CN110960956B - CO in flue gas is absorbed to applicable phase transition absorbent 2 Method and system of (2) - Google Patents
CO in flue gas is absorbed to applicable phase transition absorbent 2 Method and system of (2) Download PDFInfo
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- CN110960956B CN110960956B CN201911214630.8A CN201911214630A CN110960956B CN 110960956 B CN110960956 B CN 110960956B CN 201911214630 A CN201911214630 A CN 201911214630A CN 110960956 B CN110960956 B CN 110960956B
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- 239000002250 absorbent Substances 0.000 title claims abstract description 116
- 230000002745 absorbent Effects 0.000 title claims abstract description 116
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 65
- 239000003546 flue gas Substances 0.000 title claims abstract description 61
- 238000000034 method Methods 0.000 title claims abstract description 19
- 230000007704 transition Effects 0.000 title claims description 4
- 238000010521 absorption reaction Methods 0.000 claims abstract description 169
- 239000012071 phase Substances 0.000 claims abstract description 107
- 230000008859 change Effects 0.000 claims abstract description 56
- 239000007791 liquid phase Substances 0.000 claims abstract description 45
- 239000007788 liquid Substances 0.000 claims abstract description 33
- 238000005191 phase separation Methods 0.000 claims abstract description 29
- 239000006096 absorbing agent Substances 0.000 claims description 9
- 238000003795 desorption Methods 0.000 abstract description 21
- 238000012546 transfer Methods 0.000 abstract description 20
- 238000005516 engineering process Methods 0.000 abstract description 16
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000002156 mixing Methods 0.000 abstract description 4
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- 230000009467 reduction Effects 0.000 abstract description 4
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- 125000004122 cyclic group Chemical group 0.000 abstract description 2
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- 238000004064 recycling Methods 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 4
- 238000011068 loading method Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000011278 co-treatment Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
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- 238000005070 sampling Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- YLZOPXRUQYQQID-UHFFFAOYSA-N 3-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]propan-1-one Chemical compound N1N=NC=2CN(CCC=21)CCC(=O)N1CCN(CC1)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F YLZOPXRUQYQQID-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
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- 230000008929 regeneration Effects 0.000 description 1
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- 229920006395 saturated elastomer Polymers 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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Abstract
The invention relates to a method suitable for absorbing CO in flue gas by a phase-change absorbent 2 Is suitable for absorbing CO in flue gas by phase change absorbent 2 The technology adopts phase change absorbent to absorb CO in the flue gas 2 Absorbing CO 2 The phase of the solution is separated, and the CO after phase separation 2 The rich liquid is sequentially used for CO in the flue gas 2 Absorbing CO in the flue gas by using a phase change absorbent 2 And CO is adopted 2 Absorption of CO in flue gas by liquid rich phase 2 The process of (2) is carried out in different absorption towers to absorb CO in the flue gas again 2 CO of (c) 2 Desorbing the rich liquid, and separating the desorbed solution from the phase-separated CO 2 Mixing lean liquid phase and then continuously using the mixed lean liquid phase for CO in flue gas 2 Absorption is performed. The invention can effectively improve CO in the flue gas 2 Is used for realizing the absorption efficiency of the phase change absorbent and CO 2 Optimization of mass transfer efficiency in the absorption tower, realization of cyclic utilization of the phase change absorbent and reduction of CO 2 And the desorption energy consumption of the rich liquid.
Description
Technical Field
The invention relates to a method for absorbing CO in flue gas 2 In particular to a method and a system which are suitable for absorbing CO in flue gas by a phase change absorbent 2 Is suitable for absorbing CO in flue gas by phase change absorbent 2 Is an absorption system of (a).
Background
In recent years, from CO 2 The 'greenhouse effect' caused by the main greenhouse gases poses serious threat to the human living environment, and the CO is currently used 2 Emission reduction has become a human consensus. Carbon capture and sequestration (Carbon Capture and Storage, CCS) technology is a viable approach to control and curtail global carbon dioxide emissions. In CCS technology, chemical absorption method is most mature technology due to large absorption capacity, and is the most widely applied CO at present 2 The trapping technology has the problem that the regeneration energy consumption is always too high.
Researchers have been developing efficient low energy phase change absorbers for the last decade 2 Homogeneous phase and CO absorption 2 After which liquid-liquid phase separation occurs and absorbed CO 2 Concentrate on the lower liquid phase, so that only the lower liquid phase is required to be sent into the desorption device, the liquid quantity entering the desorption device is greatly reduced, the evaporation latent heat and the heating heat development energy consumption can be effectively reduced, and the low energy consumption CO is realized 2 The method is hopeful to be applied to CO in the flue gas of large-scale coal-fired power plants 2 Trapping。
Unlike conventional absorbents, phase change absorbents absorb CO 2 In the process, phase separation occurs, but at the moment, the lower liquid phase after phase separation still does not reach the saturated absorption capacity and still has a certain CO due to the influence of phase balance 2 Absorption capacity, high viscosity of the lower liquid phase after phase separation, leading to absorbent and CO 2 The mass transfer coefficient between the two is reduced, the absorption rate is obviously reduced, and the size of the absorption tower is required to be greatly increased in design, so that the equipment investment is increased. On the other hand, for a given absorber, the phase-change absorber has a large viscosity and a low absorption rate after phase separation, which results in a large reduction in throughput and a sharp increase in running cost. Because the viscosity of the phase change absorbent changes sharply before and after phase separation, and the mass transfer coefficient changes suddenly in the absorption tower, the absorption tower needs to be provided with different design requirements before and after the phase separation of the absorbent, and therefore, the optimization of the mass transfer efficiency in the same absorption tower is difficult to realize.
A high-temperature absorption tower and a low-temperature absorption tower are adopted to achieve the trade-off of CO 2 The technology of two key parameters of absorption capacity and absorbent viscosity is proposed, the upper liquid phase after phase separation of the technology returns to the low-temperature absorption tower to continuously absorb CO 2 The absorbent viscosity is reduced by the provision of a high temperature column, but this technique requires the provision of a heat exchanger between the two columns, which additionally increases investment costs. More importantly, the technology separates the upper liquid phase from the lower liquid phase when the absorbent is subjected to phase separation, so that the upper liquid phase continuously absorbs CO 2 . Among the currently reported phase change absorbers, a major class of phase change absorbers absorbs CO 2 After phase separation, the upper liquid phase has almost no absorption capacity, so the technological process of the technology can only further reduce the viscosity of the absorbent before absorption for the phase-change absorbent, but does not act on the lower liquid phase which is already phase-separated and has further absorption capacity, namely the purpose of improving the absorption capacity of the phase-change absorbent cannot be achieved. The technology has proposed the use of phase change absorbents to capture CO 2 However, the main phase change absorbent has no practical effect, and the problem of mass transfer efficiency reduction caused by the sharp increase of viscosity is not really solved.
Disclosure of Invention
To overcome the defects in the prior art, the invention provides a method suitable for absorbing CO in flue gas by a phase-change absorbent 2 Is suitable for absorbing CO in flue gas by phase change absorbent 2 Can effectively improve CO in the flue gas 2 Is used for realizing the absorption efficiency of the phase change absorbent and CO 2 Optimizing mass transfer efficiency in an absorption tower.
The technical scheme for achieving the aim of the invention is as follows: CO in flue gas is absorbed to applicable phase transition absorbent 2 The method adopts the original phase change absorbent (refers to the phase change absorbent before phase separation, can be fresh phase separation absorbent, can also be recycled phase separation absorbent or the mixture of the two) to absorb CO in the flue gas 2 Absorbing CO 2 The phase of the solution is separated, and the CO after phase separation 2 The rich liquid is sequentially used for CO in the flue gas 2 Absorbing CO in the flue gas by adopting an original phase change absorbent 2 And using split-phase CO 2 Absorption of CO in flue gas by liquid rich phase 2 Is carried out in a different absorption column.
Further, to reabsorption CO 2 Post CO 2 Desorbing the rich liquid, and separating the desorbed solution from the phase-separated CO 2 The lean liquid phase is added after mixing or recycled as the original phase change absorbent.
Further, the phase change absorbent is a phase change absorbent of an amine-organic solvent-water system.
Further, the phase change absorbent is ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water phase change absorbent.
Further, the viscosity range of the original phase change absorbent is 2-10 mPa.s.
Further, the phase separated CO 2 The viscosity of the liquid-rich phase is 10-200 mPa.s.
Generally, the operating pressures of the different absorption towers are normal pressure, and the operating temperatures in the different absorption towers are 30-60 ℃.
Suitable for phase changeThe absorbent absorbs CO in the flue gas 2 The absorption system comprises a first absorption tower, a second absorption tower and a phase separator, wherein the first absorption tower and the second absorption tower are respectively provided with an air inlet at the bottom of the tower, an air outlet at the top of the tower, an absorbent inlet at the upper part of the tower and a solution outlet at the lower part of the tower, the air inlet of the first absorption tower is communicated with the air outlet of the second absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase separator, the rich solution outlet of the phase separator is communicated with the absorbent inlet of the second absorption tower, the first absorption tower is used for the absorption reaction of an original phase-change absorbent, and the second absorption tower is used for the CO after phase separation 2 Absorption of a liquid rich phase, said phase separator being used for the absorption of CO 2 Phase separation of the original phase change absorbent.
Further, the system also includes CO 2 The solution outlet of the second absorption tower is communicated with the inlet of the desorption device, the liquid phase outlet of the desorption device is communicated with the absorbent inlet of the first absorption tower, the lean solution outlet of the phase separator is communicated with the absorbent inlet of the first absorption tower, and the desorption device is used for re-absorbing CO 2 Post CO 2 Desorption of the rich liquid.
Further, a first transfer pump is installed on an absorbent transfer pipeline connected with the absorbent inlet of the first absorption tower, and a second transfer pump is installed on a transfer pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower.
The beneficial effects of the invention are as follows:
1. the invention respectively utilizes the phase-change absorbent and the phase-change absorbent to absorb CO through different absorption towers 2 Post CO 2 CO in rich liquid relative flue gas 2 Compared with the traditional technology adopting a single absorption tower, the phase change absorbent and CO can be realized 2 The optimization of mass transfer efficiency in the absorption tower avoids the condition that the mass transfer coefficient in the absorption tower is suddenly reduced due to the rapid change of viscosity of the phase change absorbent before and after phase separation, and can effectively improve the CO content of the phase change absorbent 2 Is used for the absorption efficiency of the (a),CO can also be realized 2 Rich liquor relative to CO 2 The absorption capacity is reused, the size of the absorption tower is not required to be changed, and the equipment investment and the operation cost are reduced.
2. The invention can realize the CO treatment 2 Desorbing the rich solution and CO 2 The lean liquid phase is recycled, so that the phase change absorbent is recycled, the utilization efficiency of the phase change absorbent is improved, and the production cost is reduced.
3. The invention only uses CO 2 The rich liquid is sent to the desorption device for desorption, compared with the prior art, the solution quantity entering the desorption device can be effectively reduced, and the desorption energy consumption is reduced.
Drawings
FIG. 1 is a schematic diagram of a phase change absorber of the present invention for absorbing CO in flue gas 2 A schematic structural view of an embodiment of an absorbent system;
FIG. 2 is a schematic diagram of a phase change absorber of the present invention for absorbing CO in flue gas 2 A schematic structural view of another embodiment of the absorbent system.
Detailed Description
The invention discloses a method suitable for absorbing CO in flue gas by a phase-change absorbent 2 The method adopts a phase change absorbent (which can be called as original phase change absorbent) to absorb CO in the flue gas 2 Absorbing CO 2 The phase of the solution is separated, and the CO after phase separation 2 The rich liquid is sequentially used for CO in the flue gas 2 Absorbing CO in the flue gas by using a phase change absorbent 2 And CO is adopted 2 Absorption of CO in flue gas by liquid rich phase 2 Is carried out in a different absorption column. Further, for reabsorption of CO in the flue gas 2 CO of (c) 2 Desorbing the rich liquid, and separating the desorbed solution from the phase-separated CO 2 Mixing lean liquid phase to restore homogeneous phase and then continuously using the mixture to treat CO in flue gas 2 Absorption is performed.
In general, the method is implemented by adopting two absorption towers, namely a first absorption tower and a second absorption tower, wherein an air inlet at the bottom end of the first absorption tower is communicated with exhaust gas at the top end of the second absorption towerA port for allowing the flue gas entering the second absorption tower to be sent into the first absorption tower for CO 2 The work flow is as follows: containing CO 2 The flue gas enters the second absorption tower from the air inlet at the bottom end of the second absorption tower and then enters the first absorption tower, the phase-change absorbent enters the first absorption tower from the upper part of the first absorption tower, and the phase-change absorbent firstly absorbs CO in the first absorption tower 2 (phase-change absorbent with CO) 2 Mass transfer occurs), the phase change absorbent absorbs CO 2 The latter solution is split in the bottom of the first absorption column, preferably by a phase separator to separate the solution into CO 2 Rich liquid phase and CO 2 Lean liquid phase, high viscosity CO 2 The rich liquid phase is sent into the second absorption tower from the upper part of the second absorption tower, and is in countercurrent contact with the high-concentration flue gas entering the second absorption tower from the bottom end of the second absorption tower, so as to re-absorb CO in the flue gas 2 CO of (c) 2 The rich liquid flows out from the lower part of the second absorption tower and is sent into a desorption device, and the desorbed solution and the separated CO 2 Is sent into the first absorption tower from the upper part of the first absorption tower for recycling after the lean liquid phase is mixed and restored to be homogeneous, and is continuously used for recycling CO in the flue gas 2 Absorption is performed.
The invention respectively utilizes the phase-change absorbent and the phase-change absorbent to absorb CO through different absorption towers 2 Post CO 2 CO in rich liquid relative flue gas 2 Compared with the traditional technology adopting a single absorption tower, the phase change absorbent and CO can be realized 2 The optimization of mass transfer efficiency in the absorption tower avoids the condition that the mass transfer coefficient in the absorption tower is suddenly reduced due to the rapid change of viscosity of the phase change absorbent before and after phase separation, and can effectively improve the CO content of the phase change absorbent 2 Can also realize the absorption efficiency of CO 2 Rich liquor relative to CO 2 The absorption capacity is reused, the size of the absorption tower is not required to be changed, and the equipment investment and the operation cost are reduced. The invention can realize the CO treatment 2 Desorbing the rich solution and CO 2 Recycling of lean liquid phase is realized, thereby realizing recycling of phase change absorbent and improving phase changeThe utilization efficiency of the absorbent reduces the production cost. The invention only uses CO 2 The rich liquid is sent to the desorption device for desorption, compared with the prior art, the solution quantity entering the desorption device can be effectively reduced, and the desorption energy consumption is reduced.
The phase change absorbent is an absorbent of an amine-organic solvent-water system, and can adopt ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water.
The viscosity range of the phase change absorbent is preferably 2-10 mPas, such as 2 mPas, 5 mPas, 8 mPas or 10 mPas. Phase separated CO 2 The viscosity of the liquid-rich phase is preferably in the range of 10 to 200 mPas, such as 10 mPas, 100 mPas, 150 mPas or 200 mPas.
In general, the operating pressures of the different absorption towers are all normal pressure, and the operating temperatures in the different absorption towers are all 30-60 ℃, such as 30 ℃, 40 ℃, 50 ℃ or 60 ℃.
Referring to fig. 1 and 2, the invention also discloses a method for absorbing CO in flue gas by using the phase-change absorbent 2 Comprises a first absorption tower 1, a second absorption tower 2 and a phase separator 3, wherein the first absorption tower and the second absorption tower are respectively provided with an air inlet positioned at the bottom of the tower, an air outlet positioned at the top of the tower, an absorbent inlet positioned at the upper part of the tower and a solution outlet positioned at the lower part of the tower, and the absorption system comprises CO 2 The phase change absorbent enters the first absorption tower from an absorbent inlet at the upper part of the first absorption tower, the air inlet of the first absorption tower is communicated with an air outlet of the second absorption tower, so that the flue gas in the second absorption tower can enter the first absorption tower, a solution outlet of the first absorption tower is communicated with an inlet of a phase separator, and the phase separator is used for absorbing CO to the phase change absorbent in the first absorption tower 2 The solution after phase separation is carried out, and the rich liquid outlet of the phase separator is communicated with the absorbent inlet of the second absorption tower and is used for separating CO after phase separation 2 Feeding the rich liquid phase into the second absorption tower to make CO 2 Countercurrent flow of the rich liquid phase and the high-concentration flue gas entering from the bottom of the second absorption towerContact, continue absorbing CO in the flue gas 2 In general, the lower liquid phase after phase separation by the phase separator is a rich liquid phase.
Further, the system also includes CO 2 The desorption device 6 of the rich liquid, the solution outlet of the second absorption tower is communicated with the inlet of the desorption device and is used for absorbing CO in the flue gas again 2 CO of (c) 2 The rich liquid is sent into the desorption device for desorption, the outlet of the desorption device is communicated with the absorbent inlet of the first absorption tower, the lean liquid outlet of the phase separator is communicated with the absorbent inlet of the first absorption tower, and the rich liquid is used for desorbing the resolved solution and the separated CO 2 The lean liquid phase is sent into the first absorption tower for cyclic utilization and is continuously used for recycling CO in the flue gas 2 The absorption is usually performed such that the upper liquid phase after phase separation by the phase separator is a lean liquid phase. To facilitate the solution after resolution and the CO after phase separation 2 The lean liquid phase is mixed, and the lean liquid phase are sent to a mixing device to be mixed and restored to be homogeneous phase, and then sent to the first absorption tower from an absorbent inlet of the first absorption tower.
In general, the absorbent delivery pipe with the absorbent inlet of the first absorption tower is provided with a first delivery pump 4 for delivering phase-change absorbent, and the delivery pipe between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower is provided with a second delivery pump 5 for delivering CO 2 And the rich liquid phase is conveyed, and other conveying pipelines can be provided with proper conveying pumps so as to facilitate the conveying of substances in the pipelines.
Experimental example 1:60 ℃ flue gas (CO) 2 Concentration 20vol.% of 1.2. 1.2 m) 3 The flow rate of/h was fed from the bottom of the second absorption column, and the phase-change absorbent A (initial viscosity: 7.7 mPa.s) was pumped from the first transfer pump to the top of the first absorption column at a flow rate of 20L/h. Phase change absorbent for absorbing CO 2 The solution after passing through the phase separator, the lower liquid phase is pumped into the top of the second absorption tower by the second delivery pump, and CO is absorbed in the second absorption tower 2 . For CO at the bottom of the second absorption tower 2 The rich liquid was sampled to give a viscosity of 29 mPas, CO 2 The load was 2.2mol/kg and the required absorption time was 4 hours in total.
Experimental example 2:60 ℃ flue gas (CO) 2 Concentration 20vol.% of 2.2. 2.2 m) 3 The flow rate of/h was fed from the bottom of the second absorption column, and the phase-change absorbent B (initial viscosity: 5.2 mPa.s) was pumped from the first transfer pump to the top of the first absorption column at a flow rate of 20L/h. Phase change absorbent for absorbing CO 2 The solution after passing through the phase separator, the lower liquid phase is pumped into the top of the second absorption tower by the second delivery pump, and CO is absorbed in the second absorption tower 2 . For CO at the bottom of the second absorption tower 2 Sampling the rich solution to obtain a viscosity of 77 mPas, CO 2 The load was 2.8 mol/kg and the required absorption time was 2.5h in total.
Experimental example 3: flue gas (CO) at 30 DEG C 2 Concentration 50vol.% of 1.2. 1.2 m) 3 The flow rate of/h was fed from the bottom of the second absorption column, and the phase-change absorbent A (initial viscosity: 7.7 mPa.s) was pumped from the first transfer pump to the top of the first absorption column at a flow rate of 20L/h. Phase change absorbent for absorbing CO 2 The solution after passing through the phase separator, the lower liquid phase is pumped into the top of the second absorption tower by the second delivery pump, and CO is absorbed in the second absorption tower 2 . For CO at the bottom of the second absorption tower 2 The rich liquid was sampled to give a viscosity of 49 mPas, CO 2 The load was 2.4mol/kg and the required absorption time was 4 hours in total.
Experimental example 4:40 ℃ flue gas (pure CO) 2 ) At 2.2m 3 The flow rate of/h was fed from the bottom of the second absorption column, and the phase-change absorbent B (initial viscosity: 5.2 mPa.s) was pumped from the first transfer pump to the top of the first absorption column at a flow rate of 20L/h. Phase change absorbent for absorbing CO 2 The solution after passing through the phase separator, the lower liquid phase is pumped into the top of the second absorption tower by the second delivery pump, and CO is absorbed in the second absorption tower 2 . For CO at the bottom of the second absorption tower 2 Sampling the rich phase to obtain a viscosity of 127 mPa.s, CO 2 The load was 3.5mol/kg and the required absorption time was 2.5h in total.
As can be seen from various experimental examples, the technology of the invention is fully applicable to CO in flue gas 2 Absorption is performed.
Comparative example 1 (principle of conventional technology): 60 ℃ flue gas (CO) 2 Concentration 20vol.% of 1.2. 1.2 m) 3 The flow rate of/h enters from the bottom of the second absorption tower, and the phase-change absorbent A (with initial viscosity of 7.7 mPa.s) is pumped into the top of the first absorption tower by a first conveying pump to circularly absorb CO 2 The flow is 20L/h, and CO is absorbed by the phase-change absorbent after absorption for 4h 2 Standing and layering the solution, taking down the liquid phase to measure CO 2 The loading was 1.4 mol/kg.
As can be seen from a comparison of experimental example 1 and comparative example 1, CO was absorbed in the same time 2 Experimental example 1 enables CO 2 CO in rich solution 2 The load is increased from 1.4 mol/kg to 2.2mol/kg, compared with the prior art, the technology of the invention has the advantages of CO 2 The absorption efficiency of (a) is greatly improved.
Comparative example 2:60 ℃ flue gas (CO) 2 Concentration 20vol.% of 1.2. 1.2 m) 3 The flow rate of/h was fed from the bottom of the second absorption column, and the phase-change absorbent A (initial viscosity: 7.7 mPa.s) was pumped from the first transfer pump to the top of the first absorption column at a flow rate of 20L/h. Phase change absorbent for absorbing CO 2 The solution after passing through a phase separator is sampled to measure the loading amount of the upper liquid phase to be 0.2 mol/kg, the upper liquid phase is pumped into the top of the first absorption tower to be circularly absorbed for 5 hours, and the CO is sampled to measure 2 The load was still 0.2 mol/kg.
CO before and after recycling of the upper liquid phase after phase separation in comparative example 2 2 Comparison of the loadings shows that the present technology is applicable to phase change absorbers (for absorbing CO 2 The upper liquid phase of the separated solution is free of CO 2 Absorbent with absorption capacity) for CO in flue gas 2 Is not limited to the absorption of (a).
Claims (3)
1. CO in flue gas is absorbed to applicable phase transition absorbent 2 Characterized in that the original phase-change absorbent is adopted to absorb CO in the flue gas 2 Absorbing CO 2 The phase of the solution is separated, and the CO after phase separation 2 The rich liquid is sequentially used for CO in the flue gas 2 Absorbing CO in the flue gas by adopting an original phase change absorbent 2 And using split-phase CO 2 Absorbing C in flue gas by rich liquid phaseO 2 Is carried out in a different absorption tower to re-absorb CO 2 Post CO 2 Desorbing the rich liquid, and separating the desorbed solution from the phase-separated CO 2 The poor liquid phase is mixed and then added or recycled as an original phase-change absorbent, wherein the phase-change absorbent is an ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water phase-change absorbent, the viscosity range of the original phase-change absorbent is 2-10 mPa.s, the operating pressures of different absorption towers are normal pressure, and the operating temperatures in the different absorption towers are 30-60 ℃.
2. A method according to claim 1, suitable for use in a phase change absorber for absorbing CO in flue gas 2 Characterized by the phase separated CO 2 The viscosity of the liquid rich phase is in the range of 10 to 200 mPas.
3. A phase change absorbent suitable for absorbing CO in flue gas using a method according to any one of claims 1-2 2 The absorption system is characterized by comprising a first absorption tower, a second absorption tower and a phase separator, wherein the first absorption tower and the second absorption tower are respectively provided with an air inlet positioned at the bottom of the tower, an air outlet positioned at the top of the tower, an absorbent inlet positioned at the upper part of the tower and a solution outlet positioned at the lower part of the tower, the air inlet of the first absorption tower is communicated with the air outlet of the second absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase separator, the rich liquid outlet of the phase separator is communicated with the absorbent inlet of the second absorption tower, the first absorption tower is used for the absorption reaction of an original phase-change absorbent, and the second absorption tower is used for CO after phase separation 2 Absorption of a liquid rich phase, said phase separator being used for the absorption of CO 2 The phase of the original phase-change absorbent after the phase separation, an absorbent conveying pipeline communicated with an absorbent inlet of the first absorption tower is provided with a first conveying pump, and a conveying pipeline between a rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower is provided with a second conveying pump.
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| CN113350973B (en) * | 2021-07-08 | 2022-07-22 | 浙江工业大学 | Multistage phase separation process method for treating carbon dioxide in flue gas |
| CN113731118A (en) * | 2021-09-09 | 2021-12-03 | 湖南大学 | Liquid-liquid phase change absorbent for capturing carbon dioxide |
| CN114159954B (en) * | 2021-12-07 | 2024-03-15 | 兰州理工大学 | Phase-change solvent coupling membrane for separating flue gas CO 2 Systems and methods of (1) |
| CN114452779B (en) * | 2022-03-09 | 2022-09-27 | 清华大学 | Carbon dioxide capture system based on phase change absorbent |
| CN114904364B (en) * | 2022-05-30 | 2024-04-09 | 万华化学集团股份有限公司 | Tail gas treatment method for polyacrylic acid device |
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