WO2023066400A1 - 二氧化碳吸收液以及从燃料气中捕集二氧化碳的方法 - Google Patents
二氧化碳吸收液以及从燃料气中捕集二氧化碳的方法 Download PDFInfo
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- WO2023066400A1 WO2023066400A1 PCT/CN2022/127150 CN2022127150W WO2023066400A1 WO 2023066400 A1 WO2023066400 A1 WO 2023066400A1 CN 2022127150 W CN2022127150 W CN 2022127150W WO 2023066400 A1 WO2023066400 A1 WO 2023066400A1
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- carbon dioxide
- activator
- weight
- fuel gas
- parts
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 194
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 97
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 96
- 239000007788 liquid Substances 0.000 title claims abstract description 90
- 239000002737 fuel gas Substances 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000010521 absorption reaction Methods 0.000 title claims abstract description 25
- 230000008929 regeneration Effects 0.000 claims abstract description 74
- 238000011069 regeneration method Methods 0.000 claims abstract description 74
- 239000012190 activator Substances 0.000 claims abstract description 55
- 239000007789 gas Substances 0.000 claims abstract description 47
- 150000001413 amino acids Chemical class 0.000 claims abstract description 26
- 150000001412 amines Chemical class 0.000 claims abstract description 22
- 239000002904 solvent Substances 0.000 claims abstract description 12
- 239000002608 ionic liquid Substances 0.000 claims description 38
- 239000012528 membrane Substances 0.000 claims description 34
- 235000001014 amino acid Nutrition 0.000 claims description 26
- DHMQDGOQFOQNFH-UHFFFAOYSA-N Glycine Chemical compound NCC(O)=O DHMQDGOQFOQNFH-UHFFFAOYSA-N 0.000 claims description 19
- -1 methylguanidine dodecane dicarboxylate Chemical compound 0.000 claims description 17
- 230000002378 acidificating effect Effects 0.000 claims description 14
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 claims description 10
- 239000012510 hollow fiber Substances 0.000 claims description 9
- RAXXELZNTBOGNW-UHFFFAOYSA-N imidazole Natural products C1=CNC=N1 RAXXELZNTBOGNW-UHFFFAOYSA-N 0.000 claims description 9
- 125000005496 phosphonium group Chemical group 0.000 claims description 8
- FSYKKLYZXJSNPZ-UHFFFAOYSA-N sarcosine Chemical compound C[NH2+]CC([O-])=O FSYKKLYZXJSNPZ-UHFFFAOYSA-N 0.000 claims description 8
- 125000000217 alkyl group Chemical group 0.000 claims description 7
- DHMQDGOQFOQNFH-UHFFFAOYSA-M Aminoacetate Chemical compound NCC([O-])=O DHMQDGOQFOQNFH-UHFFFAOYSA-M 0.000 claims description 6
- 239000004471 Glycine Substances 0.000 claims description 6
- YNAVUWVOSKDBBP-UHFFFAOYSA-N Morpholine Chemical compound C1COCCN1 YNAVUWVOSKDBBP-UHFFFAOYSA-N 0.000 claims description 6
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical group [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 6
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 claims description 5
- QNAYBMKLOCPYGJ-REOHCLBHSA-N L-alanine Chemical compound C[C@H](N)C(O)=O QNAYBMKLOCPYGJ-REOHCLBHSA-N 0.000 claims description 5
- OPKOKAMJFNKNAS-UHFFFAOYSA-N N-methylethanolamine Chemical group CNCCO OPKOKAMJFNKNAS-UHFFFAOYSA-N 0.000 claims description 5
- 235000004279 alanine Nutrition 0.000 claims description 5
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 claims description 5
- XFGLCISNNKNIKV-UHFFFAOYSA-N butanedioic acid;1,1,3,3-tetramethylguanidine Chemical compound CN(C)C(=N)N(C)C.OC(=O)CCC(O)=O XFGLCISNNKNIKV-UHFFFAOYSA-N 0.000 claims description 5
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 claims description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- KDXKERNSBIXSRK-YFKPBYRVSA-N L-lysine Chemical compound NCCCC[C@H](N)C(O)=O KDXKERNSBIXSRK-YFKPBYRVSA-N 0.000 claims description 4
- KDXKERNSBIXSRK-UHFFFAOYSA-N Lysine Natural products NCCCCC(N)C(O)=O KDXKERNSBIXSRK-UHFFFAOYSA-N 0.000 claims description 4
- 239000004472 Lysine Substances 0.000 claims description 4
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 4
- 108010077895 Sarcosine Proteins 0.000 claims description 4
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 claims description 4
- 235000018977 lysine Nutrition 0.000 claims description 4
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 4
- 229940043230 sarcosine Drugs 0.000 claims description 4
- KYVBNYUBXIEUFW-UHFFFAOYSA-N 1,1,3,3-tetramethylguanidine Chemical compound CN(C)C(=N)N(C)C KYVBNYUBXIEUFW-UHFFFAOYSA-N 0.000 claims description 3
- RILLZYSZSDGYGV-UHFFFAOYSA-N 2-(propan-2-ylamino)ethanol Chemical compound CC(C)NCCO RILLZYSZSDGYGV-UHFFFAOYSA-N 0.000 claims description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 3
- WFCSWCVEJLETKA-UHFFFAOYSA-N 2-piperazin-1-ylethanol Chemical compound OCCN1CCNCC1 WFCSWCVEJLETKA-UHFFFAOYSA-N 0.000 claims description 3
- 239000002202 Polyethylene glycol Substances 0.000 claims description 3
- 150000004985 diamines Chemical class 0.000 claims description 3
- LVTYICIALWPMFW-UHFFFAOYSA-N diisopropanolamine Chemical compound CC(O)CNCC(C)O LVTYICIALWPMFW-UHFFFAOYSA-N 0.000 claims description 3
- 229940043276 diisopropanolamine Drugs 0.000 claims description 3
- 229920001223 polyethylene glycol Polymers 0.000 claims description 3
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims description 3
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 239000011780 sodium chloride Substances 0.000 claims description 3
- MTCFGRXMJLQNBG-REOHCLBHSA-N (2S)-2-Amino-3-hydroxypropansäure Chemical compound OC[C@H](N)C(O)=O MTCFGRXMJLQNBG-REOHCLBHSA-N 0.000 claims description 2
- WLSTULAJVVMDFD-UHFFFAOYSA-N 1-(3-methylimidazol-3-ium-1-yl)propan-1-amine Chemical compound CCC(N)N1C=C[N+](C)=C1 WLSTULAJVVMDFD-UHFFFAOYSA-N 0.000 claims description 2
- YIUHWLIUHXPXEI-UHFFFAOYSA-M 2-aminoacetate tetrabutylazanium Chemical compound NCC([O-])=O.CCCC[N+](CCCC)(CCCC)CCCC YIUHWLIUHXPXEI-UHFFFAOYSA-M 0.000 claims description 2
- XRHHUBLPEBPWQY-UHFFFAOYSA-M 2-aminoacetate tetraethylazanium Chemical compound NCC([O-])=O.CC[N+](CC)(CC)CC XRHHUBLPEBPWQY-UHFFFAOYSA-M 0.000 claims description 2
- 239000004475 Arginine Substances 0.000 claims description 2
- WHUUTDBJXJRKMK-UHFFFAOYSA-N Glutamic acid Natural products OC(=O)C(N)CCC(O)=O WHUUTDBJXJRKMK-UHFFFAOYSA-N 0.000 claims description 2
- ONIBWKKTOPOVIA-BYPYZUCNSA-N L-Proline Chemical compound OC(=O)[C@@H]1CCCN1 ONIBWKKTOPOVIA-BYPYZUCNSA-N 0.000 claims description 2
- ODKSFYDXXFIFQN-BYPYZUCNSA-P L-argininium(2+) Chemical compound NC(=[NH2+])NCCC[C@H]([NH3+])C(O)=O ODKSFYDXXFIFQN-BYPYZUCNSA-P 0.000 claims description 2
- WHUUTDBJXJRKMK-VKHMYHEASA-N L-glutamic acid Chemical compound OC(=O)[C@@H](N)CCC(O)=O WHUUTDBJXJRKMK-VKHMYHEASA-N 0.000 claims description 2
- HNDVDQJCIGZPNO-YFKPBYRVSA-N L-histidine Chemical compound OC(=O)[C@@H](N)CC1=CN=CN1 HNDVDQJCIGZPNO-YFKPBYRVSA-N 0.000 claims description 2
- ONIBWKKTOPOVIA-UHFFFAOYSA-N Proline Natural products OC(=O)C1CCCN1 ONIBWKKTOPOVIA-UHFFFAOYSA-N 0.000 claims description 2
- MTCFGRXMJLQNBG-UHFFFAOYSA-N Serine Natural products OCC(N)C(O)=O MTCFGRXMJLQNBG-UHFFFAOYSA-N 0.000 claims description 2
- ODKSFYDXXFIFQN-UHFFFAOYSA-N arginine Natural products OC(=O)C(N)CCCNC(N)=N ODKSFYDXXFIFQN-UHFFFAOYSA-N 0.000 claims description 2
- YMKDRGPMQRFJGP-UHFFFAOYSA-M cetylpyridinium chloride Chemical compound [Cl-].CCCCCCCCCCCCCCCC[N+]1=CC=CC=C1 YMKDRGPMQRFJGP-UHFFFAOYSA-M 0.000 claims description 2
- 229960001927 cetylpyridinium chloride Drugs 0.000 claims description 2
- 235000013922 glutamic acid Nutrition 0.000 claims description 2
- 239000004220 glutamic acid Substances 0.000 claims description 2
- HNDVDQJCIGZPNO-UHFFFAOYSA-N histidine Natural products OC(=O)C(N)CC1=CN=CN1 HNDVDQJCIGZPNO-UHFFFAOYSA-N 0.000 claims description 2
- 239000001103 potassium chloride Substances 0.000 claims description 2
- 235000011164 potassium chloride Nutrition 0.000 claims description 2
- 235000004400 serine Nutrition 0.000 claims description 2
- BJQWBACJIAKDTJ-UHFFFAOYSA-N tetrabutylphosphanium Chemical compound CCCC[P+](CCCC)(CCCC)CCCC BJQWBACJIAKDTJ-UHFFFAOYSA-N 0.000 claims description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical class Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 claims 1
- 125000005207 tetraalkylammonium group Chemical group 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 32
- 238000000926 separation method Methods 0.000 abstract description 5
- 230000002195 synergetic effect Effects 0.000 abstract description 3
- 230000000052 comparative effect Effects 0.000 description 26
- 230000000694 effects Effects 0.000 description 12
- 239000006096 absorbing agent Substances 0.000 description 10
- 238000001179 sorption measurement Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 5
- 238000003860 storage Methods 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 230000009916 joint effect Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 229910016467 AlCl 4 Inorganic materials 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- RLGQACBPNDBWTB-UHFFFAOYSA-N cetyltrimethylammonium ion Chemical compound CCCCCCCCCCCCCCCC[N+](C)(C)C RLGQACBPNDBWTB-UHFFFAOYSA-N 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 125000002704 decyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 125000003187 heptyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 125000004051 hexyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 125000001421 myristyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 125000001400 nonyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 125000002347 octyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 125000000913 palmityl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 125000003698 tetramethyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 125000002948 undecyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
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Classifications
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- 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
-
- 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
- B01D53/22—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 diffusion
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—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
- 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
Definitions
- the invention relates to the technical field of carbon dioxide gas separation, in particular to a carbon dioxide absorbing liquid and a method for capturing carbon dioxide from fuel gas.
- CO2 capture methods mainly include chemical absorption method, adsorption method, membrane separation method, membrane absorption method and cryogenic distillation method, etc., and the most widely used method is chemical absorption method.
- the chemical absorption method generally has the disadvantages of small carbon dioxide adsorption capacity, high energy consumption for absorption liquid regeneration, poor capture effect on highly acidic feed gas, and difficulty in separating high-purity carbon dioxide.
- the purpose of the present invention is to overcome the technical problems of the chemical absorption method, such as small carbon dioxide adsorption capacity, high energy consumption for absorption liquid regeneration, poor capture effect on highly acidic raw material gas, and difficulty in separating high-purity carbon dioxide, to provide a carbon dioxide absorption liquids and methods for capturing carbon dioxide from fuel gases.
- the first aspect of the present invention provides a carbon dioxide absorbing liquid, wherein the carbon dioxide absorbing liquid contains 100 parts by weight of solvent, 10-55 parts by weight of amino acid, 20-65 parts by weight of organic amine, 5 -15 parts by weight of activator and 2-12 parts by weight of accelerator;
- the activator includes activator I and activator II, and the activator I is selected from at least one of alkyl quaternary ammonium ionic liquids, alkyl quaternary phosphonium ionic liquids, and pyridine ionic liquids;
- Activator II is selected from bisamino quaternary phosphonium ionic liquids, amino functionalized imidazole ionic liquids, diamine functional ionic liquids, amino acid ionic liquids, tetramethylguanidine succinate ionic liquids, tetramethyl At least one of guanidine dodecane dicarboxylate ionic liquid and tetramethylguanidine polyethylene glycol dicarboxylate ionic liquid.
- a second aspect of the present invention provides a method of capturing carbon dioxide from fuel gas, said method comprising the steps of:
- step (3) Returning the regenerated lean solution to step (1) as a lean solution.
- the carbon dioxide absorbing liquid provided in the present invention through the synergistic effect between amino acids, organic amines, activators and accelerators, can not only increase the carbon dioxide absorbing capacity of the carbon dioxide absorbing liquid, but also reduce the regeneration energy consumption of the carbon dioxide absorbing liquid , to obtain high-purity carbon dioxide;
- the carbon dioxide absorbing liquid provided in the present invention when containing activator I and activator II, increases the amount of amino acid, and cooperates with a specific amount of organic amine to further increase the carbon dioxide removal rate and reduce regeneration energy consumption, Obtain high-purity regeneration gas;
- the carbon dioxide absorbing liquid provided in the present invention can further improve the carbon dioxide capture effect of the decarburization solvent, reduce regeneration energy consumption, and obtain high-purity carbon dioxide by rationally adjusting the mass ratio of activator I and activator II;
- the method for trapping carbon dioxide from fuel gas provided in the present invention can improve the trapping effect of carbon dioxide through the joint action of porous membrane and specific lean liquid, and obtain purified fuel gas with carbon dioxide dry basis content lower than 3v%.
- Fig. 1 is a schematic diagram of a device for capturing carbon dioxide from fuel gas in the present invention.
- the first aspect of the present invention provides a carbon dioxide absorbing liquid, wherein, the carbon dioxide absorbing liquid contains 100 parts by weight of solvent, 10-55 parts by weight of amino acid, 20-65 parts by weight of organic amine, 5-15 parts by weight An activator and an accelerator of 2-12 parts by weight;
- the activator includes activator I and activator II, and the activator I is selected from at least one of alkyl quaternary ammonium ionic liquids, alkyl quaternary phosphonium ionic liquids, and pyridine ionic liquids;
- the activator II is selected from bisamino quaternary phosphonium ionic liquids, amino functionalized imidazole ionic liquids, diamine functionalized ionic liquids, amino acid ionic liquids, tetramethylguanidine succinate ionic liquids, tetramethylguanidine succinate ionic liquids, At least one of methylguanidine dodecane dicarboxylate ionic liquid and tetramethylguanidine polyethylene glycol dicarboxylate ionic liquid.
- the carbon dioxide absorbing liquid contains 100 parts by weight of solvent, 15-35 parts by weight, preferably 30-35 parts by weight of amino acid, 25-50 parts by weight, preferably 45-50 parts by weight of organic Amine, 6-10 parts by weight, preferably 5-10 parts by weight of activator and 3-5 parts by weight, preferably 4-5 parts by weight of accelerator.
- the carbon dioxide capture liquid when the amount of amino acid, organic amine, activator, accelerator and solvent is limited within the above range, the carbon dioxide capture liquid has a better carbon dioxide capture effect.
- the mass ratio of the amino acid to the organic amine is 0.5-1:1, preferably 0.6-0.8:1.
- the amino acid is selected from glycine, sarcosine, lysine, alanine, glutamic acid, serine, glycine, proline, arginine, histidine at least One, preferably one of glycine, sarcosine, lysine and alanine.
- the organic amine is selected from N-methyl monoethanolamine (MMEA), 2-amino-2-methyl-1-propanol (AMP), N-methyldiethanolamine (MDEA) , monoethanolamine (MEA), diethanolamine (DEA), diisopropanolamine (DIPA), isopropylaminoethanol (IPAE), hydroxyethylpiperazine (HEPZ), morpholine (MOR), diazabicyclo (DBU) and at least one of its derivatives, preferably at least one of N-methylmonoethanolamine, 2-amino-2-methyl-1-propanol, and N-methyldiethanolamine.
- MMEA N-methyl monoethanolamine
- AMP 2-amino-2-methyl-1-propanol
- MDEA N-methyldiethanolamine
- MEA monoethanolamine
- DEA diethanolamine
- DIPA diisopropanolamine
- IPAE isopropylaminoethanol
- HEPZ hydroxyethylpiperazine
- the mass ratio of the activator I to the activator II is 1:1-8.5, preferably 1:2.5-5.
- the carbon dioxide capture effect of the decarburization solvent can be further improved, the regeneration energy consumption can be reduced, and high-purity carbon dioxide can be obtained.
- the present invention does not specifically limit alkyl quaternary ammonium ionic liquids, alkyl quaternary phosphonium ionic liquids, and pyridine ionic liquids.
- alkyl quaternary ammonium ionic liquids alkyl Both quaternary phosphonium-based ionic liquids and pyridine-based ionic liquids can be used in the present invention.
- the activator I is selected from alkylphosphine tetrafluoroborate ([PR x H 4-x ] + [BF 4 ] - ), alkylamine hexafluorophosphate ([NR x H 4-x ] + [PF 6 ] - ), alkyl pyridinium aluminum chloride salt ([RPy] + [AlCl 4 ] - ).
- x is an integer of 1-4
- R is an alkyl group with 1-20 carbon atoms, preferably an alkyl group with 6-16 carbon atoms
- x R can be the same or different, each independently can be hexyl, heptyl, etc.
- the activator I is selected from one of trihexyltetradecylphosphorus tetrafluoroborate, cetyltrimethylammonium hexafluorophosphate, and cetylpyridinium chloride.
- the activator II is selected from 3-propylamino-tributylphosphonium glycinate ([aP 4443 ][Gly]), 3-propylamino-tributylphosphonium alanine ( [aP 4443 ][Ala]), tetraethylammonium glycinate ([N 2222 ][Gly]), tetrabutylammonium glycinate ([N 4444 ][Gly]), tetrabutylphosphonium glycinate [P 4444 ][Gly ], 1-aminopropyl-3-methylimidazolium glycinate ([APmim][Gly]), 3-propylamino-tributylphosphonium-2-hydroxypyridine ([aP 4443 ][2-Op]) More preferably, the activator II is selected from one of [P 4444 ][Gly], [aP 4443 ][2-Op
- the accelerator is selected from sodium chloride and/or potassium chloride, preferably sodium chloride.
- the solvent in the absorption liquid is selected from water.
- a second aspect of the present invention provides a method of capturing carbon dioxide from fuel gas, said method comprising the steps of:
- step (3) Returning the regenerated lean solution to step (1) as a lean solution.
- step (1)
- the fuel gas is selected from highly acidic fuel gas; wherein, the dry basis content of carbon dioxide in the highly acidic fuel gas is 15-60v%, preferably 25-50v%.
- the highly acidic fuel gas is selected from at least one of oilfield associated gas, PSA regeneration gas, biogas, and biocracking gas.
- the PSA regeneration gas is the pressure swing adsorption regeneration gas in the art.
- the method for capturing carbon dioxide from fuel gas provided in the present invention is not particularly limited to fuel gas, and can be especially used to treat highly acidic fuel gas with carbon dioxide dry basis content above 15v%.
- the flow ratio of the fuel gas to the absorption liquid is 1Nm 3 /h:10-80L/h, preferably 1Nm 3 /h:20-50L/h.
- the porous membrane is selected from pressure-resistant porous membranes, preferably hollow fiber membranes; wherein, the inner diameter of the membrane filaments of the hollow fiber membranes is 40-60mm, preferably 45-55mm; The diameter is 0.5-1.2 mm, preferably 0.8-0.9 mm.
- the operating conditions of the indirect contact mass transfer include: the mass transfer temperature is 25-80° C., preferably 35-50° C.; the mass transfer pressure is 1.0-20.0 MPa, preferably 4.0-16.0 MPa.
- the dry content of carbon dioxide in the purified fuel gas is ⁇ 3v%, preferably 1.5-2.5v%.
- the method for capturing carbon dioxide from fuel gas provided by the present invention can further improve the capture effect of carbon dioxide through the joint action of porous membrane and specific lean liquid, and obtain purified fuel gas with dry basis content of carbon dioxide lower than 3v%, and purify fuel Gas can reach the industrial production index.
- step (2)
- the regeneration of the rich solution is not particularly limited in the present invention, and can be performed according to conventional operations in the field.
- the rich liquid is sent to a regeneration tower for regeneration.
- the dry basis content of carbon dioxide in the regeneration gas is ⁇ 95v%, preferably ⁇ 98v%, more preferably ⁇ 99.5v%.
- the regeneration gas obtained after regeneration contains a small amount of water in addition to carbon dioxide.
- the regeneration gas can be dewatered.
- the water removal method of the regenerated gas there is no special limitation on the water removal method of the regenerated gas, and it can be carried out according to conventional operations in the field.
- the regeneration gas can be condensed to remove water.
- the regeneration energy consumption in the regeneration is 1.8-2.9 ⁇ 10 3 kcal/Nm 3 CO 2 , preferably 1.8-2.1 ⁇ 10 3 kcal/Nm 3 CO 2 .
- step (3)
- the regenerated lean liquid is heat-exchanged with the rich liquid and then returned to step (1).
- the regeneration after heat exchange can be The lean solution is cooled again.
- the present invention will be described in detail below by way of examples.
- the following examples and comparative examples are carried out in the device shown in Figure 1, including a membrane absorber 1, a heat exchanger 2, a regeneration tower 3, a lean liquid cooler 4, a lean liquid pump 5 and a fuel gas storage tank 6; wherein, The rich liquid outlet of the membrane absorber 1 is connected with the heat exchanger 2 and the top of the regeneration tower 3 in sequence, and the bottom of the regeneration tower 3 is connected with the heat exchanger 2, the lean liquid pump 5, the lean liquid cooler 4 and the membrane absorber in sequence The lean liquid inlet of 1 is connected, and the fuel gas storage tank 6 is connected with the membrane absorber 1.
- the membrane absorber 1 is a membrane absorber containing a hollow fiber membrane, which comes from Dalian Institute of Chemical Physics, Chinese Academy of Sciences.
- the dry basis content of CO 2 in the purified fuel gas is 1.8v%
- the purity of CO 2 in the obtained regenerated gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.1 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 2 Same as Example 1, the difference is that the lean solution is different, and the composition of the lean solution in Example 2 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 1.5v%
- the purity of CO 2 in the obtained regeneration gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 1.8 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 3 Same as Example 1, the difference is that the lean solution is different, and the composition of the lean solution in Example 3 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 2.0v%
- the purity of CO 2 in the obtained regenerated gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.3 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 Same as Example 1, the difference is that the simulated highly acidic fuel gas and indirect contact mass transfer operating conditions are different, the dry basis content of carbon dioxide in the simulated highly acidic fuel gas in Example 4 is 50v%, and the N content is 50v%; Indirect contact mass transfer was performed through hollow fiber membranes at 40 °C and 16.0 MPa.
- the dry basis content of CO 2 in the obtained purified fuel gas is 2.3v%
- the purity of CO 2 in the obtained regenerated gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.6 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 Same as Example 4, the difference is that the lean solution is different, and the composition of the lean solution in Example 5 is shown in Table 1.
- the dry basis content of CO 2 in the obtained purified fuel gas is 2.1v%
- the purity of CO 2 in the obtained regenerated gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.3 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 6 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Example 6 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 2.5v%
- the purity of CO 2 in the obtained regenerated gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.5 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 7 Same as Example 4, the difference is that the lean solution is different, and the composition of the lean solution in Example 7 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.0v%
- the purity of CO 2 in the obtained regeneration gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.7 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 8 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Example 8 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 2.8v%
- the purity of CO 2 in the obtained regeneration gas is ⁇ 99.5% (dry basis)
- the regeneration energy consumption is 2.9 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 1 Same as Example 1, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 1 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 2.9v%
- the purity of CO 2 in the obtained regenerated gas is 90% (dry basis)
- the regeneration energy consumption is 3.2 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 2 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 2 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.0v%
- the purity of CO 2 in the obtained regenerated gas is 88% (dry basis)
- the regeneration energy consumption is 3.7 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 Same as Example 4, the difference is that the lean solution is different, and the composition of the lean solution in Comparative Example 3 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.1v%
- the purity of CO 2 in the obtained regeneration gas is 85% (dry basis)
- the regeneration energy consumption is 3.6 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 4 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.0v%
- the purity of CO 2 in the obtained regeneration gas is 90% (dry basis)
- the regeneration energy consumption is 3.9 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 Comparative Example 3 and Comparative Example 4, it can be seen that the amount of amino acid and organic amine used is too much or too little, which is not conducive to improving the absorption capacity of carbon dioxide and reducing regeneration energy consumption.
- Example 4 Same as Example 4, the difference is that the lean solution is different, and the composition of the lean solution in Comparative Example 5 is as shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.2v%
- the purity of CO 2 in the obtained regenerated gas is 99% (dry basis)
- the regeneration energy consumption is 3.7 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 By comparing Example 4 and Comparative Example 5, it can be seen that when amino acid salts are used to replace amino acids, it is not conducive to reducing regeneration energy consumption and improving the absorption effect of carbon dioxide.
- Example 6 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 6 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 2.3v%
- the purity of CO 2 in the obtained regenerated gas is 99% (dry basis)
- the regeneration energy consumption is 3.1 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 By comparing Example 4 and Comparative Example 6, it can be seen that the synergistic effect of activator I and activator II can improve the absorption effect of carbon dioxide, reduce the regeneration energy consumption of the carbon dioxide absorption liquid, and obtain high-purity carbon dioxide. With only activator I and no activator II, the regeneration energy consumption of carbon dioxide increased significantly, indicating that the desorption performance of the absorption liquid was worse.
- Example 7 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 7 is shown in Table 1.
- the dry basis content of CO 2 in the purified fuel gas is 3.2v%
- the purity of CO 2 in the obtained regenerated gas is 99% (dry basis)
- the regeneration energy consumption is 2.6 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 By comparing Example 4 and Comparative Example 7, it can be known that only the activator II and no activator I, the absorption capacity of the carbon dioxide absorbing liquid for carbon dioxide decreases, and the content of carbon dioxide in the purified fuel gas is relatively large.
- Example 4 Same as Example 4, the difference is that the barren solution is different.
- the composition of the barren solution in Comparative Example 8 is shown in Table 1, and the activator II is 1-butyl-3-methylimidazole sodium phosphate.
- the dry basis content of CO 2 in the purified fuel gas is 3.3v%
- the purity of CO 2 in the obtained regenerated gas is 86% (dry basis)
- the regeneration energy consumption is 2.8 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 By comparing Example 4 and Comparative Example 8, it can be seen that when 1-butyl-3-methylimidazolium sodium phosphate and trihexyltetradecylphosphorus tetrafluoroborate are co-activated, the adsorption and separation of carbon dioxide is not effective.
- Example 9 Same as Example 4, except that the lean solution is different.
- the composition of the lean solution in Comparative Example 9 is shown in Table 1.
- the dry basis content of CO 2 in the obtained purified fuel gas is 3.4v%
- the purity of CO 2 in the obtained regeneration gas is 98.5% (dry basis)
- the regeneration energy consumption is 2.7 ⁇ 10 3 kcal/Nm 3 CO 2 .
- Example 4 By comparing Example 4 and Comparative Example 9, it can be known that the adsorption and separation effect of carbon dioxide can be improved by adding a promoter.
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Abstract
Description
Claims (23)
- 一种二氧化碳吸收液,其中,所述二氧化碳吸收液含有100重量份的溶剂、10-55重量份的氨基酸、20-65重量份的有机胺、5-15重量份的活化剂和2-12重量份的促进剂;其中,所述活化剂包括活化剂I和活化剂II,所述活化剂I选自烷基季铵类离子液体、烷基季鏻类离子液体、吡啶类离子液体中的至少一种;所述活化剂II选自双氨基季鏻类离子液体、胺基功能化咪唑类离子液体、双胺基功能化离子液体、氨基酸类离子液体、四甲基胍丁二酸盐类离子液体、四甲基胍十二烷二羧酸盐离子液体、四甲基胍聚乙二醇二羧酸盐离子液体中的至少一种。
- 根据权利要求1所述二氧化碳吸收液,其中,所述二氧化碳吸收液含有100重量份的溶剂、15-35重量份的氨基酸,25-50重量份的45-50重量份的有机胺,6-10重量份的活化剂和3-5重量份的促进剂。
- 根据权利要求2所述的二氧化碳吸收液,其中,所述二氧化碳吸收液含有100重量份的溶剂、30-35重量份的氨基酸,45-50重量份的有机胺,5-10重量份的活化剂和4-5重量份的促进剂。
- 根据权利要求1-3中任意一项所述的二氧化碳吸收液,其中,所述氨基酸选自甘氨酸、肌氨酸、赖氨酸、丙氨酸、谷氨酸、丝氨酸、氨基乙酸、脯氨酸、精氨酸、组氨酸中的至少一种。
- 根据权利要求4所述的二氧化碳吸收液,其中,所述氨基酸为甘氨酸、肌氨酸、赖氨酸、丙氨酸中的一种。
- 根据权利要求1-5中任意一项所述的二氧化碳吸收液,其中,所述有机胺选自N-甲基一乙醇胺、2-氨基-2-甲基-1-丙醇、N-甲基二乙醇胺、一乙醇胺、二乙醇胺、二异丙醇胺、异丙胺基乙醇、羟乙基 哌嗪、吗啉、二氮杂二环及其衍生物中的至少一种。
- 根据权利要求6所述的二氧化碳吸收液,其中,所述有机胺选自选自N-甲基一乙醇胺、2-氨基-2-甲基-1-丙醇、N-甲基二乙醇胺中的至少一种。
- 根据权利要求1-7中任意一项所述的二氧化碳吸收液,其中,所述氨基酸和有机胺质量比为0.5-1:1。
- 根据权利要求8所述的二氧化碳吸收液,其中,所述氨基酸和有机胺质量比为0.6-0.8:1。
- 根据权利要求1-9中任意一项所述的二氧化碳吸收液,其中,所述活化剂I和活化剂II的质量比为1:1-8.5。
- 根据权利要求10所述的二氧化碳吸收液,其中,所述活化剂I和活化剂II的质量比为1:2.5-5。
- 根据权利要求1-11中任意一项所述的二氧化碳吸收液,其中,所述活化剂I选自烷基膦四氟硼酸盐、烷基胺六氟磷酸盐、烷基吡啶氯化铝盐中的一种;优选地,所述活化剂I选自三己基十四烷基四氟硼酸磷、四氟硼酸四烷基铵、十六烷基氯化吡啶中的一种。
- 根据权利要求1-12中任意一项所述的二氧化碳吸收液,其中,所述活化剂II选自3-丙胺基-三丁基鳞甘氨酸盐、3-丙胺基-三丁基鏻丙氨酸盐、甘氨酸四乙基铵、甘氨酸四丁基铵、甘氨酸四丁基磷、1-氨丙基-3-甲基咪唑甘氨酸盐、3-丙胺基-三丁基鏻-2-羟基吡啶中的至少一种。
- 根据权利要求1-13中任意一项所述的二氧化碳吸收液,其中,所述促进剂选自氯化钠和/或氯化钾,所述溶剂选自水。
- 一种从燃料气中捕集二氧化碳的方法,其特征在于,所述方 法包括以下步骤:(1)将燃料气与贫液通过多孔膜进行间接接触传质,得到富液和净化燃料气;其中,所述贫液选自权利要求1-14中任意一项所述二氧化碳吸收液;(2)将所述富液进行再生,得到再生贫液和再生气;(3)将所述再生贫液作为贫液返回步骤(1)。
- 根据权利要求15所述的方法,其中,所述燃料气选自高酸性燃料气;其中,所述高酸性燃料气中二氧化碳的干基含量为15-60v%。
- 根据权利要求16所述的方法,其中,所述高酸性燃料气中二氧化碳的干基含量为25-50v%。
- 根据权利要求16或17所述的方法,其中,所述高酸性燃料气选自油田伴生气、PSA再生气、生物沼气、生物裂解气中的至少一种。
- 根据权利要求15-18中任意一项所述的方法,其中,所述燃料气与所述吸收液的流量比为1Nm 3/h:10-80L/h。
- 根据权利要求19所述的方法,其中,所述燃料气与所述吸收液的流量比为1Nm 3/h:20-50L/h。
- 根据权利要求15-20中任意一项所述的方法,其中,所述多孔膜为中空纤维膜。
- 根据权利要求21所述的方法,其中,所述中空纤维膜的膜丝内径为40-60mm,膜丝外径为0.5-1.2mm;优选地,所述中空纤维膜的膜丝内径为45-55mm,膜丝外径为0.8-0.9mm。
- 根据权利要求15-22中任意一项所述的方法,其中,所述间接接触传质的操作条件包括:传质温度为25-80℃,传质压力为 1-20MPa;优选地,传质温度为35-50℃;传质压力为4-16MPa。
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Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101700454A (zh) * | 2009-11-25 | 2010-05-05 | 南京大学 | 一种绿色二氧化碳吸收剂 |
US20110014100A1 (en) * | 2008-05-21 | 2011-01-20 | Bara Jason E | Carbon Sequestration Using Ionic Liquids |
US20110214566A1 (en) * | 2010-03-02 | 2011-09-08 | Hyundai Motor Company | Carbon dioxide absorbents |
CN102228772A (zh) * | 2011-07-11 | 2011-11-02 | 中国石油化工集团公司 | 一种胺溶液膜吸收法捕集烟气中二氧化碳的工艺方法 |
WO2011147033A2 (en) * | 2010-05-27 | 2011-12-01 | Saint Mary's University | Compositions and methods for capturing carbon dioxide |
CN102527192A (zh) * | 2011-12-23 | 2012-07-04 | 中国石油化工股份有限公司 | 含有离子液体的二氧化碳吸收剂 |
CN102553396A (zh) * | 2011-12-23 | 2012-07-11 | 武汉凯迪工程技术研究总院有限公司 | 一种高效低能耗捕集电站烟气中二氧化碳的方法及其设备 |
CN104415642A (zh) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | 用于二氧化碳捕集的双氨基离子液体-mdea复合吸收剂 |
US20150125372A1 (en) * | 2011-05-13 | 2015-05-07 | Ion Engineering | Compositions and methods for gas capture processes |
CN105561757A (zh) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | 一种离子液体活化的燃烧后二氧化碳捕集溶剂 |
-
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-
2022
- 2022-10-24 WO PCT/CN2022/127150 patent/WO2023066400A1/zh active Application Filing
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20110014100A1 (en) * | 2008-05-21 | 2011-01-20 | Bara Jason E | Carbon Sequestration Using Ionic Liquids |
CN101700454A (zh) * | 2009-11-25 | 2010-05-05 | 南京大学 | 一种绿色二氧化碳吸收剂 |
US20110214566A1 (en) * | 2010-03-02 | 2011-09-08 | Hyundai Motor Company | Carbon dioxide absorbents |
WO2011147033A2 (en) * | 2010-05-27 | 2011-12-01 | Saint Mary's University | Compositions and methods for capturing carbon dioxide |
US20150125372A1 (en) * | 2011-05-13 | 2015-05-07 | Ion Engineering | Compositions and methods for gas capture processes |
CN102228772A (zh) * | 2011-07-11 | 2011-11-02 | 中国石油化工集团公司 | 一种胺溶液膜吸收法捕集烟气中二氧化碳的工艺方法 |
CN102527192A (zh) * | 2011-12-23 | 2012-07-04 | 中国石油化工股份有限公司 | 含有离子液体的二氧化碳吸收剂 |
CN102553396A (zh) * | 2011-12-23 | 2012-07-11 | 武汉凯迪工程技术研究总院有限公司 | 一种高效低能耗捕集电站烟气中二氧化碳的方法及其设备 |
CN104415642A (zh) * | 2013-08-20 | 2015-03-18 | 中国石油化工股份有限公司 | 用于二氧化碳捕集的双氨基离子液体-mdea复合吸收剂 |
CN105561757A (zh) * | 2014-10-14 | 2016-05-11 | 中国石油化工股份有限公司 | 一种离子液体活化的燃烧后二氧化碳捕集溶剂 |
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