dioxide recycle removing side of carrying vapour activated reactor according to claim 2
Method, it is characterised in that：The carbon-based fuel is one kind in coal, biomass, natural gas, coal gas, synthesis gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710293779.4A CN106975341A (en) | 2017-04-28 | 2017-04-28 | A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710293779.4A CN106975341A (en) | 2017-04-28 | 2017-04-28 | A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106975341A true CN106975341A (en) | 2017-07-25 |
Family
ID=59342383
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710293779.4A Pending CN106975341A (en) | 2017-04-28 | 2017-04-28 | A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN106975341A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107398173A (en) * | 2017-08-27 | 2017-11-28 | 北方民族大学 | A kind of lime stone carries out CO in double tower fluid bed2Circularly trapping device and its technique |
| CN107983112A (en) * | 2017-11-29 | 2018-05-04 | 安徽建筑大学 | A kind of band regenerated swinging fixed bed carbon dioxide recycle catching method of filler activator |
| CN108006684A (en) * | 2017-11-29 | 2018-05-08 | 安徽建筑大学 | A kind of carbon dioxide high temperature circulation removal methods based on swinging fixed bed |
| 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 |
| CN111234850A (en) * | 2020-01-17 | 2020-06-05 | 江苏大学 | Calcium-based biomass chemical chain pyrolysis system |
| CN115178075A (en) * | 2022-07-20 | 2022-10-14 | 合肥中亚环保科技有限公司 | Process system for removing carbon dioxide in flue gas of small kiln |
| CN115430363A (en) * | 2022-10-12 | 2022-12-06 | 安徽科达洁能股份有限公司 | Carbon dioxide trapping method and carbonating furnace |
| CN116336464A (en) * | 2023-04-07 | 2023-06-27 | 南京工程学院 | Calcium-based hazardous waste synergistic trapping SO 2 /NO X /CO 2 Technological method and system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101298023A (en) * | 2008-06-17 | 2008-11-05 | 东南大学 | Device for removing CO2 of flue gas by highly active potassium-base absorbing agent dry method and method thereof |
| CN101987277A (en) * | 2008-10-08 | 2011-03-23 | 阿尔斯通技术有限公司 | Method and assembly for separating co2 from combustion waste gas |
| CN102307646A (en) * | 2008-11-19 | 2012-01-04 | 俄亥俄州立大学研究基金会 | Carbonation calcination reaction process for CO2 capture using a highly regenerable sorbent |
| CN104174280A (en) * | 2014-08-19 | 2014-12-03 | 东南大学 | Method and device with hydration reactor for circularly capturing CO2 by calcium-based sorbent |
| CN105521702A (en) * | 2014-10-27 | 2016-04-27 | 财团法人工业技术研究院 | Carbon dioxide capture device and method |
-
2017
- 2017-04-28 CN CN201710293779.4A patent/CN106975341A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101298023A (en) * | 2008-06-17 | 2008-11-05 | 东南大学 | Device for removing CO2 of flue gas by highly active potassium-base absorbing agent dry method and method thereof |
| CN101987277A (en) * | 2008-10-08 | 2011-03-23 | 阿尔斯通技术有限公司 | Method and assembly for separating co2 from combustion waste gas |
| CN102307646A (en) * | 2008-11-19 | 2012-01-04 | 俄亥俄州立大学研究基金会 | Carbonation calcination reaction process for CO2 capture using a highly regenerable sorbent |
| CN104174280A (en) * | 2014-08-19 | 2014-12-03 | 东南大学 | Method and device with hydration reactor for circularly capturing CO2 by calcium-based sorbent |
| CN105521702A (en) * | 2014-10-27 | 2016-04-27 | 财团法人工业技术研究院 | Carbon dioxide capture device and method |
Non-Patent Citations (1)
| Title |
|---|
| 钱枫 等: "生石灰孔结构对高温脱硫性能的影响", 《环境污染治理技术与设备》 * |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107398173A (en) * | 2017-08-27 | 2017-11-28 | 北方民族大学 | A kind of lime stone carries out CO in double tower fluid bed2Circularly trapping device and its technique |
| CN107398173B (en) * | 2017-08-27 | 2023-10-27 | 北方民族大学 | Limestone CO in a double tower fluidized bed 2 Circulation trapping device and technology thereof |
| CN107983112B (en) * | 2017-11-29 | 2021-06-18 | 安徽建筑大学 | Rotary fixed bed carbon dioxide cyclic capture method with filler activation regeneration |
| CN107983112A (en) * | 2017-11-29 | 2018-05-04 | 安徽建筑大学 | A kind of band regenerated swinging fixed bed carbon dioxide recycle catching method of filler activator |
| CN108006684A (en) * | 2017-11-29 | 2018-05-08 | 安徽建筑大学 | A kind of carbon dioxide high temperature circulation removal methods based on swinging fixed bed |
| CN108006684B (en) * | 2017-11-29 | 2019-05-28 | 安徽建筑大学 | A kind of carbon dioxide high temperature circulation removal methods based on rotary fixed bed |
| 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 |
| CN111234850A (en) * | 2020-01-17 | 2020-06-05 | 江苏大学 | Calcium-based biomass chemical chain pyrolysis system |
| CN115178075A (en) * | 2022-07-20 | 2022-10-14 | 合肥中亚环保科技有限公司 | Process system for removing carbon dioxide in flue gas of small kiln |
| CN115430363A (en) * | 2022-10-12 | 2022-12-06 | 安徽科达洁能股份有限公司 | Carbon dioxide trapping method and carbonating furnace |
| CN115430363B (en) * | 2022-10-12 | 2023-11-24 | 安徽科达洁能股份有限公司 | Carbon dioxide capturing method and carbonator |
| CN116336464A (en) * | 2023-04-07 | 2023-06-27 | 南京工程学院 | Calcium-based hazardous waste synergistic trapping SO 2 /NO X /CO 2 Technological method and system |
| CN116336464B (en) * | 2023-04-07 | 2024-01-19 | 南京工程学院 | Calcium-based hazardous waste synergistic trapping SO 2 /NO X /CO 2 Technological method and system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106975341A (en) | A kind of devices and methods therefor of the calcium-base absorbing agent circularly removing carbon dioxide of carrying vapour activated reactor | |
| CA2743911C (en) | Carbonation calcination reaction process for co2 capture using a highly regenerable sorbent | |
| Bosoaga et al. | CO2 capture technologies for cement industry | |
| CN1642620B (en) | Combustion method with integrated co2 separation by means of carbonation | |
| CN101570315B (en) | Method and device for producing hydrogen through biomass gasification by using single fluidized bed and two-step method | |
| US20130213280A9 (en) | Methods and systems for reducing carbon dioxide emissions | |
| CN103742899A (en) | Oxygen-enriched combustion circulating fluidized bed poly-generation system and process | |
| CN102773006A (en) | Device and process for cyclic capture of carbon dioxide by taking CaO as carrier | |
| CN113606946B (en) | Carbon dioxide capturing system and emission reduction method for cement kiln tail flue gas | |
| CN102796561A (en) | Anaerobic gasification method and device for biomass fuels by carbon dioxide circulation | |
| CN107057772B (en) | A kind of calcium carrier loop H2-CO-C2H2Poly-generation cooperates with CO2Capture method | |
| CN107694340A (en) | A kind of calcium-base absorbing agent active regeneration and circularly removing CO2Method | |
| KR20230118839A (en) | Cement clinker manufacturing system and cement clinker manufacturing method | |
| CN210092233U (en) | Molten carbonate fuel cell and calcium circulation integrated system | |
| CN101333463B (en) | Oxygen supplying and hydrogen making process from iron base oxygen carrier of three-linked transport bed | |
| JP2022149127A (en) | Manufacturing system of cement clinker and manufacturing method of cement clinker | |
| CN103664016B (en) | Method of producing cement through active coal gasification and rotary kiln device | |
| JP2022148174A (en) | Manufacturing system of cement clinker and manufacturing method of cement clinker | |
| CN220083708U (en) | Cement kiln waste heat power generation system for removing CO2 by utilizing solid absorbent | |
| CN217264848U (en) | Device for preparing hydrogen by utilizing low-carbon coal | |
| CN220061734U (en) | Carbon dioxide trapping device under pure oxygen combustion | |
| CN203703950U (en) | Oxygen-rich combustion circulating fluidized bed poly-generation system | |
| CN114163151B (en) | By using CO 2 Carbon emission reduction method and system for storing solar energy to calcine cement clinker | |
| CN107983112A (en) | A kind of band regenerated swinging fixed bed carbon dioxide recycle catching method of filler activator | |
| CN116583705A (en) | Cement clinker manufacturing system and cement clinker manufacturing method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB02 | Change of applicant information |
Address after: 230601 Anhui construction university, South 292, Ziyun Road, Hefei economic and Technological Development Zone, Anhui Applicant after: Anhui University of Architecture Address before: 230601 Anhui Road, Ziyun Road, Hefei, Anhui 292, China Applicant before: Anhui University of Architecture |
|
| CB02 | Change of applicant information | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20170725 |
|
| RJ01 | Rejection of invention patent application after publication |