CN101804287B - Absorbing agent for catching or separating carbon dioxide - Google Patents

Absorbing agent for catching or separating carbon dioxide Download PDF

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CN101804287B
CN101804287B CN2010101529461A CN201010152946A CN101804287B CN 101804287 B CN101804287 B CN 101804287B CN 2010101529461 A CN2010101529461 A CN 2010101529461A CN 201010152946 A CN201010152946 A CN 201010152946A CN 101804287 B CN101804287 B CN 101804287B
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gas
absorbent
carbon dioxide
separating
absorption
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CN101804287A (en
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陈健
郭东方
费维扬
骆广生
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Tsinghua University
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    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

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Abstract

The invention relates to an absorbing agent for catching or separating carbon dioxide from gas mixture, which mainly comprises the components by weight percent: 10-50wt% of N-ethylethanolamine, 10-40wt% of tetramethylene sulfone and balance water. The absorbing agent adopts the N-ethylethanolamine as effective component, and the N-ethylethanolamine has high solubility for low-pressure carbon dioxide, good desorbing effect, lower reaction heat of absorption reaction and lower energy consumption for catching or separating the carbon dioxide; and as the 3-dimethyl amino-1-propyl alcohol has the functions of improving the desorbing effect and reducing the volatilization of water, so that the energy consumption of desorbing is further reduced. The absorbing agent can be used for catching or separating the carbon dioxide in various gas mixtures such as flue gas, refinery gas, natural gas, synthesis gas, shift gas, hydrogen preparation gas and the like.

Description

The absorbent of a kind of capture or separating carbon dioxide
Technical field
The present invention relates to chemical materials and gas separation technique field, be specifically related to a kind of from admixture of gas, the capture or separating carbon dioxide (CO 2) absorbent.
Background technology
CO 2The isothermal chamber gas purging is a principal element that causes climate change, how from being rich in CO 2Admixture of gas in, capture or separation of C O 2Just seem very important.These admixture of gas comprise flue gas, refinery gas, natural gas, synthesis gas, conversion gas and hydrogen or the like.Generally contain 5%～50% CO in these admixture of gas 2, other main gas composition comprises N 2, O 2, CO, H 2, CH 4, C 2H 6, SO 2, H 2S and organic sulfur CH 3S, COS etc.; The pressure range of gas is big, and (50～9000kPa), suitable chemical absorbing or the Chemical Physics composite absorbent method of adopting captures separation of C O 2Component.
Comparatively ripe chemical absorption method captures separation of C O in the industry both at home and abroad at present 2Technology MEA method (MEA), diethanolamine method (DEA), diisopropanolamine process (DIPA) and methyl diethanolamine method (MDEA) are arranged.In order to improve absorbent solution to CO 2Infiltration rate, so, add infiltration rate solvent such as MEA (MEA) and piperazine (PZ) etc. faster, form the method for absorbing and separating of some modified forms to diisopropanolamine (DIPA) (DIPA), the methyl diethanolamine slower solvents of infiltration rate such as (MDEA).
In order further to cut down the consumption of energy, because it is to CO 2Solubility is high, desorption effect is better, and the circulating load that absorbs desorb is higher, and 2-amino-2-methyl-1-propanol (AMP) bulky amine method has also obtained some application.But because the special construction of these bulky amine causes degraded in use many, use cost is still higher.
Therefore, be necessary to propose the absorbent of good capture of a kind of assimilation effect or separating carbon dioxide.
Summary of the invention
The purpose of this invention is to provide a kind of from admixture of gas, the capture or the absorbent of separating carbon dioxide.
Another object of the present invention provides the method for using of above-mentioned absorbent.
Said absorbent comprises the component of following percetage by weight:
N-ehtylethanolamine (be also referred to as 2-ethyl amido alcohol, ethyl oxyethylamine, 2-ethamine ethanol, be abbreviated as EMEA): 10wt%～50wt%;
Sulfolane (being abbreviated as TMS): 10wt%～40wt%;
Water: surplus.
Said components is the neccessary composition of absorbent according to the invention, and the N-ehtylethanolamine is big to the solubility of low pressure CO 2, and desorption effect is good, and the reaction heat of absorption reaction is lower simultaneously, and energy consumption is lower concerning capturing separating carbon dioxide; And sulfolane has the effect that improves desorption effect and the volatile quantity that reduces water, can further reduce the desorb energy consumption;
In addition, said absorbent can also comprise one or more in MEA, methylethanolamine, piperazine, the physical solvent except that sulfolane, inorganic salts or the auxiliary agent, and its percentage by weight is 2wt%～30wt%;
Particularly preferably be, in the said absorbent, MEA, methylethanolamine, piperazine, inorganic salts and auxiliary agent the percetage by weight sum be no more than 10wt%.
Wherein, said other physical solvents (except that sulfolane) are one or both in methyl-sulfoxide, the N-methyl pyrrolidone; Preferred its percetage by weight is no more than 20wt%.
Said inorganic salts are K 2CO 3, Na 2CO 3Or their mixture.
Said auxiliary agent is one or more in corrosion inhibitor, anti-oxidant and the antifoaming agent.
Said corrosion inhibitor, anti-oxidant and antifoaming agent can be selected water treatment field medicament commonly used, can select vanadium pentoxide etc. like corrosion inhibitor; Anti-oxidant can be selected sodium sulfite etc.; Antifoaming agent can be selected organosilan etc.;
Mentioned component is directly mixed, just can obtain absorbent of the present invention.
The present invention also provides the method for using of above-mentioned absorbent.
Absorbent according to the invention can be used for capturing or separating various gas mixtures, comprises the CO in flue gas, refinery gas, natural gas, synthesis gas, conversion gas and hydrogen or the like 2Can the absorption tower of using said absorbent be arranged at the decarbonization process of conventional absorption, flash distillation, heat exchange, desorb; Or the technology that after heat exchange, gets into the stage casing, absorption tower from desorber stage casing extraction semi lean solution; Or multistage absorbs the technology of multistage desorb, or is used for the technology of absorption and separation sulfur dioxide, hydrogen sulfide and organic sulfurs such as cos and methyl mercaptan simultaneously.
Experiment showed, and utilize absorbent according to the invention to capture or separation of C O 2Process conditions be: the temperature that lyosoption enters the absorption tower is 30～80 ℃; The temperature of lean solution is 80～150 ℃ at the bottom of the regenerator; Pressure at the bottom of the regenerator is 50～500kPa.
Use the N-ehtylethanolamine as active ingredient in the absorbent of the present invention, because the N-ehtylethanolamine is big to the solubility of low pressure CO 2, desorption effect is good, and the reaction heat of absorption reaction is lower simultaneously, and energy consumption is lower concerning capturing separating carbon dioxide; The N-ehtylethanolamine is a kind of secondary amine simultaneously, and carbochain is a straight chain, and the stability of molecule is good than monoethanolamine, can reduce the degraded loss of solvent in use significantly; And the adding of sulfolane can improve the desorption effect of carbon dioxide, reduces the volatile quantity of water, thereby further reduces the desorb energy consumption.
The specific embodiment
Following examples are used to explain the present invention, but are not used for limiting scope of the present invention.
Embodiment 1
Getting three parts of N-ehtylethanolamines (EMEA) content is that 10wt%, sulfolane (TMS) content are the aqueous solution (i.e. 80% water) of 10wt%, is 40 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 10kPa, 45kPa, 100kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 1.
The experimental result of the aqueous solution of 40 ℃ in table 1,10wt%N-ehtylethanolamine+10wt% sulfolane
Figure GSA00000073824000031
Embodiment 2
Getting three parts of N-ethyl hexanol amine contents is that 10wt%, sulfolane content are the aqueous solution (i.e. 80% water) of 10wt%, is 120 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 20kPa, 60kPa, 100kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 2.
The experimental result of the aqueous solution of 120 ℃ in table 2,10wt%N-ehtylethanolamine+10wt% sulfolane
Figure GSA00000073824000041
Embodiment 3
Getting three parts of N-ethyl hexanol amine contents is that 22wt% and sulfolane content are the aqueous solution (i.e. 48% water) of 30wt%, is 40 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 8.6kPa, 18kPa, 63kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 3.
The experimental result of the aqueous solution of 40 ℃ in table 3,22wt%N-ehtylethanolamine+30wt% sulfolane
Figure GSA00000073824000042
Embodiment 4
Getting three parts of N-ethyl hexanol amine contents is that 22wt% and sulfolane content are the aqueous solution (i.e. 48% water) of 30wt%, is 120 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 22kPa, 58kPa, 106kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 4.
The experimental result of the aqueous solution of 120 ℃ in table 4,22wt%N-ehtylethanolamine+30wt% sulfolane
Embodiment 5
Getting three parts of N-ehtylethanolamines is that 50wt% and sulfolane content are the aqueous solution (i.e. 10% water) of 40wt%, is 40 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 9kPa, 40kPa, 100kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 5.
The experimental result of the aqueous solution of 40 ℃ in table 5,50wt%N-ehtylethanolamine+40wt% sulfolane
Figure GSA00000073824000052
Embodiment 6
Getting three parts of N-ehtylethanolamines is that 50wt% and sulfolane content are the aqueous solution (i.e. 10% water) of 40wt%, is 120 ℃ with temperature, gas phase CO 2Partial pressure is the CO that contains of 25kPa, 50kPa, 1054kPa 2And N 2Mist import three parts of said solvents respectively, after gas-liquid two-phase reaches balance, CO in the lyosoption 2With CO in the mol ratio of N-ehtylethanolamine and the lyosoption 2Solubility referring to table 6.
The experimental result of the aqueous solution of 120 ℃ in table 6,50wt%N-ehtylethanolamine+40wt% sulfolane
Figure GSA00000073824000061
Can find out from embodiment 1 and embodiment 2, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 45kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 60kPa, and the aqueous solution of 1 liter of 10wt%EEA+10wt%TMS can absorption and separation CO 2Amount be 46-18=28 gram;
Can find out from embodiment 3 and embodiment 4, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 18kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 58kPa, and the aqueous solution of 1 liter of 22wt%EEA+30wt%TMS can absorption and separation CO 2Amount be 80-17=53 gram;
Can find out from embodiment 5 and embodiment 6, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 40kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 50kPa, and the aqueous solution of 1 liter of 50%EEA+40wt%TMS can absorption and separation CO 2Amount be 123-16=107 gram.
Embodiment 7
N-ehtylethanolamine, sulfolane and the MEA getting weight ratio and be 5: 1: 0.5 directly mix, and are prepared into raw sorbent.
Be used for capturing the CO of refinery gas 2, during application, the weight of raw sorbent by N-ehtylethanolamine, sulfolane and MEA is respectively: 50wt%, 10wt%, 5wt% dissolves in percetage by weight is the water of 35wt%, and agent is absorbed.
At 40 ℃ of following CO 2Dividing potential drop absorbs during for 10kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 50kPa, and 1 liter of absorbent can capture separation of C O 2Amount be 110-25=85 gram.
Embodiment 8
N-ehtylethanolamine, the sulfolane getting weight ratio and be 1: 4 directly mix; Percetage by weight by N-ehtylethanolamine, sulfolane is respectively: 10wt%, 40wt% add percetage by weight and are respectively in methyl-sulfoxide and the water of 10wt%, 40wt% and are prepared into absorbent.
Be used for capturing the CO of conversion gas 2, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 450kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 50kPa, and 1 liter of absorbent can capture separation of C O 2Amount be 50-10=40 gram.
Embodiment 9
Getting weight ratio and be 1: 2 N-ehtylethanolamine, sulfolane, is 10% by the percetage by weight of N-ehtylethanolamine, adds the Na of 2wt% 2CO 3, it (is N-ehtylethanolamine, sulfolane, Na that methylethanolamine and the piperazine that is respectively 3wt%, 3wt% directly mixes 2CO 3, methylethanolamine and piperazine weight ratio be 10: 20: 2: 3: 3), be prepared into raw sorbent.
During application; Is 10wt% with raw sorbent by the percetage by weight of N-ehtylethanolamine, is respectively 48wt% with percetage by weight, 12% water and N-methyl pyrrolidone mix, and then sneaks into 2% corrosion inhibitor and antifoaming agent; Stir, the agent aqua is absorbed.
Be used for capturing the CO of hydrogen 2, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 450kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 50kPa, and 1 liter of absorbent can capture separation of C O 2Amount be 85-15=70 gram.
Embodiment 10
N-ehtylethanolamine, the sulfolane getting weight ratio and be 2.5: 1 directly mix, and are prepared into raw sorbent.
During application, the solvent raw material is respectively 25%, 10% by the percetage by weight of N-ehtylethanolamine, sulfolane, adds MEA, piperazine, K 2CO 3, Na 2CO 3Percetage by weight be respectively: 2wt%, 3wt%, 2wt% and 2wt% dissolve in percetage by weight is the water of 55wt%, add the anticorrisive agent that percetage by weight is 1wt% at last, the agent aqua is absorbed.
Be used for capturing the CO of flue gas 2, at 40 ℃ of following CO 2Dividing potential drop absorbs during for 10kPa, at 120 ℃ of following CO 2Dividing potential drop is carried out desorb during for 50kPa, and 1 liter of absorbent can capture separation of C O 2Amount be 90-20=70 gram.

Claims (4)

1. one kind captures from admixture of gas or the absorbent of separating carbon dioxide, is made up of the component of following percetage by weight:
N-ehtylethanolamine: 10wt%～50wt%;
Sulfolane: 10wt%～40wt%;
Water: surplus.
2. the application of the described absorbent of claim 1 is characterized in that, said absorbent is used for capturing or the CO of separating gas mixture 2, said admixture of gas comprises flue gas, refinery gas, natural gas, synthesis gas, conversion gas or hydrogen.
3. application as claimed in claim 2; It is characterized in that; The absorption tower of using said absorbent is arranged at the decarbonization process of conventional absorption, flash distillation, heat exchange, desorb, or the technology that after heat exchange, gets into the stage casing, absorption tower from desorber stage casing extraction semi lean solution, or the technology of multistage absorption multistage desorb; Or be used for the technology of absorption and separation sulfur dioxide, hydrogen sulfide and cos and methyl mercaptan simultaneously, be used for capturing or the CO of separating gas mixture 2
4. application as claimed in claim 3 is characterized in that, said absorbent captures or separation of C O 2Process conditions be: the temperature that absorbent enters the absorption tower is 30～80 ℃; The temperature of lean solution is 80～150 ℃ at the bottom of the regenerator; Pressure at the bottom of the regenerator is 50～500kPa.
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CN102743952A (en) * 2011-12-13 2012-10-24 南京大学 Low temperature co-melting organic acid salt-sulfolane formulated solution and SO2 capturing process thereof
CN105032123B (en) * 2015-06-30 2018-07-06 中国华能集团清洁能源技术研究院有限公司 A kind of application method of middle low-temp recovery collecting carbonic anhydride absorbent
CN106984152B (en) * 2017-03-27 2019-08-09 大连理工大学 It is a kind of for trapping the two-phase mixture of carbon dioxide
CN110124448B (en) * 2019-04-22 2021-12-21 浙江工业大学 Ternary double-liquid-phase absorbent for treating carbon dioxide in flue gas
CN110201490A (en) * 2019-06-21 2019-09-06 江苏新海石化有限公司 A kind of amine liquid regenerative system
CN112546840B (en) * 2020-11-18 2022-02-25 清华大学 Carbon dioxide absorbent and carbon dioxide absorption method thereof
CN113318571A (en) * 2021-05-27 2021-08-31 华侨大学 For capturing CO2Biphasic absorbent and use thereof
CN113731119A (en) * 2021-09-10 2021-12-03 湖南大学 Liquid-liquid phase change absorbent with controllable carbon dioxide capture threshold
CN114870570B (en) * 2022-05-31 2023-10-03 西南化工研究设计院有限公司 Liquid-solid phase-splitting absorbent for separating carbon dioxide

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EP0348251B2 (en) * 1988-05-24 1997-08-13 Elf Aquitaine Production Liquid absorbant of acid gases containing a tertiary alcanolamin compound and an absorption activator for CO2 and its use for the deacidification of CO2 and possibly other acid gases
CN100379485C (en) * 2002-01-14 2008-04-09 国际壳牌研究有限公司 Process for removing carbon dioxide from gas mixtures
CN101279181A (en) * 2008-05-28 2008-10-08 清华大学 Absorbing solvent for capturing or separating carbon dioxide from gas mixture or liquid gas

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