CN117582804A - Liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of coal-fired power plant, preparation method and application - Google Patents
Liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of coal-fired power plant, preparation method and application Download PDFInfo
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 230000002745 absorbent Effects 0.000 title claims abstract description 85
- 239000002250 absorbent Substances 0.000 title claims abstract description 85
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 72
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 72
- 239000007788 liquid Substances 0.000 title claims abstract description 63
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 21
- 239000003546 flue gas Substances 0.000 title claims description 21
- 238000002360 preparation method Methods 0.000 title claims description 7
- 239000012071 phase Substances 0.000 claims abstract description 114
- BFSVOASYOCHEOV-UHFFFAOYSA-N 2-diethylaminoethanol Chemical compound CCN(CC)CCO BFSVOASYOCHEOV-UHFFFAOYSA-N 0.000 claims abstract description 64
- RPNUMPOLZDHAAY-UHFFFAOYSA-N Diethylenetriamine Chemical compound NCCNCCN RPNUMPOLZDHAAY-UHFFFAOYSA-N 0.000 claims abstract description 64
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000010521 absorption reaction Methods 0.000 claims abstract description 35
- 239000007791 liquid phase Substances 0.000 claims abstract description 19
- 238000003795 desorption Methods 0.000 claims abstract description 18
- 238000000034 method Methods 0.000 claims abstract description 18
- 238000002156 mixing Methods 0.000 claims abstract description 15
- 239000007789 gas Substances 0.000 claims description 9
- 238000010438 heat treatment Methods 0.000 claims description 5
- 239000003973 paint Substances 0.000 claims 1
- 230000008929 regeneration Effects 0.000 abstract description 30
- 238000011069 regeneration method Methods 0.000 abstract description 30
- 238000005265 energy consumption Methods 0.000 abstract description 18
- 238000004064 recycling Methods 0.000 abstract 1
- 239000000243 solution Substances 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 7
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 6
- 238000005191 phase separation Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- IMUDHTPIFIBORV-UHFFFAOYSA-N aminoethylpiperazine Chemical compound NCCN1CCNCC1 IMUDHTPIFIBORV-UHFFFAOYSA-N 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- PYSGFFTXMUWEOT-UHFFFAOYSA-N 3-(dimethylamino)propan-1-ol Chemical compound CN(C)CCCO PYSGFFTXMUWEOT-UHFFFAOYSA-N 0.000 description 1
- KXDHJXZQYSOELW-UHFFFAOYSA-M Carbamate Chemical compound NC([O-])=O KXDHJXZQYSOELW-UHFFFAOYSA-M 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- -1 alcohol amine Chemical class 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 150000003141 primary amines Chemical class 0.000 description 1
- BDERNNFJNOPAEC-UHFFFAOYSA-N propan-1-ol Chemical compound CCCO BDERNNFJNOPAEC-UHFFFAOYSA-N 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003335 secondary amines Chemical class 0.000 description 1
- 230000009919 sequestration Effects 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 150000003512 tertiary amines Chemical class 0.000 description 1
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
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- 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
- B01D2251/80—Organic bases or salts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Gas Separation By Absorption (AREA)
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Abstract
The liquid-liquid two-phase absorbent comprises Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water, and the liquid-liquid two-phase absorbent is obtained after full mixing; in the carbon dioxide absorption process, the mixed gas containing carbon dioxide is introduced into a liquid-liquid two-phase absorbent, and the liquid-liquid two-phase absorbent absorbs CO 2 Then the uniform liquid phase is converted into liquid-liquid two phases, most carbon dioxide products are concentrated in a lower liquid phase, the lower liquid phase is a rich phase, and an upper liquid phase is a lean phase; in the carbon dioxide desorption processHeating the rich phase to release carbon dioxide; mixing the rich phase and the lean phase of the released carbon dioxide, recycling, and absorbing the carbon dioxide again; the invention has the advantages of strong absorption capacity, low regeneration energy consumption and the like.
Description
Technical Field
The invention belongs to the technical field of carbon dioxide capture, and particularly relates to a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant, a preparation method and application thereof.
Background
With the acceleration of global industrialization, the massive emission of carbon dioxide causes climate warming, and carbon dioxide capture and sequestration (CCUS) is used as a large-scale greenhouse gas emission reduction technology, which becomes one of important paths for coping with global climate warming. Because the flue gas of the coal-fired power plant has large flow rate and CO 2 Low partial pressure and complex composition (except CO 2 In addition, there is a higher NO content x 、SO x And pollutants such as dust) and the like, in a plurality of carbon trapping technologies, the chemical absorption method has good adaptability to the existing flue gas purification process of the coal-fired power plant, and the process is mature and gradually develops into the flue gas CO of the coal-fired power plant with the most application potential at the present stage 2 One of the trapping techniques. Organic alcohol amine solution represented by ethanolamine (MEA) has high absorption activity and low cost, and becomes the chemical absorbent with the most wide industrial application, but the mass fraction of amine in the traditional organic amine absorbent is generally not more than 30 percent, the water accounts for 70 percent, and a large amount of energy is consumed in the heating (sensible heat) and evaporation (latent heat) of the water during the regeneration, so that the regeneration energy consumption is overhigh (3.6-4.0 GJ/t CO) 2 ) Limiting its industrial application. Therefore, the development of novel low energy absorber is a current research hotspot.
Patent application publication No. CN101804286A discloses an absorbent for capturing carbon dioxide in a mixed gas, which comprises 10 to 40wt% of 3-dimethylamino-1-propanol, 5 to 10wt% of primary or secondary amine, and the balance of water. The absorbent reduces the reaction heat to a certain extent, but has higher overall water content, and a large amount of water still evaporates during regeneration, so that the regeneration energy consumption is high.
Patent application publication No. CN112892160A discloses a phase change absorbent for capturing carbon dioxide, comprising10 to 40 weight percent of N-Aminoethylpiperazine (AEP), wherein the mass ratio of N-propanol to water is 4: 6-6: 4. the absorbent reduces the volume of rich phase by phase separation on the basis of ensuring high absorption performance, but has higher reaction heat of AEP (1.9 GJ/t CO) 2 ) The regeneration energy consumption is higher (2.74 GJ/t CO) 2 )。
Disclosure of Invention
In order to overcome the defects in the prior art, the invention aims to provide a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of coal-fired power plants, a preparation method and application thereof, which adopts high-amine-concentration Diethylenetriamine (DETA) and N, N-Diethylaminoethanol (DEEA) to prepare a water-reduced DETA-DEEA two-phase absorbent, can reduce the fractional phase ratio, reduce the volume of a regeneration solution, thereby having the potential of reducing regeneration energy consumption and improving CO 2 The invention has the advantages of high performance, low water content and low energy consumption.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant comprises Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water.
The mass percentage concentration of the Diethylenetriamine (DETA) is 25wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 50wt%, and the balance is water.
The invention also provides a preparation method of the liquid-liquid two-phase absorbent for capturing carbon dioxide in the flue gas of the coal-fired power plant, which comprises the following steps: uniformly mixing Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water according to a proportion, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water, and fully mixing to obtain a uniform-phase solution, thus obtaining the liquid-liquid two-phase absorbent for capturing carbon dioxide.
Uniformly mixing the Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water according to a proportion, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 25wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 50wt%, and the balance is water, and fully mixing to obtain a uniform-phase solution, thus obtaining the liquid-liquid two-phase absorbent for capturing carbon dioxide.
The invention also provides application of the liquid-liquid two-phase absorbent for capturing carbon dioxide in the flue gas of the coal-fired power plant, in the carbon dioxide absorption process, the mixed gas containing the carbon dioxide is introduced into the liquid-liquid two-phase absorbent, the liquid-liquid two-phase absorbent is converted into liquid-liquid two phases from a uniform liquid phase after absorbing the carbon dioxide, most carbon dioxide products are concentrated in a lower liquid phase, the lower liquid phase is a rich phase, and an upper liquid phase is a lean phase; in the carbon dioxide desorption process, heating the rich phase to release carbon dioxide; and (3) mixing the desorbed rich phase with the absorbed lean phase to form a liquid-liquid two-phase absorbent, and circularly absorbing and desorbing the carbon dioxide.
The volume percentage of carbon dioxide in the mixed gas containing carbon dioxide is 10-15%.
Conditions of the carbon dioxide absorption process: the absorption temperature is 40-50 ℃.
Conditions of the carbon dioxide desorption process: the desorption temperature is 100-120 ℃.
Compared with the prior art, the technical scheme provided by the invention has the following beneficial technical effects:
1. the two-phase absorbent provided by the invention is automatically divided into an upper layer and a lower layer of liquid-liquid after absorbing carbon dioxide to a certain amount, the volume of the rich phase is only 40% -60% of the total volume, and only 40% -60% of the rich phase is required to be desorbed during regeneration, so that the regeneration heat and the trapping cost in the carbon dioxide trapping process are reduced.
2. The two-phase absorbent provided by the invention takes Diethylenetriamine (DETA) as a main absorbent, and the DETA has a plurality of amino structures, so that the high absorption performance of the liquid-liquid two-phase absorbent can be ensured, and the absorption load can reach 3.7mol/L.
3. The two-phase absorbent provided by the invention takes N, N-Diethylaminoethanol (DEEA) as a phase-splitting agent, has good phase-splitting capacity, reduces the water content of a system, reduces the water solution entering rich liquid, reduces the evaporation heat of water, further reduces the regeneration energy consumption, and reduces the regeneration energy consumption to 2.42GJ/t CO 2 。
In conclusion, the two-phase absorbent provided by the invention has the characteristics of large carbon dioxide absorption capacity, high absorption rate, large circulation capacity, and the carbon dioxide trapping by using the two-phase absorbent has the advantages of strong absorption capacity, low regeneration energy consumption and the like.
Drawings
FIG. 1 shows the absorption of CO by the liquid-liquid two-phase absorbent of the present invention 2 And a phase separation condition chart.
FIG. 2 is a graph comparing the absorption performance of the liquid-liquid two-phase absorbent of the present invention and MEA.
FIG. 3 is a graph comparing desorption performance of the liquid-liquid two-phase absorbent of the present invention and MEA.
Fig. 4 is a graph of regenerated energy consumption versus the liquid-liquid two-phase absorbent of the present invention and MEA.
Detailed Description
The present invention will be described in more detail with reference to the following examples and drawings.
A liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant comprises Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water.
The liquid-liquid two-phase absorbent, DETA is the main absorbent. DETA has multiple amino structures, and is easy to react with CO 2 The chemical reaction can be carried out, so that the high absorption performance of the liquid-liquid two-phase absorbent can be ensured; the volatility is low, so that the recovery of the absorbent is facilitated; has lower reaction heat than the MEA.
The liquid-liquid two-phase absorbent, DEEA is the phase-splitting agent. DEEA as tertiary amine with CO 2 The product is insoluble, and can promote the two-phase absorbent to absorb CO 2 After that, phase separation occurs, and the solution is carried outOnly the rich phase is heated during absorption, so that the quantity of regenerated solution can be reduced, and the low regeneration energy consumption of the phase change absorbent is ensured; it is combined with CO 2 The reaction can form carbonate and bicarbonate which are easy to decompose, thereby being beneficial to the regeneration of the absorbent; the presence of DEEA ensures DETA priority over CO 2 The reaction, thus, DETA has a higher CO 2 Absorption capacity.
The liquid-liquid two-phase absorbent is prepared from water serving as a solvent. The water can effectively dissolve the absorption product, and promote the liquid-liquid two-phase absorbent to CO 2 While avoiding the formation of solid precipitates.
The invention also provides a preparation method of the liquid-liquid two-phase absorbent for capturing carbon dioxide in the flue gas of the coal-fired power plant, which comprises the following steps: uniformly mixing Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water according to a proportion, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water, and fully mixing to obtain a uniform-phase solution, thus obtaining the liquid-liquid two-phase absorbent for capturing carbon dioxide.
The invention also provides application of the liquid-liquid two-phase absorbent for capturing carbon dioxide in the flue gas of the coal-fired power plant, in the carbon dioxide absorption process, the mixed gas containing the carbon dioxide is introduced into the liquid-liquid two-phase absorbent, the liquid-liquid two-phase absorbent is converted into liquid-liquid two phases from a uniform liquid phase after absorbing the carbon dioxide, most carbon dioxide products are concentrated in a lower liquid phase, the lower liquid phase is a rich phase, and an upper liquid phase is a lean phase; in the carbon dioxide desorption process, heating the rich phase to release carbon dioxide; and (3) mixing the desorbed rich phase with the absorbed lean phase to form a liquid-liquid two-phase absorbent, and circularly absorbing and desorbing the carbon dioxide.
The volume percentage of carbon dioxide in the mixed gas containing carbon dioxide is 10-15%.
Conditions of the carbon dioxide absorption process: the absorption temperature is 40-50 ℃.
Conditions of the carbon dioxide desorption process: the desorption temperature is 100-120 ℃.
Example 1
Three portions of Diethylenetriamine (DETA) with the content of 20wt percent are taken, 60wt percent, 55wt percent and 50wt percent of N, N-Diethylaminoethanol (DEEA) are respectively added, and the rest is water to prepare three portions of 100g of DETA+DEEA+H 2 O liquid-liquid two-phase absorbent.
Example 2
Three portions of Diethylenetriamine (DETA) with a content of 25% by weight were taken, 55% by weight, 50% by weight and 45% by weight of N, N-Diethylaminoethanol (DEEA), respectively, the remainder being water, the remainder being the same as in example 1.
Example 3
Three portions of Diethylenetriamine (DETA) having a content of 30wt% were taken, 50wt%, 45wt% and 40wt% of N, N-Diethylaminoethanol (DEEA), respectively, and the remainder was water, and the remainder was the same as in example 1.
Comparative example 1
As comparative example 1, an aqueous solution of ethanolamine (MEA) was used, and 30wt% of ethanolamine (MEA) was mixed with water to prepare 100g of a 30wt% aqueous MEA solution.
Experimental example 1
At an absorption temperature of 40deg.C, N is contained 2 And CO 2 (CO 2 15% by volume) of the above-mentioned liquid-liquid two-phase absorbent was introduced, and the phase separation of the liquid-liquid two-phase absorbent of examples 1 to 3 was examined, while the absorption properties of the liquid-liquid two-phase absorbent of examples 1 to 3 and the 30wt% mea aqueous solution of comparative example 1 were examined.
As shown in FIG. 1, DETA+DEEA+H 2 O two-phase absorbent for absorbing CO 2 Liquid-liquid phase separation will occur later. The upper liquid phase is a lean phase, the lower liquid phase is a rich phase, and the proportion of the rich phase to the total solution is the phase ratio. In the figure DT stands for DETA and D stands for DEEA. From the figure, DETA+DEEA+H 2 The phase ratio of the O two-phase absorbent is 45-65%, and compared with 30wt% of MEA, the two-phase absorbent can reduce the volume of the regeneration solution, thereby reducing the regeneration energy consumption.
As shown in fig. 2, the absorption performance of the liquid-liquid two-phase absorbents of examples 1 to 3 and the 30wt% mea aqueous solution of comparative example 1 are shown. By CO 2 Absorption of loadThe absorption performance is improved. From the graph, as DETA concentration increases, CO 2 The absorption load also increases because at deta+deea+h 2 In the O two-phase absorbent, DEEA acts as a proton acceptor, ensuring that DETA preferentially associates with CO 2 Rather than acting as a deprotonating base, DETA thus has a higher CO 2 Absorption capacity. CO of liquid-liquid two-phase absorbent of examples 1 to 3 2 The absorption load was higher than 30wt% MEA, with the highest CO 2 The absorption load was 3.68mol/L, 39.4% higher than 30wt% MEA.
Experimental example 2
And heating and desorbing the rich phase at the desorption temperature of 120 ℃. The desorption properties of the aqueous 30wt% MEA solutions of examples 1 to 3 were examined.
As shown in FIG. 3, the results demonstrate the desorption performance of the liquid-liquid two-phase absorbents of examples 1 to 3 and the 30wt% MEA aqueous solution of comparative example 1. The desorption performance was demonstrated by the circulation capacity. From the graph, as DEEA concentration increases, the circulation capacity also increases, because of DEEA and CO 2 The reaction can form carbonate and bicarbonate which are easy to decompose, and the regeneration of the absorbent is facilitated, so that the DEEA concentration is improved, the regeneration performance of the system can be improved, and the desorption of the absorbent is faster and more thorough. The liquid-liquid two-phase absorbents of examples 1 to 3 each had a circulation capacity higher than 30wt% MEA, with the highest circulation capacity of 2.72mol/L, 58.8% higher than 30wt% MEA.
Experimental example 3
The liquid-liquid two-phase absorbents of examples 1 to 3 were examined for the regeneration energy consumption of 30wt% mea aqueous solution of comparative example 1.
As shown in FIG. 4, the results demonstrate the regeneration energy consumption of the liquid-liquid two-phase absorbents of examples 1-3 and the 30wt% MEA aqueous solution of comparative example 1. The regeneration energy consumption mainly comprises three parts: regenerated sensible heat (Qsen) and CO of absorbent 2 The heat of desorption (Qdes) of the product and the latent heat (Qlatent) carried away by the regeneration gas. As can be seen from the graph, the regeneration energy consumption of 30wt% MEA is 3.8GJ/tCO 2 ，DETA+DEEA+H 2 The regeneration energy consumption of the O two-phase absorbent is as low as 2.42GJ/tCO 2 Reduced from 30wt% MEA23.6 to 36.3 percent. This is mainly due to the reduction of sensible and latent heat, and for two-phase absorbent only CO needs to be taken 2 The rich phase is used for regeneration, so that the regeneration amount of the absorbent can be greatly reduced, the sensible heat of regeneration is further reduced, and meanwhile, the water content of the two-phase system is very low, so that the water vapor amount in the mixed gas at the top of the tower is relatively low during regeneration, and the latent heat generated by a small amount of water vapor is relatively low. The reaction heat is reduced because of DEEA and CO 2 Reaction to form HCO 3- /CO 3 2- The heat released is less than that of MEA and CO 2 And (3) reacting to form the carbamate.
In summary, DETA+DEEA+H of the present invention 2 The O liquid-liquid two-phase absorbent still has lower fractional phase ratio, higher absorption performance and desorption performance and lower regeneration energy consumption under the condition of low water content, so the invention has better industrial application prospect.
Claims (8)
1. A liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant, which is characterized in that: the water-based paint comprises Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water.
2. A liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant according to claim 1, wherein: the mass percentage concentration of the Diethylenetriamine (DETA) is 25wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 50wt%, and the balance is water.
3. A preparation method of a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant is characterized by comprising the following steps of: comprising the following steps: uniformly mixing Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water according to a proportion, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 20-30wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 40-60wt%, and the balance is water, and fully mixing to obtain a uniform-phase solution, thus obtaining the liquid-liquid two-phase absorbent for capturing carbon dioxide.
4. A method for preparing a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of coal-fired power plants according to claim 3, wherein: uniformly mixing Diethylenetriamine (DETA), N, N-Diethylaminoethanol (DEEA) and water in proportion, wherein the mass percentage concentration of the Diethylenetriamine (DETA) is 25wt%, the mass percentage concentration of the N, N-Diethylaminoethanol (DEEA) is 50wt%, and the balance is water, and fully mixing to obtain a uniform-phase solution, thus obtaining the liquid-liquid two-phase absorbent for capturing carbon dioxide.
5. Based on the application of the liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant according to claim 1 or 2, in the carbon dioxide absorption process, introducing a mixed gas containing carbon dioxide into the liquid-liquid two-phase absorbent, converting the liquid-liquid two-phase absorbent from a uniform liquid phase into liquid-liquid two-phase after absorbing carbon dioxide, wherein most carbon dioxide products are concentrated in a lower liquid phase, the lower liquid phase is a rich phase, and an upper liquid phase is a lean phase; in the carbon dioxide desorption process, heating the rich phase to release carbon dioxide; and (3) mixing the desorbed rich phase with the absorbed lean phase to form a liquid-liquid two-phase absorbent, and circularly absorbing and desorbing the carbon dioxide.
6. The use of a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant according to claim 5, wherein the volume percentage of carbon dioxide in the mixed gas containing carbon dioxide is 10-15%.
7. Use of a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant according to claim 5, conditions of the carbon dioxide absorption process: the absorption temperature is 40-50 ℃.
8. Use of a liquid-liquid two-phase absorbent for capturing carbon dioxide in flue gas of a coal-fired power plant according to claim 5, conditions of the carbon dioxide desorption process: the desorption temperature is 100-120 ℃.
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