CN105561736A - Method for removing CO2 from gas - Google Patents
Method for removing CO2 from gas Download PDFInfo
- Publication number
- CN105561736A CN105561736A CN201610131184.4A CN201610131184A CN105561736A CN 105561736 A CN105561736 A CN 105561736A CN 201610131184 A CN201610131184 A CN 201610131184A CN 105561736 A CN105561736 A CN 105561736A
- Authority
- CN
- China
- Prior art keywords
- absorbent
- ammonium salt
- aqueous solution
- desorb
- salt aqueous
- 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
- 238000000034 method Methods 0.000 title claims abstract description 26
- 230000002745 absorbent Effects 0.000 claims abstract description 77
- 239000002250 absorbent Substances 0.000 claims abstract description 77
- 150000003863 ammonium salts Chemical class 0.000 claims abstract description 71
- 239000007864 aqueous solution Substances 0.000 claims abstract description 58
- 238000010521 absorption reaction Methods 0.000 claims abstract description 46
- VILCJCGEZXAXTO-UHFFFAOYSA-N 2,2,2-tetramine Chemical compound NCCNCCNCCN VILCJCGEZXAXTO-UHFFFAOYSA-N 0.000 claims abstract description 8
- 229960001124 trientine Drugs 0.000 claims abstract description 8
- 238000003795 desorption Methods 0.000 claims description 18
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000010438 heat treatment Methods 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 abstract description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract 1
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- FAGUFWYHJQFNRV-UHFFFAOYSA-N tetraethylenepentamine Chemical compound NCCNCCNCCNCCN FAGUFWYHJQFNRV-UHFFFAOYSA-N 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 33
- 238000005261 decarburization Methods 0.000 description 28
- 239000008246 gaseous mixture Substances 0.000 description 14
- 239000003795 chemical substances by application Substances 0.000 description 11
- 150000001412 amines Chemical class 0.000 description 5
- 239000011800 void material Substances 0.000 description 5
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 3
- 229940043237 diethanolamine Drugs 0.000 description 3
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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
- B01D53/14—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 by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- 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
- B01D53/14—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 by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a method for removing CO2 from a gas. The method is characterized in that one of triethylene tetramine or tetraethylenepentamine reacts with H3BO3 with same mole to generate an aqueous solution of ammonium salt to serve as an absorbent; the absorbent is in contact with a CO2-containing gas to absorb and remove the CO2, wherein the mass percentage of the absorbent, namely the aqueous solution of the ammonium salt, is 10 to 20 percent; the volume percentage concentration of the CO2 in the absorbed gas is 0.1 to 85 percent; the absorption temperature is 0 to 50 DEG C; after the CO2 is absorbed, the absorbent, namely the aqueous solution of the ammonium salt, can be reused after being heated to desorb the CO2 at normal pressure; the temperature for desorbing the CO2 is 70 to 103 DEG C, and the time is 20 to 120 minutes. Compared with the prior art, firstly, the carbon removal speed of the absorbent is high, the CO2 load is large, and the recycling performance is high; secondly, the CO2 is easy to desorb after being absorbed; thirdly, the absorbent is easily dissolved in water and does not have saturation vapour pressure, and the problem of scaling to block equipment is avoided.
Description
Technical field
The present invention relates to
one removes CO in gas 2 method, be specifically related to remove flue gas, containing CO
2waste gas or raw material of industry gas in CO
2.
Background technology
Along with developing rapidly of industry, flue gas, containing CO
2discharge amount of exhaust gas grow with each passing day, it is just day by day serious that too much carbon dioxide has caused the harm that " greenhouse effects " cause.Thus, reduce the discharge capacity of carbon dioxide, become one of environmental problem needing solution badly.
At present, decarburization technique mainly contains MEA method, diethanolamine method, N methyldiethanol amine method etc.Monoethanol method exists that absorbent easily foams, rotten, the problem such as regeneration temperature is higher of degrading; There is the defects such as the absorbability of diethanol amine is poor, clean-up effect is general, price is high in diethanolamine method; Advantages such as although N methyldiethanol amine method absorbent are easy to regeneration, Heat stability is good, not easily degrade, volatility is less, absorbing and removing efficiency is lower.Thus, the application adopts a kind of triethylene tetramine that can be recycled or TEPA and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is that absorbent is for absorbing and removing flue gas, containing CO
2waste gas and/or raw material of industry gas in CO
2.
Summary of the invention
The object of the invention is to replace traditional decarburization absorption agent, provide a kind of decarburization absorption agent that can be recycled of function admirable to remove flue gas, containing CO
2waste gas and/or raw material of industry gas in CO
2, and reclaim CO
2.
The present invention relates to
one removes CO in gas 2 method, it is characterized in that adopting the one in triethylene tetramine or TEPA and H
3bO
3the aqueous solution of the ammonium salt that equimolar ratio reaction generates is absorbent, will containing CO
2gas pass into the absorption tower that absorbent ammonium salt aqueous solution is housed and carry out absorbing and removing CO
2, the mass fraction of absorbent ammonium salt aqueous solution is 10-20%, is absorbed CO in gas
2volumetric concentration be 0.1-85%, absorb temperature 0-50 DEG C, absorb CO
2rear absorbent ammonium salt aqueous solution is in normal heating desorb CO
2reusable, wherein, absorbent ammonium salt aqueous solution desorb CO
2temperature 70-103 DEG C, time 20-120min.
Reaction condition of the present invention with the mass fraction 14-18% of absorbent ammonium salt aqueous solution, absorb temperature 30-40 DEG C, desorption temperature 90-102 DEG C, desorption time 40-60min be good.
The present invention solves this technical problem by the following technical programs:
1. the one in triethylene tetramine or TEPA and H
3bO
3the aqueous solution of the ammonium salt that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 10-20% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, by CO in absorption gas
2volumetric concentration be 0.1-85%, absorb temperature 0-50 DEG C, CO
2tail gas CO-2 analyser after decarburization absorption tower measures CO
2gas concentration, then measure absorb CO
2after in absorbent ammonium salt aqueous solution CO
3 2-and HCO
3 -content.Absorb CO
2rear absorbent ammonium salt aqueous solution is in normal heating desorb CO
2, desorption temperature 70-103 DEG C, time 20-120min, measure desorb CO afterwards
2after in absorbent ammonium salt aqueous solution CO
3 2-and HCO
3 -content, desorb CO
2after absorbent ammonium salt aqueous solution reusable.
2. the absorbent decarburization capacity that uses of method of the present invention is strong, reusable, and separating obtained absorbent only needs heating desorption namely to can be used for absorbing decarburization, the CO of desorb next time
2recyclable, absorbent reuses 40 times, and its decarburization capacity has no decline.
The present invention has following features:
1. fast, the CO of absorbent decarbonization rate
2load is large, repeat performance is good.
2. absorbent absorbs CO
2saturated rear easy desorb, desorption temperature is low, CO after desorb
2with absorbent natural separation.
3. ammonium salt absorption agent is water-soluble and without vapour pressure, absorbs CO
2rear products therefrom is still ammonium salt, and it is water-soluble also without saturated vapor pressure, therefore there is not the problem such as absorbent loss, fouling and clogging equipment in absorption and regenerative process.
Specific implementation method
Being described further method of the present invention below in conjunction with embodiment, is not limitation of the invention.
Embodiment 1: with triethylene tetramine and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 15% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, continue to pass into the CO that concentration of volume percent is 14% at 30 DEG C at the bottom of tower
2with 86% N
2gaseous mixture, CO
2tail gas CO-2 analyser after the decarburization absorption of absorption tower measures CO
2gas concentration, when record absorb after CO in tail gas
2stop passing into of gaseous mixture when void fraction is 1000ppm, then measure and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 1.87 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.61 molecule
2, the carbon-drop rate 99.77% of whole process, desorption efficiency 85.98%.
Comparative example 1: using 15% aqueous monoethanolamine as decarburization absorption agent, dropped into by absorbent in absorption tower, continues to pass into the CO that concentration of volume percent is 14% at 30 DEG C at the bottom of tower
2with 86% N
2gaseous mixture, as absorbent saturated absorption CO
2, the tail gas CO-2 analyser namely after the decarburization absorption of absorption tower measures CO
2gas concentration and the CO that passes into
2when gas concentration is equal, stop passing into of gaseous mixture, then measure and absorb CO
2cO in rear absorbent aqueous monoethanolamine
3 2-and HCO
3 -content, calculate the CO that 1 molecule MEA can absorb 0.52 molecule
2, absorbent aqueous monoethanolamine saturated after absorbing is in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent aqueous monoethanolamine
3 2-and HCO
3 -content, calculating 1 molecule MEA can the CO of desorb 0.33 molecule
2, the carbon-drop rate 55.37% of whole process, desorption efficiency 64.38%.
Comparative example 2: using the solution of 10% MEA+5% methyl diethanolamine as decarburization absorption agent, dropped into by absorbent in absorption tower, continue to pass into the CO that concentration of volume percent is 14% at 30 DEG C at the bottom of tower
2with 86% N
2gaseous mixture, as absorbent saturated absorption CO
2, the tail gas CO-2 analyser namely after the decarburization absorption of absorption tower measures CO
2gas concentration and the CO that passes into
2when gas concentration is equal, stop passing into of gaseous mixture, then measure and absorb CO
2cO in the rear absorbent mixed amine aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecular mixing amine can absorb 0.51 molecule
2, the absorbent mixed amine aqueous solution after absorption is in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in the rear absorbent mixed amine aqueous solution
3 2-and HCO
3 -content, calculating 1 molecular mixing amine can the CO of desorb 0.30 molecule
2, the carbon-drop rate 58.56% of whole process, desorption efficiency 66.38%.
Embodiment 2: with TEPA and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 15% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, continue to pass into the CO that concentration of volume percent is 14% at 30 DEG C at the bottom of tower
2with 86% N
2gaseous mixture, CO
2tail gas CO-2 analyser after the decarburization absorption of absorption tower measures CO
2gas concentration, when record absorb after CO in tail gas
2stop passing into of gaseous mixture when void fraction is 1000ppm, then measure and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 2.17 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.85 molecule
2, the carbon-drop rate 99.82% of whole process, desorption efficiency 85.17%.
Embodiment 3: be absorbent by the aqueous solution of ammonium salt in embodiment 1, carries out cyclic absorption and desorb CO according to the absorption and desorption condition of embodiment 1
240 times, measure the 40th time and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 1.75 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.59 molecule
2, the carbon-drop rate 99.65% of whole process, desorption efficiency 90.87%.
Embodiment 4: be absorbent by the aqueous solution of ammonium salt in embodiment 2, according to absorption and desorption condition cyclic absorption and the desorb CO of embodiment 2
240 times, measure the 40th time and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 2.04 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.86 molecule
2, the carbon-drop rate 99.71% of whole process, desorption efficiency 91.33%.
Embodiment 5: with triethylene tetramine and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 10% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, continue to pass into the CO that concentration of volume percent is 0.1% at 30 DEG C at the bottom of tower
2with 99.9% N
2gaseous mixture, CO
2tail gas CO-2 analyser after the decarburization absorption of absorption tower measures CO
2gas concentration, when record absorb after CO in tail gas
2stop passing into of gaseous mixture when void fraction is 1000ppm, then measure and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 1.72 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 70 DEG C of desorb CO
2120min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.01 molecule
2, the carbon-drop rate 99.57% of whole process, desorption efficiency 70.68%.
Embodiment 6: with TEPA and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 20% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, continue to pass into the CO that concentration of volume percent is 85% at 0 DEG C at the bottom of tower
2with 15% N
2gaseous mixture, CO
2tail gas CO-2 analyser after the decarburization absorption of absorption tower measures CO
2gas concentration, when record absorb after CO in tail gas
2stop passing into of gaseous mixture when void fraction is 1000ppm, then measure and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 2.26 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 102 DEG C of desorb CO
260min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 1.92 molecule
2, the carbon-drop rate 99.75% of whole process, desorption efficiency 85.03%.
Embodiment 7: with triethylene tetramine and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is decarburization absorption agent, and the mass fraction 15% of absorbent ammonium salt aqueous solution, drops in decarburization absorption tower by absorbent, continue to pass into the CO that concentration of volume percent is 14% at 50 DEG C at the bottom of tower
2with 86% N
2gaseous mixture, CO
2tail gas CO-2 analyser after the decarburization absorption of absorption tower measures CO
2gas concentration, when record absorb after CO in tail gas
2stop passing into of gaseous mixture when void fraction is 1000ppm, then measure and absorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculate the CO that 1 molecule ammonium salt can absorb 1.44 molecules
2, absorb CO
2after absorbent ammonium salt aqueous solution in normal pressure 103 DEG C of desorb CO
220min, and measure desorb CO
2cO in rear absorbent ammonium salt aqueous solution
3 2-and HCO
3 -content, calculating 1 molecule ammonium salt can the CO of desorb 0.94 molecule
2, the carbon-drop rate 99.37% of whole process, desorption efficiency 75.22%.
Claims (2)
1. one kind removes CO in gas
2method, it is characterized in that adopting the one in triethylene tetramine or TEPA and H
3bO
3the ammonium salt aqueous solution that equimolar ratio reaction generates is absorbent, will containing CO
2gas pass into the absorption tower that absorbent ammonium salt aqueous solution is housed and carry out absorbing and removing CO
2, the mass fraction of wherein said absorbent ammonium salt aqueous solution is 10-20%, is absorbed CO in gas
2concentration of volume percent be 0.1-85%, absorb temperature 0-50 DEG C, absorb CO
2after absorbent ammonium salt aqueous solution in normal heating desorb CO
2reusable, wherein, absorbent ammonium salt aqueous solution desorb CO
2temperature 70-103 DEG C, time 20-120min.
2. the method for claim 1, it is characterized in that reaction condition with the mass fraction 14-18% of absorbent ammonium salt aqueous solution, absorb temperature 30-40 DEG C, desorption temperature 90-102 DEG C, desorption time 40-60min be good.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610131184.4A CN105561736A (en) | 2016-03-08 | 2016-03-08 | Method for removing CO2 from gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610131184.4A CN105561736A (en) | 2016-03-08 | 2016-03-08 | Method for removing CO2 from gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105561736A true CN105561736A (en) | 2016-05-11 |
Family
ID=55872698
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610131184.4A Pending CN105561736A (en) | 2016-03-08 | 2016-03-08 | Method for removing CO2 from gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105561736A (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993378A (en) * | 2010-09-10 | 2011-03-30 | 中国石油大学(北京) | Amido-containing ionic liquid used for absorbing acidic gases and preparation method and application thereof |
| CN103170216A (en) * | 2013-03-13 | 2013-06-26 | 上海锅炉厂有限公司 | Alcohol amine type ion liquor-containing compound absorbent capable of capturing carbon dioxide |
| CN103596662A (en) * | 2011-06-09 | 2014-02-19 | 旭化成株式会社 | Carbon-dioxide absorber and carbon-dioxide separation/recovery method using said absorber |
-
2016
- 2016-03-08 CN CN201610131184.4A patent/CN105561736A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101993378A (en) * | 2010-09-10 | 2011-03-30 | 中国石油大学(北京) | Amido-containing ionic liquid used for absorbing acidic gases and preparation method and application thereof |
| CN103596662A (en) * | 2011-06-09 | 2014-02-19 | 旭化成株式会社 | Carbon-dioxide absorber and carbon-dioxide separation/recovery method using said absorber |
| CN103170216A (en) * | 2013-03-13 | 2013-06-26 | 上海锅炉厂有限公司 | Alcohol amine type ion liquor-containing compound absorbent capable of capturing carbon dioxide |
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Application publication date: 20160511 |
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